WO1998015350A2 - Catalyseurs d'hydrogenation, procede de fabrication de ces catalyseurs et leur utilisation pour preparer du peroxyde d'hydrogene - Google Patents
Catalyseurs d'hydrogenation, procede de fabrication de ces catalyseurs et leur utilisation pour preparer du peroxyde d'hydrogene Download PDFInfo
- Publication number
- WO1998015350A2 WO1998015350A2 PCT/BE1997/000115 BE9700115W WO9815350A2 WO 1998015350 A2 WO1998015350 A2 WO 1998015350A2 BE 9700115 W BE9700115 W BE 9700115W WO 9815350 A2 WO9815350 A2 WO 9815350A2
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- catalyst
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- palladium
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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
- B01J23/48—Silver or 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0205—Impregnation in several steps
Definitions
- Hydrogenation catalysts process for the manufacture of these catalysts and their use for preparing hydrogen peroxide
- the present invention relates to hydrogenation catalysts based on palladium, platinum or rhodium deposited on supports of zirconium and silicon oxides, their manufacturing process and their use in hydrogenation reactions and in particular for preparing hydrogen peroxide.
- patent application EP-A1-0149816 describes particular catalysts based on palladium, zirconium oxide and silica.
- the object of the present invention is to provide other hydrogenation catalysts which have a high and stable catalytic activity.
- Another object of the present invention is to provide hydrogenation catalysts which have a high catalytic selectivity.
- the catalysts according to the invention when used for the synthesis of hydrogen peroxide by the AO process (auto-oxidation process), limit the formation of degradation products.
- the invention relates to hydrogenation catalysts based on palladium, platinum or rhodium on a support of zirconium and silicon oxides comprising at least one other metal M and / or in which the support does not is not in the physical form of airgel.
- the invention also relates to the process for the manufacture of these catalysts, as well as to the use of these catalysts in hydrogenation reactions and in particular for preparing hydrogen peroxide.
- the catalysts comprise, on the one hand, palladium, platinum or rhodium, palladium being preferred, and, on the other hand, at least one other metal M.
- the metal M can be chosen from the group consisting of silver, copper, gold, germanium, tin, iron, tellurium, nickel and their mixtures.
- the metal M is preferably chosen from silver, copper and gold Particularly preferably, the metal M is silver or copper Excellent results have been obtained by combining palladium and silver
- the catalysts of the first variant of the invention preferably consist essentially of of palladium, platinum or rhodium and another metal M, on a support of zirconium and silicon oxides
- the support of the catalysts according to the invention contains zirconium and silicon oxides
- the support can be in crystalline, partially crystalline, amorphous or partially amorphous form
- the support is advantageously amorphous II preferably has a homogeneous distribution between zirconium oxide and silicon oxide
- a homogeneous distribution between zirconium oxide and silicon oxide is understood to mean a distribution such that the experimental Zr / Si ratio, measured by X-ray photoelectron spectroscopy (XPS), does not differ more 20% of the theoretical Zr / Si ratio established by calculation on the basis of the chemical composition of the support.
- Particularly preferred are the supports in which the difference between the experimental Zr / Si ratio measured by XPS and the theoretical Zr / Si ratio does not exceed not 10%
- the presence of the metal M in the catalysts according to the invention as defined above is optional.
- the support must not be in the physical form of an airgel De such catalysts can be used in the liquid phase without exhibiting the filtration disadvantages observed with aerogel-based catalysts.
- the palladium, platinum or rhodium and the metal M may be in the elementary state or in the form of a compound such as a salt or an oxide
- catalysts preferably comprise palladium, platinum or rhodium and metal M in the elementary state
- the amount of palladium, platinum or rhodium in the catalysts is advantageously at least 0.1%, preferably at least at least 0.2% by weight relative to the total weight of the catalyst, that is to say of all of the metal compounds and of the support.
- an amount is preferably used.
- the amount of palladium, platinum or rhodium does not exceed 5% of the weight of the catalyst. Preferably, it does not exceed 4% or even 3%.
- the amount of metal M in the catalysts of the first variant of the invention is advantageously at least 0.1%, preferably at least 0.2% by weight relative to the weight of the catalyst. Usually, the amount of this metal M does not exceed 5% by weight relative to the weight of the catalyst Preferably, it does not exceed 4%
- the weight ratio of palladium, platinum or rhodium to metal M is preferably at least 0.05. In a particularly preferred manner, this weight ratio is at least minus 0, 1 In a very particularly preferred manner, this ratio is at least 0.25 Preferably, the weight ratio of palladium, platinum or rhodium to metal M does not exceed 20 In a particularly preferred manner, this ratio does not exceed 10 In a very particularly preferred manner, this ratio does not exceed 4
- the amount of zirconium oxide in the catalysts is advantageously at least 1%, preferably at least 2% by weight relative to the weight of the catalyst. Usually, the amount of zirconium oxide does not exceed 10% by weight. weight relative to the weight of the catalyst Preferably, it does not exceed 5%
- the amount of silicon oxide generally represents at least 75% by weight relative to the weight of the catalyst, in particular at least 80%, or even 85%
- the amount of silicon oxide is usually less than or equal to 98.8% , especially 95%
- Catalysts of the first variant of the invention giving good results comprise from 0.5 to 2.5% of Pd, Pt or Rh by weight relative to the weight of the catalyst, from 0.5 to 2.5% of metal M by weight relative to the weight of the catalyst, from 4 to 6% of Zr ⁇ 2 by weight relative to the weight of the catalyst, and from 89 to 95% of Si ⁇ 2 by weight relative to the weight of the catalyst
- Catalysts of the second variant of the invention which give good results comprise from 15 to 25 g of Pd / kg of catalyst, from 40 to 60 g of Zr ⁇ 2 / g of catalyst, from 945 to 915 g of Si ⁇ 2 / kg of catalyst
- the catalysts according to the invention can also optionally comprise at least one additional metal chosen from the metals of group IB, IIB, IIIA, IVA, VA and VIII, in the elementary state or in the form of a composed of this metal (the designation of the groups is made according to the CAS nomenclature as reproduced in the CRC Handbook of Chemistry and Physics, 75th Edition, 1994-1995, DR Lide, cover page). Where appropriate, the quantity of this additional metal does not exceed 50% by weight of the overall weight of palladium, platinum or rhodium and of metal M.
- the catalysts of the invention can be prepared by the usual techniques, such as for example for the catalysts of the first variant, by co-impregnation of the metals on the support, by co-precipitation of the metals on the support or by successive deposits of metals on the support.
- the catalysts of the first variant according to the invention are prepared by successive deposits, on the one hand, of palladium, platinum or rhodium and, on the other hand, of metal M in any order on a support of oxides of zirconium and silicon by impregnation.
- the support is impregnated, first, with palladium, platinum or rhodium and, then, with the other metal M.
- the impregnation of the support can be carried out using solutions containing the metallic constituents of the catalyst.
- the impregnating solutions are preferably aqueous saline solutions.
- the salts used for this purpose are in particular chlorides, nitrates, acetates or ammoniacal complexes.
- the metal M is deposited by impregnating a Pd / Si ⁇ 2.ZrC> 2, Pt / Si ⁇ 2-Zr ⁇ 2 or Rh / Si ⁇ 2.ZrC> 2 catalyst with a solution containing the metallic constituent M under a reducing atmosphere. such as for example a hydrogen atmosphere.
- the deposition of the metal M by reduction with hydrogen or by any other form of reduction also leads to the reduction of palladium, platinum or rhodium.
- the catalysts can then be filtered, washed and dried.
- the Pd.Ag/Si ⁇ 2-Zr ⁇ 2 catalysts can be prepared by suspending a Pd / Si ⁇ 2-Zr ⁇ 2 catalyst in a solution of AgN03 and reducing the metals by bubbling hydrogen.
- the Pd.Cu/Si ⁇ 2- r ⁇ 2 catalysts can be prepared in the same way starting from a CuCl2 solution.
- the catalysts of the invention unexpectedly exhibit a catalytic selectivity much higher than that observed with the catalysts described in patent application EP-A1-0009802.
- the catalysts according to the present invention are suitable for all types of hydrogenation catalysis Consequently, the invention also relates to their use in hydrogenation reactions.
- Examples of hydrogenation reactions that may be mentioned include the hydrogenation of alkynes to alkenes, hydrogenation of CO to methanol and reduction of unsaturated aldehydes to unsaturated alcohols
- the catalysts according to the invention are used with very good results in the processes for manufacturing hydrogen peroxide Consequently, the invention relates also on a process for manufacturing hydrogen peroxide in their presence
- a process for the synthesis of hydrogen peroxide which has given particularly advantageous results in the presence of the catalysts of the invention is the process for the synthesis of hydrogen peroxide known as the AO process or the anthraquinone process This process is described in particular in ULLMANN's Encyclopedia of Industrial Chemistry - 5th Edition, 1989, Vol. A13, p. 443 et seq.
- the palladium catalysts according to the present invention give excellent results, in particular those of the first variant, especially when the metal M is silver or copper.
- the examples which follow are intended to illustrate the present invention without however limiting its scope.
- Example 1 R - Synthesis of a Pd / ZrC catalyst> 2 SiC> 2, according to example 2 of European patent application 0 009 802
- the wet filtration product was resuspended in 45 ml of demineralized water, then 4.75 ml of a solution of P Cl2 dissolved in HCl (25 g Pd / 1 HCl N) was then added to the suspension, then 0 , 37 ml of a 0.5 molar aqueous solution in
- Catalyst support obtained ZrU2 content in g / kg (emission spectrometry) - 44 BET surface in m * -7g (adsorption / desorption of N2) 292 351 pore volume in cm-Vg 1.2 1 25 average pore diameter in nm 9 1 1 Pd content in g / kg (quantities used) - 20 dispersion of Pd in% (adsorption / desorption of CO) - 23 surface occupied by the metal in m?
- Catalyst support obtained Zr ⁇ 2 content in g / kg (emission spectrometry) 49 49 BET surface in m -Vg (adsorption / desorption of N2) 291 242 pore volume in cm-Vg 1.6 1, 1 mean pore diameter in nm 12 8 Pd content in g / kg (quantities used) - 20 Pd dispersion in% (adsorption / desorption of CO) - 10 surface occupied by the metal in m ⁇ Pd / g of catalyst - 0.9 ratio Zr / Si experimental (XPS spectroscopy) - 0.026 theoretical established by calculation _ 0.025 number of acid sites / g SU pp 0r t (NH3 adsorption) 2.5 10 TM
- Example 3 Synthesis of a Pd / Si ⁇ 2 catalyst, according to Example 2 of European patent application 0 009 802 but without the use of Zr0
- the method used is that of Example 1R, except that the zirconium salt is not added.
- the characteristics of the support used and of the synthesized catalyst are presented below.
- Catalyst support obtained BET surface in m * - / g (emission spectrometry) 292 292 pore volume in cm- '/ g (adsorption desorption of N2) 1, 2 1.2 mean pore diameter in nm 9 9 Pd content in g / kg (quantities used) - 20 dispersion of Pd in% (adsorption / desorption of CO) - 10 surface occupied by the metal in rr - Pd / g of catalyst - 0.9 number of acid sites / g SU pp 0r1 ; (NH3 adsorption) 1, 1 10 TM
- the catalysts of Examples 1R, 2 and 3R were evaluated from the point of view of their activity and their selectivity of hydrogenation of amylanthraquinone (AQ) in solution in a diisobutylcarbinol-Solvesso 150 mixture.
- the initial rate of consumption of hydrogen was measured and the importance of the transformation processes of amylanthraquinone into amyltetrahydroanthraquinone (ATQ), amyloxanthrone (AO) and amylanthrone (AA) as well as the transformation of amyltetrahydroanthraquinone into amyltetrahydrodihydrooxanthrone (ATDO) are expressed as a function the amount of hydrogen peroxide produced over time.
- Procedure for evaluating catalysts in a continuous hydrogenation reactor the installation consisted of a hydrogenator, an oxidizer and an extraction column placed in series, the oxidized working solution being recycled to the hydrogenator after extraction of the hydrogen peroxide produced by Oxidation with oxygen of hydroanthraquinone, produced in the hydrogenator
- the working solution consisted of amylanthraquinone at 70 g / kg in the mixture diisobutylcarbinol (20% by weight) -Solvesso 150 (80% by weight)
- the total volume of working solution was 1,260 ml and its flow rate 6 ml / min
- the temperature in the hydrogenator was 50 ° C, the hydrogen pressure of 18 bar absolute and the catalyst concentration of 100 g / 1
- the time average residence time of the working solution in the hydrogenator was 33 min
- the oxidizer operated at 45 ° C.
- composition of the working solution was established by HPLC chromatography and its evolution followed over time and according to the quantity of hydrogen peroxide produced
- selectivity of the catalysts was established on the basis of the quantities of AQ transformed into ATQ, AO and AA, and of ATDO produced from ATQ, referred to a unit quantity of peroxide hydrogen produced
- Example 4 5 6 operating mode Catalyst implemented IR 2 3R relative catalytic activity 1 2 1 3 1 0 batch degradation rate of AQ -1 8 -1 1 -1 9 continuous rate of formation of ATQ 1 4 0 5 1 5 continuous formation speed of AO 0 2 0 3 0 2 continuous formation speed of AA 0 2 0 2 0 2 continuous degradation rate of ATQ -0 2 0 0 -0 1 continuous formation speed of ATDO 0.06 0 004 0 08 continuous
- Pd Cu / Si ⁇ 2 r ⁇ 2 catalysts containing respectively 0.5% (ex 10) and 0.9% (ex 1 1) of copper (by weight relative to the weight of the catalyst) were prepared according to the same procedure as the Pd Ag / SiO2 Zr ⁇ 2 catalysts of Examples 7 to 9 except that the AgN03 solution was replaced by a solution of CuCl 2 2H 2 O at 26.8 g / kg (10 g / 1 in Cu ++ )
- Examples 12 and 13 Hydrogenation of a mixture of amylanthraquinone and amyltetrahydroanthraquinone continuously by the Pd / Si ⁇ 2 Zr ⁇ 2and Pd Ag] oySi ⁇ 2 Zr ⁇ 2 catalysts according to the invention
- the catalysts of Examples 2 and 8 were evaluated from the point of view of their activity in regime, of the evolution of their activity over time and from the point of view of their selectivity for hydrogenation of a mixture of amylanthraquinone ( AQ) and amyltetrahydroanthraquinone (ATQ) continuously in solution in a DBC-S 150 mixture
- the test installation consists of a hydrogenator, an oxidizer and an extraction column placed in series.
- Hydrogen peroxide is produced by oxygen oxidation of amylanthrahydroquinone (AQH) and l 'amyltetrahydroanthrahydroquinone (ATQH) produced in the hydrogenator
- AQH amylanthrahydroquinone
- ATQH l 'amyltetrahydroanthrahydroquinone
- the working solution consists of amylanthraquinone at 25 g / kg and amyltetrahydroanthraquinone at 75 g / kg dissolved in the DBC-S 150 mixture (20/80)
- the total volume of the working solution is 1260 ml and its flow rate is 6 ml / min
- the temperature in the hydrogenator is 55 ° C and the pressure d hydrogen of 2 bar absolute
- the concentration of the catalyst is adapted to compensate for the initial de
- FIGS. 1 to 3 The results are presented in FIGS. 1 to 3. They clearly demonstrate the influence of the addition of silver on the activity under catalyst regime, on the evolution of its activity over time and on its selectivity.
- the graph in FIG. 1 compares the evolution of the activity of the catalyst Pd Ag ⁇ o / 0 / S ⁇ 2 Zrt> 2 (example 13) to that of the catalyst Pd / S ⁇ 2 Zr ⁇ 2 (example 12)
- the curves represent the evolution of quinones hydrogenated (mixture of AQH and ATQH) produced per g of catalyst, depending on the cumulative amount of hydrogen peroxide produced
- the graph in FIG. 2 represents the change in the concentration of amyltetrahydrodihydroanthraquinone (ATDQ) as a function of the cumulative amount of hydrogen peroxide produced
- the graph in FIG. 3 represents the change in the concentration of amyltetrahydrodihydrooxanthrone (ATDO) as a function of the cumulative amount of hydrogen peroxide produced
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BR9712193-2A BR9712193A (pt) | 1996-10-04 | 1997-10-03 | Catalisadores de hidrogenação à base de paládio, platina ou ródio, sobre um suporte de óxidos de zircónio e de silício, processo de fabricação e utilização dos mesmos, e, processo de fabricação de peróxido de hidrogênio. |
US09/269,877 US6306359B1 (en) | 1996-10-04 | 1997-10-03 | Hydrogenation catalysts, method for making same and use thereof for preparing hydrogen peroxide |
AU44469/97A AU4446997A (en) | 1996-10-04 | 1997-10-03 | Hydrogenation catalysts, method for making same and use thereof for preparing hydrogen peroxide |
EP97942722A EP0930938A2 (fr) | 1996-10-04 | 1997-10-03 | Catalyseurs d'hydrogenation, procede de fabrication de ces catalyseurs et leur utilisation pour preparer du peroxyde d'hydrogene |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BE9600835A BE1010665A3 (fr) | 1996-10-04 | 1996-10-04 | Catalyseurs d'hydrogenation et leur utilisation pour preparer du peroxyde d'hydrogene. |
BE9600835 | 1996-10-04 | ||
BE9700743 | 1997-09-11 | ||
BE9700743A BE1011364A6 (fr) | 1997-09-11 | 1997-09-11 | Catalyseurs d'hydrogenation, procede de fabrication de ces catalyseurs et leur utilisation pour preparer du peroxyde d'hydrogene. |
Publications (2)
Publication Number | Publication Date |
---|---|
WO1998015350A2 true WO1998015350A2 (fr) | 1998-04-16 |
WO1998015350A3 WO1998015350A3 (fr) | 1998-07-30 |
Family
ID=25663057
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/BE1997/000115 WO1998015350A2 (fr) | 1996-10-04 | 1997-10-03 | Catalyseurs d'hydrogenation, procede de fabrication de ces catalyseurs et leur utilisation pour preparer du peroxyde d'hydrogene |
Country Status (5)
Country | Link |
---|---|
US (1) | US6306359B1 (fr) |
EP (1) | EP0930938A2 (fr) |
AU (1) | AU4446997A (fr) |
BR (1) | BR9712193A (fr) |
WO (1) | WO1998015350A2 (fr) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2013053617A1 (fr) | 2011-10-11 | 2013-04-18 | Solvay Sa | Procédé pour la production de peroxyde d'hydrogène |
WO2013053616A1 (fr) | 2011-10-11 | 2013-04-18 | Solvay Sa | Procédé pour la production de peroxyde d'hydrogène |
EP2639200A1 (fr) | 2012-03-13 | 2013-09-18 | Solvay Sa | Installation de production de peroxyde d'hydrogène et procédé l'utilisant |
WO2013160163A1 (fr) | 2012-04-27 | 2013-10-31 | Solvay Sa | Catalyseurs d'hydrogénation, leur procédé de fabrication et leur utilisation pour la préparation de peroxyde d'hydrogène |
WO2014001133A1 (fr) | 2012-06-27 | 2014-01-03 | Solvay Sa | Catalyseur d'hydrogénation, procédé de fabrication de celui-ci et procédé pour préparer du peroxyde d'hydrogène |
EP2705901A1 (fr) | 2012-09-06 | 2014-03-12 | Solvay SA | Catalyseurs d'hydrogénation, procédé de fabrication associé et son utilisation pour préparer du peroxyde d'hydrogène |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6420613B1 (en) * | 1999-03-09 | 2002-07-16 | Tokuyama Corporation | Process for preparing reductants of unsaturated organic compounds by the use of trichlorosilane and reducing agents |
EP1101733B1 (fr) * | 1999-11-22 | 2005-12-28 | Akzo Nobel N.V. | Procédé et composition pour la production de l'eau oxygénée |
US7390768B2 (en) * | 2002-01-22 | 2008-06-24 | The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration | Stabilized tin-oxide-based oxidation/reduction catalysts |
CN106486687B (zh) * | 2016-11-21 | 2019-03-19 | 重庆大学 | 光催化产过氧化氢与光催化燃料电池耦合系统 |
KR102044382B1 (ko) * | 2017-08-16 | 2019-11-13 | 한국과학기술연구원 | 과산화수소 합성용 촉매 및 이를 이용한 과산화수소 합성 방법 |
CN109833901A (zh) * | 2017-11-29 | 2019-06-04 | 中国科学院大连化学物理研究所 | 一种高分散负载型浆态床加氢颗粒催化剂及其制备方法 |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0009802A1 (fr) * | 1978-10-02 | 1980-04-16 | E.I. Du Pont De Nemours And Company | Catalyseur d'hydrogénation Pd/SiO2, procédé pour préparer ce catalyseur et son utilisation dans la production du peroxyde d'hydrogène |
EP0149816A1 (fr) * | 1983-12-27 | 1985-07-31 | Stauffer Chemical Company | Aéogels d'oxydes inorganiques et leur préparation |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4007256A (en) * | 1975-04-11 | 1977-02-08 | Shell Oil Company | Catalytic production of hydrogen peroxide from its elements |
US4240933A (en) * | 1979-02-26 | 1980-12-23 | E. I. Du Pont De Nemours And Company | Pd/SiO2 Hydrogenation catalyst suitable for H2 O2 manufacture |
DE3166782D1 (en) * | 1980-04-23 | 1984-11-29 | Rhone Poulenc Spec Chim | Oxidation process of hydrogen sulfide and organic compounds of sulfur |
US4601996A (en) * | 1984-11-13 | 1986-07-22 | Chevron Research Company | Hydrofinishing catalyst comprising palladium |
-
1997
- 1997-10-03 AU AU44469/97A patent/AU4446997A/en not_active Abandoned
- 1997-10-03 WO PCT/BE1997/000115 patent/WO1998015350A2/fr not_active Application Discontinuation
- 1997-10-03 US US09/269,877 patent/US6306359B1/en not_active Expired - Fee Related
- 1997-10-03 BR BR9712193-2A patent/BR9712193A/pt unknown
- 1997-10-03 EP EP97942722A patent/EP0930938A2/fr not_active Withdrawn
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0009802A1 (fr) * | 1978-10-02 | 1980-04-16 | E.I. Du Pont De Nemours And Company | Catalyseur d'hydrogénation Pd/SiO2, procédé pour préparer ce catalyseur et son utilisation dans la production du peroxyde d'hydrogène |
EP0149816A1 (fr) * | 1983-12-27 | 1985-07-31 | Stauffer Chemical Company | Aéogels d'oxydes inorganiques et leur préparation |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2013053617A1 (fr) | 2011-10-11 | 2013-04-18 | Solvay Sa | Procédé pour la production de peroxyde d'hydrogène |
WO2013053616A1 (fr) | 2011-10-11 | 2013-04-18 | Solvay Sa | Procédé pour la production de peroxyde d'hydrogène |
US9617153B2 (en) | 2011-10-11 | 2017-04-11 | Solvay Sa | Process for producing hydrogen peroxide |
US10793433B2 (en) | 2011-10-11 | 2020-10-06 | Solvay Sa | Process for producing hydrogen peroxide |
EP2639200A1 (fr) | 2012-03-13 | 2013-09-18 | Solvay Sa | Installation de production de peroxyde d'hydrogène et procédé l'utilisant |
WO2013135491A1 (fr) | 2012-03-13 | 2013-09-19 | Solvay Sa | Installation de production de peroxyde d'hydrogène et procédé l'utilisant |
WO2013160163A1 (fr) | 2012-04-27 | 2013-10-31 | Solvay Sa | Catalyseurs d'hydrogénation, leur procédé de fabrication et leur utilisation pour la préparation de peroxyde d'hydrogène |
WO2014001133A1 (fr) | 2012-06-27 | 2014-01-03 | Solvay Sa | Catalyseur d'hydrogénation, procédé de fabrication de celui-ci et procédé pour préparer du peroxyde d'hydrogène |
EP2705901A1 (fr) | 2012-09-06 | 2014-03-12 | Solvay SA | Catalyseurs d'hydrogénation, procédé de fabrication associé et son utilisation pour préparer du peroxyde d'hydrogène |
WO2014037300A1 (fr) * | 2012-09-06 | 2014-03-13 | Solvay Sa | Procédé de production de peroxyde d'hydrogène |
Also Published As
Publication number | Publication date |
---|---|
EP0930938A2 (fr) | 1999-07-28 |
WO1998015350A3 (fr) | 1998-07-30 |
US6306359B1 (en) | 2001-10-23 |
BR9712193A (pt) | 1999-08-31 |
AU4446997A (en) | 1998-05-05 |
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