EP2440490A1 - Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle - Google Patents

Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle

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Publication number
EP2440490A1
EP2440490A1 EP10724763A EP10724763A EP2440490A1 EP 2440490 A1 EP2440490 A1 EP 2440490A1 EP 10724763 A EP10724763 A EP 10724763A EP 10724763 A EP10724763 A EP 10724763A EP 2440490 A1 EP2440490 A1 EP 2440490A1
Authority
EP
European Patent Office
Prior art keywords
catalyst
ruthenium
hydrogen chloride
fluidized bed
metals
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP10724763A
Other languages
German (de)
English (en)
Inventor
Guido Henze
Heiko Urtel
Martin Sesing
Martin Karches
Peter VAN DEN ABEL
Kai Thiele
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
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Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Priority to EP10724763A priority Critical patent/EP2440490A1/fr
Publication of EP2440490A1 publication Critical patent/EP2440490A1/fr
Withdrawn legal-status Critical Current

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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
    • B01J23/90—Regeneration or reactivation
    • B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • 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
    • B01J21/20—Regeneration or reactivation
    • 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
    • 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
    • B01J23/70—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
    • B01J23/892—Nickel and 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • 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
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/42—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using halogen-containing material
    • 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
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/48—Liquid treating or treating in liquid phase, e.g. dissolved or suspended
    • B01J38/50—Liquid treating or treating in liquid phase, e.g. dissolved or suspended using organic liquids
    • B01J38/54—Liquid treating or treating in liquid phase, e.g. dissolved or suspended using organic liquids halogen-containing
    • 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
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/48—Liquid treating or treating in liquid phase, e.g. dissolved or suspended
    • B01J38/68—Liquid treating or treating in liquid phase, e.g. dissolved or suspended including substantial dissolution or chemical precipitation of a catalyst component in the ultimate reconstitution of the catalyst
    • 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
    • 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
    • B01J23/70—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
    • 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
    • B01J37/0201—Impregnation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention relates to a process for the catalytic oxidation of hydrogen chloride over a catalyst containing ruthenium on a particulate carrier with low surface roughness.
  • EP-A 0 743 277 discloses a process for the preparation of chlorine by catalytic hydrogen chloride oxidation, in which a ruthenium-containing supported catalyst is used. Ruthenium is applied to the carrier in the form of ruthenium chloride, ruthenium oxychlorides, chlororuthenate 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.
  • ruthenium (III) chloride on alumina is used as catalyst in a process of catalytic hydrogen chloride oxidation.
  • Suitable promoters for doping are 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, also called titanium, manganese, molybdenum and tin.
  • 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, p
  • a fluidized bed catalyst operated in a reactor made of nickel containing steels produces corrosion of erosion from the reactor during the Deacon reaction. The continued erosion impairs the life of the fluidized bed reactor.
  • the object of the present invention is to remedy the disadvantages described above.
  • the object is achieved by a process for the catalytic oxidation of hydrogen chloride with oxygen to chlorine in a fluidized bed process in the presence of a catalyst containing ruthenium on a particulate support of alpha alumina having an average particle size of 10 to 200 .mu.m, characterized in that the catalyst support has a low surface roughness and is obtainable from a used catalyst which has been used for at least 500 operating hours in a fluidized bed process.
  • a fluidized bed catalyst based on carrier particles of alpha-alumina which were recovered from a used fluidized bed catalyst, causes a significantly lower abrasion on the wall of the fluidized bed reactor, if the used fluidized bed catalyst previously used at least 500 operating hours in a fluidized bed process has been.
  • the used fluidized bed catalyst was used for at least 1000 operating hours in a fluidized bed process.
  • the catalyst support preferably has an average diameter (d 50 value) of preferably 30 to 100, particularly preferably 40 to 80.
  • the fluidized bed reactors used in the process according to the invention are reactors made of a nickel-containing material.
  • the nickel content is at least 10 wt .-%.
  • the ckel inconveniencen materials still contain one or more other metals as alloying constituents, for example selected from iron, molybdenum, chromium and titanium.
  • nickel-containing materials are HC4 (2.4810 NiCM 5 Fe) and Inconel 600 (Ni-Mo16Cr16Ti).
  • the fluidized bed is operated at a gas velocity which is generally 3 to 500 times, preferably 10 to 200 times, more preferably 30 to 100 times the gas velocity at the vortex point (i.e., at the onset of fluidization).
  • the powdery catalyst support used according to the invention is obtained from previously used in the Deacon process, used ruthenium-containing catalysts containing alpha alumina as a carrier, optionally in admixture with other carrier materials.
  • the carrier consists essentially of alpha-alumina, but may contain other carrier materials, for example graphite, silicon dioxide, titanium dioxide and / or zirconium dioxide, preferably titanium dioxide and / or zirconium dioxide.
  • the carrier used according to the invention can be obtained from a used catalyst containing ruthenium oxide by
  • the catalyst containing ruthenium oxide in a gas stream containing hydrogen chloride and optionally an inert gas at a temperature of 300 to 500 0 C is reduced;
  • step b) the reduced catalyst from step a) is treated with hydrochloric acid in the presence of an oxygen-containing gas, the metallic ruthenium present on the support being dissolved as ruthenium chloride and being separated off as aqueous ruthenium chloride solution,
  • the catalyst containing ruthenium oxide in a gas stream containing hydrogen and optionally an inert gas at a temperature of 150 to 600 0 C is reduced;
  • step b) the reduced catalyst from step a) is treated with hydrochloric acid in the presence of an oxygen-containing gas, wherein the carrier present on the support ing metallic ruthenium is dissolved as ruthenium chloride and separated as an aqueous ruthenium chloride solution.
  • the ruthenium chloride solution can, if appropriate after concentration, be used to prepare a new catalyst.
  • the catalysts used according to the invention are obtained by impregnation of the used support material with aqueous solutions of salts of the metals.
  • the metals are usually applied as aqueous solutions of their chlorides, oxychlorides or oxides on the support.
  • the specific surface area of the alpha alumina support before the metal salt deposition is generally in the range of 0.1 to 10 m 2 / g.
  • Alpha-alumina can be prepared by heating gamma-alumina to temperatures in excess of 1000 ° C, preferably it is prepared. Generally calcined for 2 to 24 hours.
  • the catalyst according to the invention may contain, in addition to ruthenium, further metals. These are usually contained in the catalyst in amounts of up to 10% by weight, based on the weight of the catalyst.
  • the catalyst used according to the invention has, in addition to ruthenium, nickel. It has been found that a nickel-doped ruthenium-containing catalyst has a higher activity than a catalyst without nickel. It is believed that this increase in activity is due both to the promoting properties of the nickel chloride and to the better dispersity of the active component on the surface of the catalyst caused by the nickel chloride.
  • ruthenium is present on the catalyst according to the invention in fresh or regenerated form as RuO 2 crystallites with a crystallite size ⁇ 7 nm. The crystallite size is determined by the half-width of the reflection of the species in the XRD measurement.
  • the ruthenium-containing catalysts for the catalytic hydrogen chloride oxidation may additionally contain compounds of one or more further noble metals selected from palladium, platinum, iridium and silver.
  • the catalysts may further contain 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, particularly preferably potassium, alkaline earth metals such as magnesium, Calcium, strontium and barium, 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.
  • alkaline earth metals such as magnesium, Calcium, strontium and barium
  • 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.
  • the weights are based on the weight of the metal, even if the metals are usually present in oxidic or chloridic form on the support.
  • the catalyst used in the invention contains 0.5 to 5 wt .-% ruthenium and 0.5 to 5 wt .-% nickel, based on the weight of the catalyst.
  • the catalyst according to the invention contains about 1 to 3 wt .-% ruthenium and 1 to 3.5 wt .-% nickel on alpha alumina as a carrier and next to no further active metals and promoter metals, wherein ruthenium is present as RuC> 2 ,
  • the ruthenium-supported catalysts can be obtained, for example, by impregnation of the support material with aqueous solutions of RuCl.sub.2 and optionally NiCl.sub.2 and of the further promoters for doping, preferably in the form of their chlorides.
  • the powder can then be carried out at temperatures of 100 to 500 0 C, preferably 100 to 300 0 C, for example under a nitrogen, argon or air atmosphere getrock- net and optionally calcined.
  • the powders are first dried at 100 to 150 0 C and then calcined at 200 to 500 0 C.
  • the support After deactivation of the catalyst, the support can be recovered and reused to prepare a ruthenium supported catalyst.
  • a hydrogen chloride stream and an oxygen-containing stream are fed to the fluidized bed reactor and partially oxidized hydrogen chloride in the presence of the 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 0 C, usual reaction pressures are between 1 and 25 bar, for example 4 bar.
  • the reaction temperature is> 300 0 C, more preferably it is between 350 0 C and 420 0 C.
  • oxygen in superstoichiometric amounts. For example, a 1.5 to 4-fold excess of oxygen is customary. Since no selectivity losses are to be feared, it may be economically advantageous to work at relatively high pressures and, accordingly, at longer residence times than normal pressure.
  • the catalyst fluidized bed may contain, in addition to the catalyst, additional inert material, preferably in the form of additional, inactive carrier material.
  • additional inert material is also used carrier material, which has a low surface roughness due to the use in a fluidized bed process over a period of at least 500 operating hours.
  • Inert material can be used in amounts of 0 to 90 wt .-%, preferably 10 to 50 wt .-%, based on the sum of catalyst and inert material.
  • 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, the drying of the product obtained, consisting essentially of chlorine and oxygen residual gas stream and the separation of chlorine from the dried stream.
  • a ruthenium-containing hydrogen chloride oxidation catalyst used according to the invention can also be obtained by regeneration of a used fluidized bed catalyst which has been used for at least 500 operating hours in a hydrogen chloride oxidation process. This can be regenerated, for example, by:
  • RuC> 2 can be reduced with hydrogen chloride. It is believed that reduction takes place via RuCl 3 to elemental ruthenium. Thus, treating a partially deactivated ruthenium oxide-containing catalyst with hydrogen chloride, presumably, after a sufficiently long treatment time, ruthenium oxide is quantitatively reduced to ruthenium. This reduction destroys the RuO 2 crystallites and redisperses the ruthenium, which may be present as elemental ruthenium, as a mixture of ruthenium chloride and elemental ruthenium, or as ruthenium chloride, on the support. After the reduction, the ruthenium can be reoxidized with an oxygen-containing gas, for example with air, to give the catalytically active RuO 2 . It was found that the catalyst thus obtained again has approximately the activity of the fresh catalyst. An advantage of the method is that the catalyst can be regenerated in situ in the reactor and does not need to be removed.
  • the regenerated catalyst has a low surface roughness corresponding to the operating time.
  • the fresh catalyst has a very rough surface and therefore produces a high reactor removal in the fluidized bed process.
  • 600 g of the catalyst are operated in a fluidized bed reactor with a diameter of 44 mm, a height of 990 mm and a bed height of 300 to 350 mm at 400 0 C with 200 NLh "1 HCl and 100 NL-h " 1 O 2 .
  • the catalyst is in the form of a powder with an average diameter of 50 micrometers (d 50 value). In this case, a hydrogen chloride conversion of 61% is obtained.
  • the catalyst is operated between 360 and 380 0 C.
  • FIG. 1 shows a picture of the fresh catalyst.
  • FIG. 2 shows a picture of the catalyst after 675 operating hours.
  • FIG. 3 shows a picture of the catalyst after 7175 operating hours.
  • FIG. 4 shows a picture of the catalyst after 9485 operating hours.
  • the fresh catalyst shows a rough surface and causes an average erosion rate of the reactor wall of 0.30 mm / year. After 675 hours, a slight rounding off of the catalyst surface can be seen, which is expressed by a slightly reduced erosion rate of 0.28 mm / year. After 7175 hours, the catalyst is rounded off to such an extent that the erosion rate drops to 0.04 mm / year. Finally, after 9485 hours, the erosion rate is virtually zero due to the smooth catalyst surface.
  • a recycling of the carrier allows the preparation of a fresh catalyst, which causes almost no erosion of the reactor wall from the beginning and thus increases the lifetime of the reactor by a multiple.
  • the supernatant Ru- and Ni-containing solution is separated by filtration from the solid (carrier) and the filter cake is washed with 500 mL of water.
  • the combined aqueous phases contain> 98% of the ruthenium and the nickel. Evaporation of a portion of this solution to 18 mL gives a solution containing 4.2% by weight of ruthenium and 7.0% by weight of nickel.
  • a deactivated fluidized bed catalyst which was obtained after 9485 operating hours in the fluidized bed reactor described in Example 1, are subjected to the recycling process for recovering the carrier described in Example 2.
  • the dried material is calcined at 380 ° C. under air for 1 h.
  • the resulting RuO 2 -containing catalyst can be used again for the catalytic HCl oxidation with O 2 .
  • 21 kg of the used catalyst from Example 2 (RuO 2 to Ci-Al 2 O 3 containing 2.5 wt .-% nickel chloride) are in a fluidized bed reactor with a diameter of 108 mm, a height of 4 to 4.5 m and a Bed height of 2.5 to 3 m at 400 0 C with 10.5 kg-h "1 HCl, 4.6 kg-h " 1 O 2 and 0.9 N 2 kg-h "1.
  • the catalyst is located in Forming a powder with a mean diameter of 50 microns (d 50 value) .This results in a conversion of HCl of 77% .Then after 20 h at 400 0 C, the oxygen is switched off and instead to 10.0 kg-h "1 HCl converted.
  • the catalyst is recalcined at 400 ° C. for 30 minutes at 2.0 kg-h -1 O 2 and 8.0 kg-h -1 N 2 and so reactivated.
  • the catalyst at 400 0 C with 10.5 kg-h "1 HCl, 4.6 kg-h " 1 O 2 and 0.9 N 2 kg-h "1 shows a conversion of 84% with respect to HCl.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Catalysts (AREA)

Abstract

La présente invention concerne un procédé permettant d'obtenir du chlore, dans le cadre d'un procédé à lit fluidisé, par oxydation catalytique de gaz chlorhydrique, avec utilisation d'acide en présence d'un catalyseur contenant du ruthénium sur un support particulaire en alumine alpha dont le calibre particulaire moyen va de 10 µm à 200 µm. Ce procédé se caractérise en ce que le support de catalyseur présente une faible rugosité superficielle, et qu'il est réalisable à partir d'un catalyseur usagé qui a été mis en œuvre au moins pendant 500 heures de fonctionnement dans un procédé à lit fluidisé.
EP10724763A 2009-06-10 2010-06-04 Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle Withdrawn EP2440490A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP10724763A EP2440490A1 (fr) 2009-06-10 2010-06-04 Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP09162365 2009-06-10
PCT/EP2010/057814 WO2010142604A1 (fr) 2009-06-10 2010-06-04 Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle
EP10724763A EP2440490A1 (fr) 2009-06-10 2010-06-04 Procédé d'oxydation de gaz chlorhydrique sur un catalyseur à faible rugosité superficielle

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EP2440490A1 true EP2440490A1 (fr) 2012-04-18

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US (2) US20120087855A1 (fr)
EP (1) EP2440490A1 (fr)
JP (1) JP2012529415A (fr)
KR (1) KR20120036956A (fr)
CN (1) CN102803130B (fr)
BR (1) BRPI1011010A2 (fr)
WO (1) WO2010142604A1 (fr)

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CN110961095B (zh) * 2018-09-30 2022-06-28 中国石油化工股份有限公司 费托合成催化剂及其制备方法和应用
KR102287846B1 (ko) * 2018-12-21 2021-08-06 한화솔루션 주식회사 염소 제조를 위한 염화수소 산화반응용 촉매 및 이의 제조방법
KR102262496B1 (ko) * 2018-12-21 2021-06-07 한화솔루션 주식회사 염소 제조용 산화루테늄 담지 촉매의 제조방법 및 이에 의해 제조된 촉매
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US20150360210A1 (en) 2015-12-17
JP2012529415A (ja) 2012-11-22
CN102803130A (zh) 2012-11-28
BRPI1011010A2 (pt) 2019-09-24
WO2010142604A1 (fr) 2010-12-16
CN102803130B (zh) 2015-07-15

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