WO2019072655A1 - Catalyseur utilisé pour la production d'acétate de vinyle - Google Patents

Catalyseur utilisé pour la production d'acétate de vinyle Download PDF

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Publication number
WO2019072655A1
WO2019072655A1 PCT/EP2018/076853 EP2018076853W WO2019072655A1 WO 2019072655 A1 WO2019072655 A1 WO 2019072655A1 EP 2018076853 W EP2018076853 W EP 2018076853W WO 2019072655 A1 WO2019072655 A1 WO 2019072655A1
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WO
WIPO (PCT)
Prior art keywords
palladium
gold
supported catalyst
catalyst
vinyl acetate
Prior art date
Application number
PCT/EP2018/076853
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German (de)
English (en)
Inventor
Willibald Dafinger
Roland Heidenreich
Günther RUDOLF
Original Assignee
Wacker Chemie Ag
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Wacker Chemie Ag filed Critical Wacker Chemie Ag
Publication of WO2019072655A1 publication Critical patent/WO2019072655A1/fr

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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
    • 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
    • B01J21/16—Clays or other mineral silicates
    • 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
    • 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
    • B01J35/51—Spheres
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/04—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds
    • C07C67/05—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation
    • C07C67/055—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation in the presence of platinum group metals or their compounds

Definitions

  • the invention relates to a catalyst for the preparation of vinyl acetate (VAM catalyst), and to processes for the preparation of vinyl acetate using the VAM catalyst.
  • VAM catalyst a catalyst for the preparation of vinyl acetate
  • Vinyl acetate monomer can be prepared in a continuous process with recycling of the purified product stream (cycle gas process).
  • cycle gas process a heterogeneous katalysier ⁇ th gas phase reaction of ethylene reacts ⁇ gerkatalysatoren with acetic acid and oxygen to Trä, which may be generally contain palladium and alkali metal salts on a support material and additionally doped with more gold.
  • a Pd / Au catalyst mixture is used with potassium acetate as a promoter.
  • VAM exo ⁇ thermal reaction
  • the major secondary reaction is the total ethylene oxidation to C0 2 :
  • recycle gas recycle gas
  • the condensed products vinyl acetate and water and unreacted acetic acid in a multi-stage, usually operated with heating steam, distillation process can be separated.
  • the cycle gas is optionally compressed, re-added with the educts, and passed into the fixed bed tube reactor for gas phase oxidation.
  • a supported catalyst is preferably described consisting of silicic acid which is charged with 0.1 to 6% by weight of palladium and 0.01 to 10% by weight of gold and 1 to 20% by weight of alkali metal compound.
  • DE 27 16 154 C2 describes a shell catalyst which contains Pd and Au distributed in a surface layer of the catalyst support which extends less than 0.5 mm from the support surface.
  • WO 2008/071610 A2 describes a process for the preparation of supported catalysts based on pyrogenic metal oxides without the addition of binders.
  • WO 2008/145389 A2 relates to a coated with Pd and Au shell catalyst of bentonite with a surface ⁇ 130 m 2 / g. It has been found that the smaller the thickness of the Pd / Au shell, the higher the selectivity in gas phase oxidation to VAM. To improve the selectivity of Pd / Au coated catalysts is in the WO 2008/145392 A2 proposed to dope the carrier with hafnium oxide. For the same purpose, in WO 2008/145394 A2 the substrate made of phyllosilicate is doped with zirconium oxide, it being found that the smaller the thickness of the Pd / Au shell, the higher the VAM selectivity. The doping of the support material of Pd / Au shells
  • WO 2008/145395 A2 Catalysts with various oxides are proposed in WO 2008/145395 A2.
  • Shell catalysts are also known from EP 565952 AI, WO 99/08790 AI and WO 2013/124293 AI.
  • the doping of metal oxide moldings with a combination of at least two dopants is described in WO 2016/075197 Al.
  • WO 2016/075201 A1 describes the improvement of the selectivity of supported Pd / Au catalysts by optimizing the carrier in the form of rings of defined dimensions.
  • Al spherical Pd / Au supported catalysts are used in two fractions with different ball size.
  • Al Pd / Au supported catalysts of bentonite in the form of rings are recommended.
  • the invention relates to a supported catalyst for the production of vinyl acetate comprising a support of phyllosilicate, which is loaded with palladium, gold and at least one alkali compound, characterized in that the carrier is formed as a sphere with a diameter of 4 mm to 10 mm, wherein 1 , 5 to 3.0 wt .-% palladium and 0.75 to 1.7 wt .-% gold, each based on the total weight of the supported catalyst, in a weight ratio of palladium: gold of 1: 1 to 1: 0.5 and palladium, gold and alkali compound are present in a region of the sphere volume which extends at least half the radius away from the surface.
  • the proportion by weight of palladium is preferably 1.8 to 3.0 wt .-% and the weight fraction of gold is preferably 1.3 to 1.7 wt
  • the weight ratio palladium: gold is preferably from 1: 1 to 1: 0.7. Most preferably, it is from 1: 0.8 to 1: 0.7.
  • the spherical supported catalyst is fully impregnated, that is, palladium, gold and alkali compound are distributed over the entire sphere volume.
  • Fully impregnated carrier catalysts are particularly preferably with a palladium concentration over the entire spherical volume distributed from ⁇ 30 x 10 "5 mmol / mm 3.
  • Suitable as an alkali metal compound are the acetates, carbonates, formates and hydroxides of potassium, sodium, cesium or rubidium. Preferred are the corresponding potassium compounds which are converted to potassium acetate under the conditions of gas phase oxidation.
  • the potassium content of the supported catalysts is 0.5 to 15 wt .-%, preferably 1.0 to 12 wt .-%, each based on the total weight of the shaped catalyst body.
  • the catalyst support is loaded with no further active components in addition to palladium, gold and alkali metal.
  • Suitable materials for the production of the catalyst moldings are sheet silicates, preferably bentonites.
  • Bentonites are clayey rocks which contain as their main constituent, generally more than 50% by weight, montmorillonite, an aluminum hydrosilylate belonging to the group of phyllosilicates (foliar structure silicates). Further constituents of the bentonites may be feldspar, mica, calcite and quartz, for example. Preference is given to acid-activated bentonites. Acid activation increases the surface area of the bentonite. Acid-activated bentonites are obtained by heating the natural bentonite, for example in hydrochloric acid or sulfuric acid, followed by filtration, drying and grinding. Bentonite and acid activated bentonite are commercially available in the form of powders or granules, for example from American Colloid Company.
  • the shaped catalyst body is not doped with metal oxides or other dopants.
  • the pulverulent bentonite is ground with the addition of water.
  • the amount of water is chosen so that a mixture is obtained with dough-like consistency.
  • the mass thus obtained is then shaped into spheres of the claimed dimensions.
  • the moldings thus obtained are then dried, preferably at a temperature of 25 ° C to 100 ° C.
  • the drying step is followed by the calcination of the moldings.
  • the calcination can be carried out in an oven under an air atmosphere, if appropriate under protective gas. Generally, it is heated to a temperature of 500 ° C to 1000 ° C.
  • the sintering time is generally between 2 and 10 hours.
  • spheroidal bodies with a diameter of 4 mm to 10 mm, preferably of 5 mm to 10 mm, are produced as shaped catalyst bodies.
  • the conversion of the catalyst molding in an active catalyst is done by applying the catalytically active components palladium and gold or their precursor compounds, as well as the Alkazarberitati, which can optionally be converted in a subsequent step in an active compound.
  • the shaped catalyst bodies can be impregnated with a solution containing palladium salt and gold salt.
  • the application of the solution can be carried out by the methods known in the art, such as wet chemical impregnation, the pore filling method (incipient wetness) or by spray impregnation.
  • Suitable palladium salts are, for example, palladium chloride, sodium or potassium palladium chloride, palladium acetate, palladium nitrate and Pd (NH 3 ) 4 (OH) 2 .
  • Suitable gold salts are gold (III) chloride, tetrachloroauric (III) acid, gold (III) triacetate and CsAu0 2 .
  • the reaction of the noble metal salt solution to insoluble noble metal compounds can be slow and is usually completed after 1 to 24 hours depending on the preparation method. Thereafter, the water-insoluble noble metal compounds are treated with reducing agents. It can be made a gas phase reduction, for example with hydrogen, ethene or forming gas.
  • the chloride which may be present on the support can be removed by a thorough washing with water. After the wash, the catalyst preferably contains less than 500 ppm of chloride.
  • the catalyst precursor obtained after the reduction can be dried and finally impregnated with alkali metal acetates or alkali compounds, which under the reaction conditions in the production of vinyl acetate monomer completely or partially convert to alkali metal acetates.
  • it can be impregnated with potassium acetate.
  • Supported catalysts are obtained in which palladium, gold and alkali compound are present in a region of the sphere volume which extends at least half of the radius away from the surface. Preference is given to supported catalysts in which palladium, gold and alkali compound are distributed throughout the spherical volume (fully impregnated).
  • the finished catalyst can then be dried to a residual moisture of less than 5%.
  • the drying can be carried out in air, optionally under nitrogen, as an inert gas.
  • the heterogeneously catalyzed, continuous gas phase reaction is preferably carried out in a tubular reactor, preferably made of stainless steel, which is charged with a fixed bed catalyst.
  • a fixed bed catalyst In general, this is a fixed bed tube bundle reactor with several thousand, usually 2000 to 20,000, densely packed and generally vertically disposed cylindrical tubes.
  • pipes with a length of 4 m to 10 m and an inner diameter of generally 20 mm to 50 mm.
  • the interstices between the tubes themselves, and the pipes and the container, for cooling flows through a water / steam mixture (boiling water cooling).
  • the tubes of the tubular reactors are filled with the supported catalysts as fixed bed catalysts.
  • the reactor equipped with supported catalyst is charged with ethylene, oxygen and acetic acid for start-up, or charged in continuous operation with the cycle gas laden with ethylene, oxygen and acetic acid.
  • the amounts of educts to be used are known per se to those skilled in the art. Ethylene is generally used in excess of the stoichiometric ratio to acetic acid.
  • the amount of oxygen is limited upwards by the ignition limit in the recycle gas.
  • the gas phase reaction is abs at a pressure of preferably 7 to 15 bar. and at a temperature of preferably 130 ° C to 200 ° C performed.
  • the reaction temperature is set, for example by means of boiling water cooling at a pressure of 1 to 30 bar abs., Preferably 8 to 14 bar abs., Adjusted. In this case, water vapor at a temperature of 120 ° C to 185 ° C at a pressure of 1 to 10 bar abs., Preferably 2.5 to 5 bar abs. Formed.
  • the product gas stream leaving the reactor contains essentially vinyl acetate, ethylene, acetic acid, water and C0 2 .
  • gas phase oxidation is incomplete: ethylene conversion is generally about 5 to 20%, acetic acid conversion generally 20 to 60% and oxygen conversion generally up to 90%.
  • the reaction products vinyl acetate and water and unreacted acetic acid are preferably condensed out in a so-called pre-dewatering column from the circulating gas and fed to the further work-up. Uncondensed product, essentially ethylene, C0 2 and vinyl acetate, can be removed at the top of the pre-dewatering column and washed out in a scrubber operated with acetic acid (circulating gas scrubber).
  • the head product of the pre-dewatering column (circulating gas), or at least a subset thereof, can be separated from the carbon dioxide formed in a C0 2 scrubber. oxide are cleaned.
  • the cycle gas is optionally compressed, re-added with the educts, and passed into the reactor for Gasphasenoxi dation.
  • the condensed products vinyl acetate and water as well as unreacted acetic acid in a multi-stage, usually operated with heating steam distillation process can be separated.
  • the usual distillation steps for obtaining the vinyl acetate and the acetic acid are pre-dewatering column, azeotrope column, dewatering column, pure VAM column, as well as columns for residue workup and for low boiler and high boiler separation.
  • the recycle gas is then charged again with ethylene and acetic acid and then returned to the fixed bed tubular reactor.
  • the enrichment of the cycle gas with acetic acid is usually carried out by means of a heated with steam acetic acid saturator.
  • the Pd concentration in the shell with a volume of 38 mm 3 is consequently 35 ⁇ 10 -5 mmol / mm 3 .
  • the catalysts were tested in a pilot plant corresponding to a process plant.
  • the space-time yields (STY), selectivities and the respective amount of ethyl acetate in the recycle gas obtained with the catalysts from Example 1 and Comparative Example 2 were measured over a period of 2000 hours.
  • the catalysts were placed in a flow-controlled with oil flow reactor (reactor length 6000 mm, inner diameter 33 mm) and at an absolute pressure of 9.5 bar and a space velocity (GHSV) of 3000-4000 Nm 3 / (m 3 * h) with the following Composition of the recycle gas tested: 65% by volume of ethene, 10% by volume of carbon dioxide, 13% by volume of acetic acid and 8% by volume of oxygen, the remainder being methane, ethane, argon, nitrogen.
  • the catalysts were investigated in the temperature range from 130 ° C to 180 ° C, measured in the catalyst bed.
  • V.Bsp. 2 910 92 980

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un catalyseur supporté utilisé pour la production d'acétate de vinyle, comportant un support composé de silicate lamellaire qui est chargé en palladium, en or et en au moins un composé alcalin. L'invention est caractérisée en ce que le support est réalisé sous la forme de sphères présentant un diamètre de 4 mm à 10 mm, Le catalyseur contient 1,5 % en poids à 3,0 % en poids de palladium et 0,75 % en poids à 1,7 % en poids d'or, respectivement rapporté au poids total du catalyseur supporté, dans un rapport en poids palladium/or de 1:1 à 1:0,5, et le palladium, l'or et le composé alcalin sont présents dans une zone du volume des sphères qui s'étend à l'opposé de la surface à raison d'au moins la moitié du rayon.
PCT/EP2018/076853 2017-10-13 2018-10-02 Catalyseur utilisé pour la production d'acétate de vinyle WO2019072655A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DEDE102017218375.6 2017-10-13
DE102017218375.6A DE102017218375A1 (de) 2017-10-13 2017-10-13 Katalysator zur Herstellung von Vinylacetat

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Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3743607A (en) 1965-06-25 1973-07-03 Knapsack Ag Palladium-gold catalyst
DE2716154C2 (fr) 1976-04-12 1988-07-21 E.I. Du Pont De Nemours And Co., Wilmington, Del., Us
EP0565952A1 (fr) 1992-04-08 1993-10-20 Hoechst Aktiengesellschaft Catalyseur sur support, procédé pour sa préparation, ainsi que son utilisation pour préparer l'acétate de vinyle
EP0723810A1 (fr) * 1995-01-23 1996-07-31 Degussa Aktiengesellschaft Catalyseur, procédé pour sa préparation et son utilisation pour la production du monomère d'acétate de vinyle
WO1999008790A1 (fr) 1997-08-13 1999-02-25 Celanese Chemicals Europe Gmbh Catalyseur en coque, son procede de production et son utilisation en particulier pour l'oxydation en phase gazeuse d'ethylene et d'acide acetique en acetate de vinyle
DE10064084A1 (de) * 2000-12-21 2002-07-18 Wacker Chemie Gmbh Verfahren zur Herstellung von Vinylacetat
WO2008071610A2 (fr) 2006-12-13 2008-06-19 Wacker Chemie Ag Procédé de production de catalyseurs et leur utilisation dans l'oxydation en phase gazeuse d'oléfines
WO2008145389A2 (fr) 2007-05-31 2008-12-04 Süd-Chemie AG Catalyseur sous enveloppe servant à la production de vam, procédé de production et d'utilisation dudit catalyseur
WO2008145395A2 (fr) 2007-05-31 2008-12-04 Süd-Chemie AG CATALYSEUR DOPÉ SOUS ENVELOPPE Pd/Au, PROCÉDÉ DE PRODUCTION ET D'UTILISATION DUDIT CATALYSEUR
WO2008145394A2 (fr) 2007-05-31 2008-12-04 Sud-Chemie Ag Support de catalyseur dopé à l'oxyde de zirconium, procédé de production dudit support de catalyseur et catalyseur contenant un support de catalyseur dopé à l'oxyde de zirconium
WO2008145392A2 (fr) 2007-05-31 2008-12-04 Süd-Chemie AG CATALYSEUR SOUS ENVELOPPE Pd/Au À TENEUR EN HfO2, PROCÉDÉ DE PRODUCTION ET D'UTILISATION DUDIT CATALYSEUR
DE102007043447A1 (de) 2007-09-12 2009-03-26 Süd-Chemie AG Katalysatorträger mit erhöhter thermischer Leitfähigkeit
WO2013124293A1 (fr) 2012-02-20 2013-08-29 Clariant Produkte (Deutschland) Gmbh Prédorure de catalyseurs enrobés revêtus de pd-au
WO2016066703A1 (fr) 2014-10-30 2016-05-06 Wacker Chemie Ag Procédé de préparation d'acétate de vinyle
WO2016075197A1 (fr) 2014-11-14 2016-05-19 Wacker Chemie Ag Corps moulé catalytique dopé
WO2016075201A1 (fr) 2014-11-14 2016-05-19 Wacker Chemie Ag Corps moulé catalytique pour la production d'acétate de vinyle
WO2016150894A1 (fr) 2015-03-24 2016-09-29 Wacker Chemie Ag Corps façonnés catalytiques pour la production d'acétate de vinyle
WO2017009243A1 (fr) * 2015-07-13 2017-01-19 Wacker Chemie Ag Procédé d'élimination d'oxygène contenu dans un mélange gazeux contenant un hydrocarbure et de l'oxygène

Patent Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3743607A (en) 1965-06-25 1973-07-03 Knapsack Ag Palladium-gold catalyst
DE2716154C2 (fr) 1976-04-12 1988-07-21 E.I. Du Pont De Nemours And Co., Wilmington, Del., Us
EP0565952A1 (fr) 1992-04-08 1993-10-20 Hoechst Aktiengesellschaft Catalyseur sur support, procédé pour sa préparation, ainsi que son utilisation pour préparer l'acétate de vinyle
EP0723810A1 (fr) * 1995-01-23 1996-07-31 Degussa Aktiengesellschaft Catalyseur, procédé pour sa préparation et son utilisation pour la production du monomère d'acétate de vinyle
WO1999008790A1 (fr) 1997-08-13 1999-02-25 Celanese Chemicals Europe Gmbh Catalyseur en coque, son procede de production et son utilisation en particulier pour l'oxydation en phase gazeuse d'ethylene et d'acide acetique en acetate de vinyle
DE10064084A1 (de) * 2000-12-21 2002-07-18 Wacker Chemie Gmbh Verfahren zur Herstellung von Vinylacetat
WO2008071610A2 (fr) 2006-12-13 2008-06-19 Wacker Chemie Ag Procédé de production de catalyseurs et leur utilisation dans l'oxydation en phase gazeuse d'oléfines
WO2008145389A2 (fr) 2007-05-31 2008-12-04 Süd-Chemie AG Catalyseur sous enveloppe servant à la production de vam, procédé de production et d'utilisation dudit catalyseur
WO2008145395A2 (fr) 2007-05-31 2008-12-04 Süd-Chemie AG CATALYSEUR DOPÉ SOUS ENVELOPPE Pd/Au, PROCÉDÉ DE PRODUCTION ET D'UTILISATION DUDIT CATALYSEUR
WO2008145394A2 (fr) 2007-05-31 2008-12-04 Sud-Chemie Ag Support de catalyseur dopé à l'oxyde de zirconium, procédé de production dudit support de catalyseur et catalyseur contenant un support de catalyseur dopé à l'oxyde de zirconium
WO2008145392A2 (fr) 2007-05-31 2008-12-04 Süd-Chemie AG CATALYSEUR SOUS ENVELOPPE Pd/Au À TENEUR EN HfO2, PROCÉDÉ DE PRODUCTION ET D'UTILISATION DUDIT CATALYSEUR
DE102007043447A1 (de) 2007-09-12 2009-03-26 Süd-Chemie AG Katalysatorträger mit erhöhter thermischer Leitfähigkeit
WO2013124293A1 (fr) 2012-02-20 2013-08-29 Clariant Produkte (Deutschland) Gmbh Prédorure de catalyseurs enrobés revêtus de pd-au
WO2016066703A1 (fr) 2014-10-30 2016-05-06 Wacker Chemie Ag Procédé de préparation d'acétate de vinyle
WO2016075197A1 (fr) 2014-11-14 2016-05-19 Wacker Chemie Ag Corps moulé catalytique dopé
WO2016075201A1 (fr) 2014-11-14 2016-05-19 Wacker Chemie Ag Corps moulé catalytique pour la production d'acétate de vinyle
WO2016150894A1 (fr) 2015-03-24 2016-09-29 Wacker Chemie Ag Corps façonnés catalytiques pour la production d'acétate de vinyle
WO2017009243A1 (fr) * 2015-07-13 2017-01-19 Wacker Chemie Ag Procédé d'élimination d'oxygène contenu dans un mélange gazeux contenant un hydrocarbure et de l'oxygène

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