WO2007125004A1 - Procédé de fabrication de catalyseurs pour l'oxydation catalytique de chlorure d'hydrogène - Google Patents

Procédé de fabrication de catalyseurs pour l'oxydation catalytique de chlorure d'hydrogène Download PDF

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Publication number
WO2007125004A1
WO2007125004A1 PCT/EP2007/053297 EP2007053297W WO2007125004A1 WO 2007125004 A1 WO2007125004 A1 WO 2007125004A1 EP 2007053297 W EP2007053297 W EP 2007053297W WO 2007125004 A1 WO2007125004 A1 WO 2007125004A1
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Prior art keywords
catalyst
metals
hydrogen chloride
support
impregnated
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PCT/EP2007/053297
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German (de)
English (en)
Inventor
Olga Schubert
Martin Sesing
Martin Karches
Heiko Urtel
Christian Walsdorff
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Basf Aktiengesellschaft
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Publication of WO2007125004A1 publication Critical patent/WO2007125004A1/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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/12—Oxidising
    • B01J37/14—Oxidising with gases containing free oxygen
    • 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
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/462—Ruthenium
    • 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
    • B01J23/72—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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00—Halogens; Halogen acids
    • C01B7/01—Chlorine; Hydrogen chloride
    • C01B7/03—Preparation from chlorides
    • C01B7/04—Preparation of chlorine from hydrogen chloride
    • 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
    • B01J23/56—Platinum group metals
    • B01J23/58—Platinum group metals with alkali- or alkaline earth 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
    • 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
    • B01J23/56—Platinum group metals
    • B01J23/63—Platinum group metals with rare earths or actinides
    • 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
    • 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
    • B01J23/78—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 alkali- or alkaline earth 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
    • 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
    • B01J23/83—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 rare earths or actinides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/06—Halogens; Compounds thereof
    • B01J27/08—Halides
    • B01J27/10—Chlorides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/06—Halogens; Compounds thereof
    • B01J27/08—Halides
    • B01J27/122—Halides of 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
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/06—Halogens; Compounds thereof
    • B01J27/128—Halogens; Compounds thereof with iron group metals or platinum group metals
    • B01J27/13—Platinum group metals

Definitions

  • the invention relates to a process for the preparation of catalysts for the catalytic hydrogen chloride oxidation and to a process for the catalytic hydrogen chloride hydrogenation.
  • EP-A 0 743 277 discloses a process for the production of chlorine by catalytic hydrogen chloride oxidation, in which a ruthenium-containing supported catalyst is used. Ruthenium is applied to the support in the form of ruthenium chloride, ruthenium oxychlorides, chloro-ruthenate complexes, ruthenium hydroxide, ruthenium-amine complexes or in the form of further ruthenium complexes.
  • the catalyst may contain as further metals palladium, copper, chromium, vanadium, manganese, alkali, alkaline earth and rare earth metals.
  • a catalyst obtained by applying ruthenium (III) chloride to alumina and then calcining at 250 ° C. in air is used.
  • gamma-alumina is used as the alumina carrier.
  • the oxidic support is impregnated with one or more metal salt solutions containing the active metal or metals and optionally promoter metals, the impregnated support is dried and then calcined.
  • the calcination is usually carried out in an oven, for example a rotary kiln, tray oven or fluidized bed calciner, under oxygen or air.
  • chloride-containing catalysts chlorine or hydrogen chloride is released. Because of the corrosive atmosphere, calcination must be carried out in corrosion resistant equipment.
  • the object of the present invention is to provide a simpler and more economical process for the preparation of catalysts for the catalytic hydrogen chloride oxidation. It is also an object of the present invention to provide a simpler and more economical process for catalytic hydrogen chloride oxidation.
  • the object is achieved by a process for the preparation of catalysts for the catalytic hydrogen chloride oxidation containing
  • the impregnated support in each case based on the total weight of the catalyst, on a support in which the support is impregnated with one or more metal salt solutions which comprise the active metal (s) and optionally promoter metals a) to e), the impregnated support is dried and calcined, characterized that calcining the impregnated support at 200 to 600 ° C in an oxygen-containing atmosphere in a fixed bed or fluidized bed reactor.
  • the object is further achieved by a process for the catalytic oxidation of hydrogen chloride with oxygen to chlorine in a fixed bed or fluidized bed reactor containing containing catalyst particles from a catalyst
  • the impregnated support in each case based on the total weight of the catalyst, on a carrier in which the carrier is mixed with one or more metal salt solutions which tivmetalle and optionally the promoter metals a) to e), impregnated, the impregnated support dries and calcined the impregnated support at 200 to 600 ° C in an oxygen-containing atmosphere, characterized in that the impregnated support at 200 to 600 ° C in a calcined oxygen-containing atmosphere in the fixed bed or fluidized bed reactor and performs the catalytic hydrogen chloride oxidation on the calcined in the fixed or fluidized bed reactor catalyst.
  • the catalysts used according to the invention are obtained by impregnation of the support material with aqueous solutions of salts of the metals.
  • the metals other than gold are usually applied to the support as aqueous solutions of their chlorides, oxychlorides or oxides.
  • the shaping of the catalyst can take place after or preferably before the impregnation of the support material.
  • the catalysts used according to the invention are also used as fluidized-bed catalysts in the form of powder having an average particle size of 10-200 ⁇ m. As fixed bed catalysts, they are generally used in the form of shaped catalyst bodies.
  • the copper or ruthenium-supported catalysts can be obtained, for example, by impregnating the support material with aqueous solutions of CuCl 2 or RuCl 3 and optionally a promoter for doping, preferably in the form of their chlorides.
  • Gold-containing catalysts of the present invention can be obtained by applying gold in the form of the aqueous solution of a soluble gold compound, then drying or drying and calcining.
  • gold is applied to the support as an aqueous solution of AuCl 3 or HAuCl 4 .
  • the ruthenium, copper and / or gold catalysts of the invention for the catalytic hydrogen chloride oxidation may additionally contain compounds of one or more other noble metals selected from palladium, platinum, osmium, iridium, silver or rhenium.
  • the catalysts may also be doped with one or more further metals.
  • Alkali metals such as lithium, sodium, potassium, rubidium and cesium, preferably lithium, sodium and potassium, more preferably potassium, alkaline earth metals such as magnesium, calcium, strontium and barium, preferably magnesium and calcium, more preferably magnesium, rare earth metals such as scandium, yttrium, lanthanum, Cerium, praseodymium and neodymium, preferably scandium, yttrium, lanthanum and cerium, more preferably lanthanum and cerium or mixtures thereof, furthermore titanium, manganese, molybdenum and tin.
  • alkaline earth metals such as magnesium, calcium, strontium and barium, preferably magnesium and calcium, more preferably magnesium, rare earth metals such as scandium, yttrium, lanthanum, Cerium, praseodymium and neodymium, preferably scandium, yttrium, lanthanum and cerium, more preferably lanthanum and cerium or mixtures thereof
  • the catalyst is impregnated by impregnation of an oxidic support, for example an aluminum oxide powder or shaped body, with an aqueous ruthenium chloride hydrate solution corresponding to the water absorption of the support, then dried at 100 to 200 ° C., incorporated into the fixed bed reactor or fluidized bed reactor and finally calcined at 200 to 600 ° C, preferably at 300 to 400 ° C, in an oxygen-containing atmosphere, preferably in an air atmosphere, for a period of 1 to 12 hours, preferably 2 to 4 hours in the reactor. Locally, temperature peaks (hot spots) with temperatures above 600 ° C can occur. To avoid the formation of hot spots, the oxygen supply can be controlled. After calcination, ruthenium is generally present essentially as ruthenium (IV) oxide.
  • the calcination of the catalyst and the catalytic hydrogen chloride oxidation can be carried out in a fluidized bed reactor.
  • the fluidized bed contains the catalyst as a fluidized granulate.
  • the individual granules may each consist of catalyst material or contain the catalyst material on its surface.
  • the catalyst comprises the metal components on an oxidic support.
  • Alumina for example ⁇ -aluminum oxide or ⁇ -aluminum oxide, zirconium oxide or titanium oxide or mixtures of these oxides can be used as oxidic support.
  • the oxidic supports are preferably used in powder form with an average particle diameter of 30 to 150 ⁇ m, more preferably 40 to 100 ⁇ m and in particular 50 to 80 ⁇ m.
  • the fine fraction having a particle size ⁇ 20 ⁇ m is preferably less than 40% by weight, more preferably less than 30% by weight and in particular less than 20% by weight.
  • the catalysts based on ruthenium known from GB 1, 046,313, DE-A 197 48 299 or DE-A 197 34 412 can be used.
  • % of one or more alkali metals 0 to 10% by weight of one or more rare earth metals and 0 to 10% by weight of one or more other metals selected from the group consisting of ruthenium, Palladium, osmium, iridium, silver, copper and rhenium, each based on the total weight of the catalyst.
  • the catalyst is impregnated by impregnation of a ⁇ -alumina powder with an aqueous ruthenium chloride hydrate solution corresponding to the water absorption of the carrier, then dried at 100 to 200 ° C and finally at 200 to 600 ° C, for example about 400 ° C. , calcined under air atmosphere in the fluidized bed reactor.
  • the ruthenium content of the catalyst is preferably 1 to 5 wt .-%, in particular 1, 5 to 3 wt .-%.
  • the calcination of the catalyst and the catalytic hydrogen chloride oxidation can be carried out in a fixed bed reactor.
  • a fixed bed reactor a tube bundle reactor is preferably used.
  • the fixed bed contains the catalyst as a bed of shaped catalyst bodies or catalyst split.
  • Suitable shaped catalyst bodies are any desired forms, preference being given to tablets, rings, cylinders, stars, wagon wheels or spheres, particular preference being given to rings, cylinders or star strands.
  • Suitable oxidic supports are alumina, for example gamma-alumina or ⁇ -alumina, zirconia or titania or mixtures of these oxides.
  • alpha-alumina is alpha-alumina, optionally in admixture with other carrier materials such as graphite, silicon dioxide, titanium dioxide and / or zirconium dioxide.
  • Alpha alumina can be prepared by heating gamma alumina to temperatures in excess of 1000 ° C.
  • the present invention also provides a process for the catalytic oxidation of hydrogen chloride with oxygen to chlorine on the catalyst which has been calcined according to the invention.
  • a hydrogen chloride stream and an oxygen-containing stream are fed into the fixed bed or fluidized bed reactor and hydrogen chloride is partially oxidized to chlorine in the presence of the previously calcined catalyst to give a product gas stream containing chlorine, unreacted oxygen, unreacted hydrogen chloride and water vapor.
  • the hydrogen chloride stream which may originate from an isocyanate-producing plant, may contain impurities such as phosgene and carbon monoxide.
  • Typical reaction temperatures are between 150 and 500 ° C, usual reaction pressures are between 1 and 25 bar, for example 4 bar.
  • the reaction temperature is> 300 ° C, more preferably between 350 ° C and 400 ° C.
  • oxygen in superstoichiometric amounts. For example, a 1, 5 to 4-fold excess of oxygen is customary. There no Selectivity losses are to be feared, it may be economically advantageous to work at relatively high pressures and, accordingly, with respect to normal pressure longer residence times.
  • the catalytic hydrogen chloride oxidation is carried out in the same fixed bed or fluidized bed reactor in which the catalyst has previously been calcined.
  • the hydrogen chloride oxidation can be carried out in one or more stages.
  • the catalyst bed of the fixed bed reactor or the catalyst fluidized bed may contain, in addition to the catalyst according to the invention, further suitable catalysts or additional inert material.
  • An embodiment of the fixed-bed method consists in using a structured catalyst bed in which the catalyst activity increases in the direction of flow.
  • Such structuring of the catalyst bed can be carried out by different impregnation of the catalyst support with active material or by different dilution of the catalyst bed with an inert material.
  • an inert material for example, rings, cylinders or balls of titanium dioxide, zirconium dioxide or mixtures thereof, alumina, steatite, ceramic, glass, graphite or stainless steel can be used.
  • the inert material preferably has similar external dimensions as the shaped catalyst bodies.
  • the conversion of hydrogen chloride in a single pass can be limited to 15 to 90%, preferably 40 to 85%. Unreacted hydrogen chloride can be partially or completely recycled to the catalytic hydrogen chloride oxidation after separation.
  • the volume ratio of hydrogen chloride to oxygen at the reactor inlet is generally between 1: 1 and 20: 1, preferably between 1, 5: 1 and 8: 1, more preferably between 1, 5: 1 and 5: 1.
  • the chlorine formed can subsequently be separated off in a customary manner.
  • the separation usually comprises several stages, namely the separation and if appropriate, recycling of unreacted hydrogen chloride from the product gas stream of the catalytic hydrogen chloride oxidation, drying of the resulting, consisting essentially of chlorine and oxygen residual gas stream and the separation of chlorine from the dried stream.

Abstract

L'invention concerne un procédé de fabrication de catalyseurs contenant a) 0,001 à 10 % en poids d'au moins un métal appartenant au groupe se composant de ruthénium, de cuivre et d'or, b) 0 à 5 % en poids d'un ou plusieurs métaux alcalino-terreux, c) 0 à 5 % en poids d'un ou de plusieurs métaux alcalins, d) 0 à 10 % en poids d'un ou plusieurs métaux terreux rares, e) 0 à 10 % en poids d'un ou plusieurs autres métaux, choisis dans le groupe se composant de palladium, de platine, d'osmium, d'iridium, d'argent et de rhénium, respectivement par rapport au poids total du catalyseur, sur un support, dans lequel on imprègne le support d'une ou de plusieurs solutions de sels métalliques, lesquelles contiennent le ou les métaux actifs et le cas échéant les métaux promoteurs a) à e), on sèche le support imprégné et on le calcine, caractérisé en ce que l'on calcine le support imprégné à des températures de 200 à 600°C dans une atmosphère contenant de l'oxygène dans un réacteur à lit fixe ou à lit fluidisé.
PCT/EP2007/053297 2006-04-26 2007-04-04 Procédé de fabrication de catalyseurs pour l'oxydation catalytique de chlorure d'hydrogène WO2007125004A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP06113120 2006-04-26
EP06113120.7 2006-04-26

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Publication Number Publication Date
WO2007125004A1 true WO2007125004A1 (fr) 2007-11-08

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010142604A1 (fr) * 2009-06-10 2010-12-16 Basf Se Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle
WO2012065427A1 (fr) * 2010-11-18 2012-05-24 烟台万华聚氨酯股份有限公司 Catalyseur pour la préparation de chlore par oxydation de chlorure d'hydrogène et sa préparation
CN115350707A (zh) * 2022-08-08 2022-11-18 中国科学院青岛生物能源与过程研究所 铜镧合金催化剂在氯化氢氧化制备氯气中的应用

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3461084A (en) * 1965-11-10 1969-08-12 Monsanto Co Cupric chloride-alumina catalyst
US3760067A (en) * 1968-06-18 1973-09-18 Velsicol Chemical Corp Process for the production of elemental halogen
DE19734412A1 (de) * 1996-08-08 1998-02-12 Sumitomo Chemical Co Verfahren zur Herstellung von Chlor
DE19748299A1 (de) * 1996-10-31 1998-05-07 Sumitomo Chemical Co Verfahren zur Herstellung von Chlor

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3461084A (en) * 1965-11-10 1969-08-12 Monsanto Co Cupric chloride-alumina catalyst
US3760067A (en) * 1968-06-18 1973-09-18 Velsicol Chemical Corp Process for the production of elemental halogen
DE19734412A1 (de) * 1996-08-08 1998-02-12 Sumitomo Chemical Co Verfahren zur Herstellung von Chlor
DE19748299A1 (de) * 1996-10-31 1998-05-07 Sumitomo Chemical Co Verfahren zur Herstellung von Chlor

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010142604A1 (fr) * 2009-06-10 2010-12-16 Basf Se Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle
CN102803130A (zh) * 2009-06-10 2012-11-28 巴斯夫欧洲公司 在具有低表面粗糙度的催化剂上氧化氯化氢的方法
CN102803130B (zh) * 2009-06-10 2015-07-15 巴斯夫欧洲公司 在具有低表面粗糙度的催化剂上氧化氯化氢的方法
WO2012065427A1 (fr) * 2010-11-18 2012-05-24 烟台万华聚氨酯股份有限公司 Catalyseur pour la préparation de chlore par oxydation de chlorure d'hydrogène et sa préparation
US20170274361A1 (en) * 2010-11-18 2017-09-28 Wanhua Chemical Group Co., Ltd. Catalyst for preparing chlorine by oxidation of hydrogen chloride and preparation thereof
US10576465B2 (en) 2010-11-18 2020-03-03 Wanhua Chemical Group Co., Ltd. Catalyst for preparing chlorine by oxidation of hydrogen chloride and preparation thereof
CN115350707A (zh) * 2022-08-08 2022-11-18 中国科学院青岛生物能源与过程研究所 铜镧合金催化剂在氯化氢氧化制备氯气中的应用
CN115350707B (zh) * 2022-08-08 2024-03-26 中国科学院青岛生物能源与过程研究所 铜镧合金催化剂在氯化氢氧化制备氯气中的应用

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