Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/23—Preparation of halogenated hydrocarbons by dehalogenation
• • 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
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/02—Apparatus characterised by being constructed of material selected for its chemically-resistant properties
• • 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
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/24—Chromium, molybdenum or tungsten
  • B01J23/26—Chromium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
  • B23K—SOLDERING OR UNSOLDERING; WELDING; CLADDING OR PLATING BY SOLDERING OR WELDING; CUTTING BY APPLYING HEAT LOCALLY, e.g. FLAME CUTTING; WORKING BY LASER BEAM
  • B23K20/00—Non-electric welding by applying impact or other pressure, with or without the application of heat, e.g. cladding or plating
  • B23K20/04—Non-electric welding by applying impact or other pressure, with or without the application of heat, e.g. cladding or plating by means of a rolling mill
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
  • B23K—SOLDERING OR UNSOLDERING; WELDING; CLADDING OR PLATING BY SOLDERING OR WELDING; CUTTING BY APPLYING HEAT LOCALLY, e.g. FLAME CUTTING; WORKING BY LASER BEAM
  • B23K20/00—Non-electric welding by applying impact or other pressure, with or without the application of heat, e.g. cladding or plating
  • B23K20/06—Non-electric welding by applying impact or other pressure, with or without the application of heat, e.g. cladding or plating by means of high energy impulses, e.g. magnetic energy
  • B23K20/08—Explosive welding
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
  • B23K—SOLDERING OR UNSOLDERING; WELDING; CLADDING OR PLATING BY SOLDERING OR WELDING; CUTTING BY APPLYING HEAT LOCALLY, e.g. FLAME CUTTING; WORKING BY LASER BEAM
  • B23K20/00—Non-electric welding by applying impact or other pressure, with or without the application of heat, e.g. cladding or plating
  • B23K20/22—Non-electric welding by applying impact or other pressure, with or without the application of heat, e.g. cladding or plating taking account of the properties of the materials to be welded
  • B23K20/227—Non-electric welding by applying impact or other pressure, with or without the application of heat, e.g. cladding or plating taking account of the properties of the materials to be welded with ferrous layer
• • 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
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/02—Apparatus characterised by their chemically-resistant properties
  • B01J2219/0204—Apparatus characterised by their chemically-resistant properties comprising coatings on the surfaces in direct contact with the reactive components
  • B01J2219/0236—Metal based
• • 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
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/02—Apparatus characterised by their chemically-resistant properties
  • B01J2219/025—Apparatus characterised by their chemically-resistant properties characterised by the construction materials of the reactor vessel proper
  • B01J2219/0277—Metal based
  • B01J2219/0286—Steel
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
  • B23K—SOLDERING OR UNSOLDERING; WELDING; CLADDING OR PLATING BY SOLDERING OR WELDING; CUTTING BY APPLYING HEAT LOCALLY, e.g. FLAME CUTTING; WORKING BY LASER BEAM
  • B23K2103/00—Materials to be soldered, welded or cut
  • B23K2103/02—Iron or ferrous alloys
  • B23K2103/04—Steel or steel alloys
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
  • B23K—SOLDERING OR UNSOLDERING; WELDING; CLADDING OR PLATING BY SOLDERING OR WELDING; CUTTING BY APPLYING HEAT LOCALLY, e.g. FLAME CUTTING; WORKING BY LASER BEAM
  • B23K2103/00—Materials to be soldered, welded or cut
  • B23K2103/18—Dissimilar materials
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B23—MACHINE TOOLS; METAL-WORKING NOT OTHERWISE PROVIDED FOR
  • B23K—SOLDERING OR UNSOLDERING; WELDING; CLADDING OR PLATING BY SOLDERING OR WELDING; CUTTING BY APPLYING HEAT LOCALLY, e.g. FLAME CUTTING; WORKING BY LASER BEAM
  • B23K2103/00—Materials to be soldered, welded or cut
  • B23K2103/18—Dissimilar materials
  • B23K2103/26—Alloys of Nickel and Cobalt and Chromium
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C19/00—Acyclic saturated compounds containing halogen atoms
  • C07C19/08—Acyclic saturated compounds containing halogen atoms containing fluorine
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C21/00—Acyclic unsaturated compounds containing halogen atoms
  • C07C21/02—Acyclic unsaturated compounds containing halogen atoms containing carbon-to-carbon double bonds
  • C07C21/18—Acyclic unsaturated compounds containing halogen atoms containing carbon-to-carbon double bonds containing fluorine

Definitions

• the present invention relates to methods for modifying the gas phase fluorine distribution.
• the present invention relates to methods for modifying the gas phase fluorine distribution in the presence of a chromium catalyst.
• Halogenated hydrocarbons particularly fluorinated hydrocarbons such as hydrofluoroolefins, are compounds which have a useful structure as functional materials, solvents, refrigerants, blowing agents and monomers for functional polymers or starting materials for such monomers.
• Hydrofluoroolefins such as 2,3,3,3-tetrafluoropropene (HFO-1234yf) are attracting attention because they offer promising behavior as low global warming potential refrigerants.
• the processes for producing fluoroolefins are usually carried out in the presence of a starting material such as an alkane containing chlorine or a chlorine-containing alkene, and in the presence of a fluorinating agent such as hydrogen fluoride. These processes can be carried out in the gas phase or in the liquid phase, in the absence or absence of catalyst.
• Gas phase processes are usually carried out in the presence of catalysts and hydrofluoric acid.
• the environment inside the reactor has a very high acidity generating a high corrosion of the reactor material.
• Reactors used in processes involving hydrofluoric acid generally include a base material and a corrosion resistant material. The materials used must also have good resistance to high temperature to meet the requirements of industrial safety.
• the present invention relates to a method for modifying the fluorine distribution in a hydrocarbon compound, comprising a step of contacting a hydrocarbon compound with a catalytic composition comprising a chromium-based catalyst, said process being carried out in a reactor made of a material comprising a base layer made of a material M1 and an inner layer made of a material M2, said base layer and said inner layer being arranged against each other, characterized in that the M2 material comprises at least 80% by weight of nickel based on the total weight of the material M2, preferably at least 90% by weight, preferably at least 95% by weight, in particular at least 99% by weight of nickel based on the total weight of material M2.
• the material M1 comprises iron and less than 0.2% carbon based on the total weight of the material M1.
• the material M2 comprises less than 1% iron based on the total weight of the material M2.
• the material M2 comprises less than 1% of manganese based on the total weight of the material M2.
• the material M2 comprises less than 1% by weight of titanium and / or less than 1% by weight of niobium based on the total weight of the material M2.
• the hydrocarbon compound is selected from the group consisting of tetrachloropropene, chlorotrifluoropropene, pentachloropropane, dichlorotrifluoropropane, trichlorodifluoropropane, tetrafluorochloropropane, tetrachlorofluoropropane, dichlorodifluoropropene, trichlorofluoropropene, pentafluoropropane and mixtures thereof; preferably, the hydrocarbon compound is selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 2,3-dichloro-1,1,1-trifluoropropane (HCFC- 243db), 1,1,1,2,3-pentachloropropane (HCC-240db), 1,1,2,2,3-pentachloropropane (HCC-240aa), 1,1,1,1,1,
• the fluorine content of the hydrocarbon compound is increased by reacting said hydrocarbon compound with hydrogen fluoride in phase. in the presence of said catalytic composition, the hydrocarbon compound being a halogenated saturated hydrocarbon or a halogenated unsaturated hydrocarbon or an unsaturated hydrocarbon.
• the fluorine content of the hydrocarbon compound is decreased by dehydrofluorination of said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.
• the fluorine distribution of the hydrocarbon compound is modified by isomerizing said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.
• the fluorine distribution of the hydrocarbon compound is modified by dismutting said hydrocarbon compound in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a chlorofluorinated hydrocarbon compound.
• the fluorine content of the hydrocarbon compound is decreased by reacting said hydrocarbon compound with hydrogen chloride in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a halogenated hydrocarbon compound containing at least one fluorine atom.
• the fluorine content of a first hydrocarbon compound is increased by reacting said first hydrocarbon compound with hydrogen fluoride gas phase in the presence of a catalyst composition comprising a chromium-based catalyst, the first hydrocarbon compound being a halogenated saturated hydrocarbon or a halogenated unsaturated hydrocarbon or an unsaturated hydrocarbon, and the fluorine content of a second hydrocarbon compound is decreased by dehydrofluorinating said second hydrocarbon compound in the presence of said catalyst composition comprising a catalyst based on chromium, said second hydrocarbon compound being a fluorinated hydrocarbon compound.
• the catalyst composition comprises a chromium catalyst.
• the chromium-based catalyst may be a chromium oxide (for example CrO 3 or Cr 2 O 3), a chromium oxyfluoride or a chromium fluoride (for example CrFs) or a mixture thereof.
• the chromium oxyfluoride may contain a fluorine content of between 1 and 60% by weight based on the total weight of the chromium oxyfluoride, advantageously between 5 and 55% by weight, preferably between 10 and 52% by weight, more preferably between 15 and 52% by weight, in particular between 20 and 50% by weight, more particularly between 25 and 45% by weight, preferably between 30 and 45% by weight, more preferably from 35 to 45% by weight. by weight of fluorine based on the total weight of the chromium oxyfluoride.
• the catalyst may also comprise a co-catalyst selected from the group consisting of Ni, Co, Zn, Mg, Mn, Fe, Zn, Ti, V, Zr, Mo, Ge, Sn, Pb, Sb; preferably Ni, Co, Zn, Mg, Mn; in particular Ni, Co, Zn.
• the content by weight of the cocatalyst is between 1 and 10% by weight based on the total weight of the catalytic composition.
• the catalytic composition may also comprise a support such as alumina, for example in its alpha form, activated alumina, aluminum halides (AI F3 for example), aluminum oxyhalides, activated carbon, fluoride magnesium or graphite.
• the catalytic composition has a specific surface area between 1 and 100 m 2 / g, preferably between 5 and 80 m 2 / g, more preferably between 5 and 70 m 2 / g, ideally between 5 and 50 m 2 / g. in particular between 10 and 50 m 2 / g, more particularly between 15 and 45 m 2 / g.
• the catalysts provided according to the present invention can be used to modify the fluorine distribution in hydrocarbon compounds, the latter being halogenated or non-halogenated hydrocarbon compounds.
• the fluorine distribution in a hydrocarbon compound can be varied by increasing the fluorine content of the hydrocarbon compound.
• the fluorine distribution of a hydrocarbon compound can also be modified by lowering the fluorine content of the hydrocarbon compound and / or rearranging the position of fluorine atoms on the carbon atoms of the hydrocarbon compound.
• the present invention can provide processes wherein the fluorine distribution in hydrocarbon compounds containing from one to twelve carbon atoms is modified, preferably processes in which the fluorine distribution is modified in hydrocarbon compounds containing from one to six carbon atoms. in particular processes where the fluorine distribution is modified in hydrocarbon compounds containing three carbon atoms, more particularly where the fluorine distribution is modified in halogenated hydrocarbon compounds containing three carbon atoms.
• the present invention can provide processes in which the fluorine content of hydrocarbon compounds containing from one to twelve carbon atoms is increased, preferably processes in which the fluorine content of hydrocarbon compounds containing from one to six carbon atoms is increased.
• Processes for modifying the fluorine distribution of hydrocarbon compounds, preferably of halogenated hydrocarbon compounds include fluorination, chlorofluorination, isomerization, disproportionation, dehydrofluorination and chlorodefluorination.
• the hydrocarbon compounds include those of the formula C h H a Br b Cl c F d, wherein h is an integer between 1 and 6, a is an integer between 0 and 13, b is an integer from 0 to 4, c is an integer between 0 and 13, d is an integer between 0 and 13, and the sum of a, b, c and d is 2h + 2; or those of general formula C p H e Br f Cl g F h , where p is an integer between 2 and 6, e is an integer between 0 and 10, f is an integer between 0 and 2, g is an integer between 0 and 12, h is an integer between 0 and 11, and the sum of e, f, g and h is 2p.
• the hydrocarbon compounds include those of the formula C h H a Cl c F d, wherein h is an integer between 2 and 4, a is an integer between 0 and 9, c is an integer from 0 to 9, d is an integer between 0 and 9, and the sum of a, c and d is equal to 2h + 2; or those of the general formula C p H e Cl g F h , where p is an integer between 2 and 4, e is an integer between 0 and 8, g is an integer between 0 and 8, h is an integer between 0 and 7 , and the sum of e, f, g and h is equal to 2p.
• the hydrocarbon compounds may be selected from the group consisting of tetrachloropropene, chlorotrifluoropropene, pentachloropropane, dichlorotrifluoropropane, trichlorodifluoropropane, tetrachlorofluoropropane, dichlorodifluoropropene, trichlorofluoropropene, pentafluoropropane, chlorotetrafluoropropane and their mixtures.
• the hydrocarbon compounds may be selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 2,3-dichloro-1,1,1-trifluoropropane (HCFCs -243db), 1,1,1,2,3-pentachloropropane (HCC-240db), 1,1,2,2,3-pentachloropropane (HCC-240aa), 1,1,1,3,3-pentachloropropane ( HCC-240fa), 1,1,2,3-tetrachloro-1-propene (HCO-1230xa), 2,3,3,3-tetrachloro-1-propene (HCO-1230xf), 1,1,3,3 tetrachloro-1-propene (HCO-1230za), 1,3,3,3-tetrachloro-1-propene (HCO-1230zd), 1,1,1,2,2-pentafluoropropane (HFC-245cb)
• Said method according to the present invention is implemented in a reactor made of a material comprising a base layer made of a material Ml and an inner layer made of a material M2, said base layer and said inner layer being arranged one against the other.
• the reactor may be a fixed catalytic bed reactor or a fluidized catalytic bed reactor or a multitubular reactor.
• said reactor is a fixed catalytic bed reactor.
• the corrosion rate of the material M2 is less than 1 mm / year, advantageously less than 0.5 mm / year, preferably less than 0.1 mm / year, more preferably less than 0.05. mm / year, in particular less than 0.025 mm / year, more particularly less than 10 ⁇ / year, preferably less than 5 ⁇ / year. This rate is measured according to the method of coupons ASTM D 2 328-65 T.
• the inner layer is the layer in contact with the hydrocarbon compound.
• the inner layer is also in contact with the other starting materials used, for example hydrofluoric acid, and the products generated during the reaction carried out in the reactor.
• said base layer and said inner layer are arranged against one another by plating.
• the plating is performed by welded veneer, explosion-etched veneer, hot-rolling veneer, or cold-rolling veneer.
• the plating is carried out by explosion or by hot rolling.
• the veneer is made by explosion.
• the material M2 is in contact with the hydrocarbon compound.
• the material M2 may have a tensile strength lower than that of the material M1.
• the material M2 may also have an elongation greater than that of the material Ml.
• said inner layer has a thickness of between 0.01 and 20 mm, said thickness of said inner layer being less than that of said base layer.
• said inner layer may have a thickness of between 0.05 and 15 mm, preferably between 0.1 and 10 mm, more preferably between 0.1 and 5 mm.
• the material M2 comprises at least 80% by weight of nickel based on the total weight of the material M2.
• the material M2 comprises at least 85% by weight of nickel, more preferably at least 90% by weight of nickel, in particular at least 95% by weight of nickel, more particularly at least 99% by weight of nickel based on the total weight of the material M2.
• the material M2 can comprise at least 80%, at least 81%, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%.
• the material M2 may also comprise iron in a content of less than 1% by weight based on the total weight of the material M2, advantageously less than 0.9% by weight, preferably less than 0.8% by weight, more preferably less to 0.7% by weight, in particular less than 0.6% by weight, more particularly less than 0.5% by weight based on the total weight of the material M2.
• the material M2 comprises between 0.1 and 1% by weight of iron, in particular between 0.3 and 0.8% by weight of iron, more particularly between 0.3 and 0.5% by weight of iron. based on the total weight of the material M2.
• the material M2 may also comprise manganese in a content of less than 7% by weight based on the total weight of the material M2, advantageously less than 6% by weight, preferably less than 5% by weight, more preferably less than 4% by weight. weight, in particular less than 3% by weight, more particularly less than 2% by weight, preferably less than 1% by weight, preferably less than 0.75%, particularly preferably less than 0.5% by weight % based on the total weight of the material M2.
• the material M2 comprises between 0.1 and 1% by weight of manganese, in particular between 0.3 and 0.8% by weight of manganese, more particularly between 0.3 and 0.5% by weight of manganese. based on the total weight of the material M2.
• the material M2 comprises between 3 and 7% by weight of manganese, in particular between 3.5 and 6.5% by weight of manganese, more particularly between 4 and 6% by weight of manganese on the basis of the total weight of the material. M2.
• the material M2 may also comprise silicon in a content less than
• the material M2 comprises between 0.1 and 1% by weight of silicon, in particular between 0.3 and 0.8% by weight of silicon, more particularly between 0.3 and 0.5% by weight of silicon. based on the total weight of the material M2.
• the material M2 comprises between 0.05 and 0.5% by weight of silicon, in particular between 0.1 and 0.3% by weight of silicon, more particularly between 0.1 and 0.25% by weight of silicon based on the total weight of the M2 material.
• the material M2 may also comprise copper in a content of less than 1% by weight based on the total weight of the material M2, advantageously less than 0.9% by weight, preferably less than 0.8% by weight, more preferably less to 0.7% by weight, in particular less than 0.6% by weight, more particularly less than 0.5% by weight, of preferred way less than 0.4% by weight, particularly preferably less than 0.3% by weight based on the total weight of the material M2.
• the material M2 comprises between 0.1 and 1% by weight of copper, in particular between 0.2 and 0.5% by weight of copper, more particularly between 0.2 and 0.3% by weight of copper. based on the total weight of the material M2.
• the material M2 may also comprise carbon in a content of less than 0.1% by weight based on the total weight of the material M2, advantageously less than 0.09% by weight, preferably less than 0.08% by weight, more preferably less than 0.07% by weight, in particular less than 0.06% by weight, more particularly less than 0.05% by weight, preferably less than 0.04% by weight, particularly preferably less than 0.03% by weight based on the total weight of the material M2.
• the material M2 comprises between 0.005 and 0.1% by weight of carbon, in particular between 0.01 and 0.075% by weight of carbon, more particularly between 0.01 and 0.05% by weight of carbon based on the total weight of the material M2.
• the material M2 may comprise less than 0.1% by weight of sulfur based on the total weight of the material M2, advantageously less than 0.09% by weight, preferably less than 0.08% by weight, more preferably less than 0% by weight. , 07% by weight, in particular less than 0.06% by weight, more particularly less than 0.05% by weight, preferably less than 0.04% by weight, particularly preferably less than 0.03% by weight by weight, more particularly preferably less than 0.02% by weight of sulfur based on the total weight of the material M2.
• the material M2 may comprise less than 1% by weight of titanium based on the total weight of the material M2, advantageously less than 0.5% by weight of titanium, preferably less than 0.1% by weight of titanium, more preferably less of 0.05% by weight of titanium, in particular less than 0.01% by weight of titanium based on the total weight of the material M2, in a preferred manner the material M2 is devoid of titanium.
• the material M2 may comprise less than 1% by weight by weight of niobium, advantageously less than 0.5% by weight of niobium, preferably less than 0.1% by weight of niobium, more preferably less than 0.05% by weight. weight of niobium, in particular less than 0.01% by weight of niobium on the basis of the total weight of the material M2, in a preferred manner the material M2 is devoid of niobium.
• the material M1 comprises at least 70% by weight of iron, advantageously at least 75% by weight, preferably at least 80% by weight, more preferably at least 85% by weight, in particular at least 90% by weight, more particularly at least 95% by weight of iron based on the total weight of the material M1.
• the material M1 may also comprise less than 2% by weight of carbon, advantageously less than 1.5% by weight, preferably less than 1% by weight, more preferably less than 0.75% by weight, in particular less than 0% by weight. , 5% by weight, more preferably less than 0.2% by weight, preferably less than 0.1% by weight based on the total weight of the material M1. More particularly, the material M1 can comprise between 0.01 and 0.2% by weight of carbon based on the total weight of the material M1.
• the material M1 may also comprise less than 2% by weight of molybdenum, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferably less than 1% by weight of molybdenum based on the weight total material Ml. More particularly, the material M1 may comprise between 0.1 and 1% by weight of molybdenum based on the total weight of the material M1.
• the material M1 may also comprise less than 5% by weight of chromium, advantageously less than 4% by weight, preferably less than 3% by weight, more preferably less than 2% by weight, in particular less than 1% by weight of chromium based on the total weight of the material Ml. More particularly, the material M1 can comprise between 0.5 and 2% by weight of chromium based on the total weight of the material M1.
• the material M1 may also comprise less than 2% by weight of silicon, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferably less than 1% by weight of silicon based on the weight total material Ml. More particularly, the material M1 can comprise between 0.1 and 1.5% by weight of silicon based on the total weight of the material M1.
• the material M1 may also comprise less than 2% by weight of manganese, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferably less than 1% by weight of manganese on the basis of the weight total material Ml. More particularly, the material M1 can comprise between 0.1 and 1% by weight of manganese based on the total weight of the material M1.
• the reactor used in the processes according to the invention comprises a base layer made of a material M1 and an inner layer, in contact with at least the hydrocarbon compound, made of a material M2 arranged against each other ; said M2 material comprising: at least 80% by weight of nickel, preferably at least 85% by weight of nickel, more preferably at least 90% by weight of nickel, in particular at least 95% by weight of nickel, more particularly at least 99% by weight nickel based on the total weight of the material M2; and less than 1% by weight of iron based on the total weight of the material M2, advantageously less than 0.9% by weight, preferably less than 0.8% by weight, more preferably less than 0.7% by weight, in particular less than 0.6% by weight, more particularly less than 0.5% by weight of iron based on the total weight of the material M2; and / or less than 7% by weight of manganese, advantageously less than 6% by weight, preferably less than 5% by weight, more preferably less than 4% by weight, in particular less than 3% by weight, more particularly
• niobium less than 1% by weight by weight of niobium, advantageously less than 0.5% by weight of niobium, preferably less than 0.1% by weight of niobium, more preferably less than 0.05% by weight of niobium, in especially less than 0.01% by weight of niobium on the basis of the total weight of the material M2, in a preferred manner the material M2 is devoid of niobium;
• the material M1 comprising at least 70% by weight of iron, advantageously at least 75% by weight, preferably at least 80% by weight, more preferably at least 85% by weight, in particular at least 90% by weight, more particularly at least 95% by weight of iron based on the total weight of the material M1; and less than 2% by weight of carbon, advantageously less than 1.5% by weight, preferably less than 1% by weight, more preferably less than 0.75% by weight, in particular less than 0.5% by weight , more preferably less than 0.2% by weight, preferably less than 0.1% by weight based on the total weight of the material M1, more particularly between 0.01 and 0.2% by weight of carbon based of the total weight of the material M1 and less than 2% by weight of molybdenum, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferably less than 1% by weight of molybdenum on the basis of total weight of the material M1, more particularly between 0.1 and 1% by weight of molybdenum based on the total weight
• the feed or outlet lines of the reactor are made of specific material capable of also resisting corrosion, for example made of material M2.
• the supply lines may be tubular.
• the feed or outlet lines may be made of a material comprising a base layer made of a material M1 covered with an inner layer, in contact with the hydrocarbon or other starting material, for example HF, made of M2 material.
• the reactor also comprises one or more dephlegmator (s), one or more plunger tube (s), one or more raw material introduction device (s), one or more support and retaining grid (s). catalyst.
• Said one or more dephlegmator (s) and / or said one or more plunger tube (s) and / or said one or more raw material introduction device (s) and / or said one or more grid (s) ) of support and retention of the catalyst may be made of a material comprising a base layer made of a material M1 covered with an inner layer, in contact with the hydrocarbon or other starting material, for example HF, made of M2 material. Materials Ml and M2 are as described above.
• the fluorine content of the hydrocarbon compound is increased by reacting said compound with hydrogen fluoride in the presence of said catalyst composition, the hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon.
• a hydrocarbon compound is halogenated when it comprises at least one halogen.
• a hydrocarbon is unsaturated when it contains at least one carbon-carbon double bond.
• Suitable hydrocarbon compounds as starting reagents for the fluorination process of this first embodiment may be saturated or unsaturated halogenated hydrocarbon compounds.
• Compounds saturated halogenated hydrocarbons include those having the general formula C h H a Br b Cl c F d, wherein h is an integer between 1 and 6, a is an integer between 0 and 13, b is an integer from 0 to 4, c is an integer between 0 and 13, d is an integer between 0 and 13, provided that b + c is at least 1 and the sum of a, b, c and d is 2h + 2.
• the saturated halogenated hydrocarbon compounds include those of the formula C h H a Cl c F d, wherein h is an integer from 2 to 4, a is an integer between 0 and 9, c is an integer between 1 and 9, d is an integer between 0 and 9, and the sum of a, c and d is equal to 2h + 2.
• Halogenated unsaturated hydrocarbon compounds include those of the general formula C p H e Br f Cl g Fh, where p is an integer between 2 and 6, e is an integer between 0 and 11, f is an integer between 0 and 2, g is an integer between 0 and 12, h is an integer between 0 and 11, provided that f + g is at least 1, and the sum of e, f, g and h is 2p.
• the halogenated unsaturated hydrocarbon compounds include those of the general formula CpHeCIgFh, where p is an integer between 2 and 4, e is an integer between 0 and 7, g is an integer between 1 and 8, h is an integer between 0 and 7, and the sum of e, g and h is equal to 2p.
• an HF / hydrocarbon compound molar ratio between 1: 1 and 150: 1, preferably between 2: 1 and 125: 1, more preferably between 3: 1 and 100: 1;
• a contact time between 1 and 100 s, preferably between 2 and 75 s, in particular between 3 and 50 s;
• a pressure between atmospheric pressure and 20 bara, preferably between 2 and 18 bara, more preferably between 3 and 15 bara;
• a temperature preferably of the catalytic bed, between 200 and 450 ° C, preferably between 250 and 400 ° C, more preferably between 280 ° C and 380 ° C.
• the process can be carried out over a period of between 10 and 8000 h, preferably between 50 and 5000 h, more preferably between 70 and 1000 h.
• An oxidant such as oxygen or chlorine, can be added during the process.
• the molar ratio of the oxidant to the hydrocarbon compound may be between 0.005 and 2, preferably between 0.01 and 1.5.
• the oxidant may be pure oxygen, air or a mixture of oxygen and nitrogen.
• the amount of HF reacted with the hydrocarbon compounds must be at least stoichiometric.
• the stoichiometric amount is based on the number of Br and / or Cl substituents to be replaced by F in addition to one mole of HF to saturate the carbon-carbon double bond (s), if any.
• halogenated saturated compounds of the formula C n H a Br b Cl c F d which may be reacted with HF in the presence of catalysts of this invention include CH2Cl2, CH2Br2, CHCl, CCU, C 2 Cl 6, C 2 BrCI 5, C2CI5F, C2CI4F2, C2CI3F3, C2CI2F4, C2CI F5, C2HCI5, C2HCI4F, C2HCI3F2, C2HCI2F3, C2HCI F4, C2H B F4, C2H2CI4, C2H2CI3F, C2H2CI2F2, C2H2CI F3, C2H3CI3 , C2H3CI2F, C2H3CI2F, C2H3CI F2, C2H4CI2, C2H4CI F, C3CI6F2, C3CI5F3, C3CI4F4, C3CI3F5, C3HCI7, C3HCI6F, C3HCI5F2, C
• fluorination reactions of halogenated saturated hydrocarbon compounds that can be carried out under the conditions described above using the catalysts of this invention include the conversion of 1,1,2-trichloroethane (CHCl 2 CH 2 Cl or HCC-140).
• 1-chloro-2,2-difluoroethane CH 2 CICF 2 H or HCFC-142
• the conversion of 1,1,1,3,3,3-hexachloropropane (CCI3CH2CCI3 or HCC-230
• halogenated or nonhalogenated of formula C p unsaturated compounds H e BrfCl g Fh and Hi that can be reacted with HF in the presence of catalysts of this invention include C2CI4, C 2 BrCI 3 C2CI3F, C2CI2F2, C2CI F3, C2F4 , C2HCI3, C 2 H BrCl2, C 2 HCl 2 F, C 2 HCl F 2 , C 2 HF 3 , C 2 H 2 Cl 2 , C 2 H 2 ClF, C 2 H 2 F 2 , C 2 H 3 Cl, C 2 H 3 F, C 2 H 4 , C 3 H 6 , C 3 H 5 Cl, C 3 H 4 Cl 2 , C3H3CI3, C3H2CI4, C3HCI5, C3H2CI F3, C3F3HCI2, C3F2H2CI2, C3F4H, CIC3CI6, C3CI5F, C3CI4F2, C3CI3F3, C3CI2F4,
• the hydrocarbon compound is selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 1,1,1,2,3-pentachloropropane (HCC-240db), 1,1,2,2,3-pentachloropropane (HCC-240aa), 1,1,2,3-tetrachloro-1-propene (HCO-1230xa), 2,3,3,3-tetrachloro-1-propene ( HCO-1230xf), or mixtures thereof, for the production of 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• HFCO-1233xf 2-chloro-3,3,3-trifluoro-1-propene
• HCC-240db 1,1,1,2,3-pentachloropropane
• HCC-240aa 1,1,2,2,3-pentachloropropane
• HCO-1230xa 1,1,2,3-tetrachloro-1-prop
• the hydrocarbon compound is selected from the group consisting of 1-chloro-3,3,3-trifluoro-1-propene (HCFO-1233zd), 1,1,1,3,3-pentachloropropane (HCC-240fa), 1,1,3,3-tetrachloro-1-propene (HCO-1230za), 1,3,3,3-tetrachloro-1-propene (HCO-1230zd), or mixtures thereof for the production of 1,3,3 3-tetrafluoropropene (HFO-1234ze).
• the fluorine content of the hydrocarbon compound is reduced by dehydrofluorinating said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.
• Fluorinated hydrocarbon compounds suitable as raw materials for the dehydrofluorination process of this invention are typically saturated.
• Compounds halogenated saturated hydrocarbons include those having the general formula C n H a Cl c F d, wherein n is an integer between 2 and 6, a is an integer between 1 and 13, c is an integer between 0 and 12, d is an integer between 1 and 13, and the sum of a, c and d is 2n + 2.
• the halogenated saturated hydrocarbon compounds include those of the general formula C n H a Cl c Fd, where n is an integer between 2 and 4, a is an integer between 1 and 9, c is an integer between 0 and 6, d is an integer between 1 and 9, and the sum of a, c and d is 2n + 2.
• the fluorine content of saturated compounds of formula C n H a Fd can be reduced in the presence of said catalytic composition.
• the process according to the second embodiment can be carried out in a reactor comprising a catalytic bed containing a catalyst and according to the following operating conditions: an HF / hydrocarbon compound molar ratio between 1: 1 and 150: 1, preferably between 2: 1 and 125 : 1, more preferably between 3: 1 and 100: 1;
• a contact time between 1 and 100 seconds, preferably between 2 and 75 seconds, in particular between 3 and 50 seconds;
• a pressure between atmospheric pressure and 20 bara, preferably between 2 and 18 bara, more preferably between 3 and 15 bara;
• a temperature preferably of the catalytic bed, between 200 and 450 ° C, preferably between 250 and 400 ° C, more preferably between 280 ° C and 380 ° C.
• the process can be carried out over a period of between 10 and 8000 h, preferably between 50 and 5000 h, more preferably between 70 and 1000 h.
• An oxidant such as oxygen or chlorine, can be added during the process.
• the molar ratio of the oxidant to the hydrocarbon compound may be between 0.005 and 2, preferably between 0.01 and 1.5.
• the oxidant may be pure oxygen, air or a mixture of oxygen and nitrogen.
• the product of the dehydrofluorination reaction is HF and the fluorinated unsaturated hydrocarbon compound resulting from the loss of HF by the initial reagent.
• halogenated hydrocarbon compound is 1,1,1,2,2-pentafluoropropane
• the halogenated hydrocarbon compound is 1,1,1,3,3-pentafluoropropane (HFC-245fa) for the production of 1,3,3,3-tetrafluoropropene (HFO-1234ze).
• reaction of said hydrocarbon compound with hydrogen fluoride can be carried out in the presence of oxygen or chlorine.
• the fluorine distribution in the hydrocarbon compound is modified by isomerizing said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.
• the fluorine distribution in the hydrocarbon compound is modified by dismutting said hydrocarbon compound in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a chlorofluorinated hydrocarbon compound.
• the isomerization and dismutation processes of the third and fourth embodiments are carried out in the vapor phase in the presence of said catalytic composition.
• Suitable fluorinated hydrocarbon compounds as starting materials for the isomerization and disproportionation processes may be saturated or unsaturated.
• Suitable saturated fluorinated hydrocarbon compounds for the isomerization and disproportionation processes include those of the general formula C n H a Br b Cl c F d , where n is an integer between 2 and 6, a is an integer between 0 and 13, b is an integer between 0 and 4, c is an integer between 0 and 13, d is an integer between 1 and 13, and the sum of a, b, c and d is 2n + 2, provided that a + b
• the unsaturated fluorinated hydrocarbon compounds suitable for the isomerization and disproportionation processes include those of general formula C p H e Br f Cl g F h , where p is an integer between 2 and 6, e is an integer between 0 and 11, f is an integer between 0 and 2, g is an integer between 0 and 12, h is an integer between 1 and 11, and the
• the fluorine distribution of a fluorinated hydrocarbon compound is modified by rearranging the H, Br, Cl and F substituents in the molecule (typically a thermodynamically preferred arrangement) while maintaining the same number of substituents H, Br, Cl and F, respectively . In the present, this process is called isomerization.
• the fluorine distribution of a fluorinated hydrocarbon compound is modified by exchanging at least one substituent F of the halogenated hydrocarbon feedstock with at least one substituent H, Br and / or Cl of another molecule of the halogenated hydrocarbon feedstock, to provide formation of one or more halogenated hydrocarbon compounds having a reduced fluorine content relative to the halogenated hydrocarbon feedstock and one or more halogenated hydrocarbon compounds having an increased fluorine content relative to the halogenated hydrocarbon feedstock. In the present, this process is called disproportionation.
• the isomerization and disproportionation processes are typically carried out at temperatures between about 100 ° C and 500 ° C, preferably between about 150 ° C and about 400 ° C.
• the contact time in the reactor is typically from about 1 to about 120 seconds, preferably from about 5 to about 60 seconds.
• the isomerization and disproportionation reactions can be carried out in the presence of an inert gas, such as helium, argon or nitrogen, although this is not preferred.
• the isomerization and disproportionation reactions can be carried out in the presence of HF and HCl.
• the isomerization processes can be carried out using the present catalyst and include the conversion of 1-chloro-1,1-difluoroethane (CH3CF2Cl or HCFC-142b) to 1-chloro-2,2-difluoroethane (CH 2 CICF 2 H or HCFC-142), the conversion of 1,3-dichloro-1,2,2,3,3-pentafluoropropane (CHCl 3 FCF 2 CF 2 Cl or HCFC-225cb) to 1,1,2,9-dichloro-2,2,3,3 3-Pentafluoropropane (CHCl2CF2CF3 or HCFC-225ca), the conversion of 2,2-dichloro-1,1,1,3,3-pentafluoropropane (CH F2CCI2CF3 or HCFC-225aa) to 1,1,2-dichloro-2,2 , 3,3,3-pentafluoropropane (CHCl2CF2CF3 or HC
• the (Z) isomers of hydrochlorofluoroolefins are the (Z) isomers of hydrochlorofluoropropenes and hydrochlorofluorobutenes.
• the disproportionation methods can be carried out using the present catalyst and include the conversion of chlorofluoromethane (CH 2 Cl or HCFC-31) to difluoromethane (CH 2 F 2 or HFC-32) and dichloromethane (CH 2 Cl 2 or HCC-30), the conversion of 1-chloro-1,1-difluoroethane (CH3CCI F2 or HCFC-142b) to 1,1,1-trifluoroethane (CH3CF3 or HFC-143a) and 1,1-dichloro-1-fluoroethane (CH3CCI2F or HCFC-141b), conversion of 1-chloro-1,2,2,2-tetrafluoroethane (CF3CHCIF or HCFC-124) to pentafluoroethane (CF3CH F2 or HFC-125) and 2,2-dichloro-1,1,1-trifluoroethane (CF3CHCl2) or HCFC-123), the conversion of 1,1,3-
• the fluorine content of the hydrocarbon compound is reduced by reacting said hydrocarbon compound with hydrogen chloride in the gas phase in the presence of said catalyst composition, said hydrocarbon compound being a halogenated hydrocarbon compound.
• Suitable fluorinated hydrocarbon compounds as raw materials for the process of this embodiment may be saturated or unsaturated.
• the halogenated saturated hydrocarbon compounds suitable for the chlorodefluorination processes according to this invention include those of the general formula C n H a Cl c F d , where n is an integer between 1 and 6, a is an integer between 0 and 13, c is a integer between 0 to 13, d is an integer between 1 to 13, and the sum of a, c and d is 2n + 2.
• Halogenated unsaturated hydrocarbon compounds suitable for the chlorodefluorination processes according to this invention include those of the general formula C p H e Cl g F h , where p is an integer between 2 and 6, e is an integer between 0 and 11, g is a integer between 0 and 12, h is an integer between 1 and 11, and the sum of e, g and h is 2p.
• the chlorodefluorination reactions are typically conducted at temperatures of about 250 ° C to 450 ° C, preferably about 300 ° C to about 400 ° C.
• the contact time in the reactor is typically from about 1 to about 120 seconds. Of course, contact times of about 5 to about 60 seconds are possible.
• the reactions are ideally conducted at atmospheric pressure or more.
• Chlorodefluorations involving saturated halogenated hydrocarbons are particularly noteworthy.
• the molar ratio of HCl to the saturated halogenated hydrocarbon compound is typically from about 1: 1 to about 100: 1, preferably from about 3: 1 to about 50: 1, and most preferably from about 4: 1 to about 30: 1.
• the higher the temperature, the longer the contact time the greater the molar ratio of HCl to the saturated halogenated hydrocarbon compound, and the greater the conversion of the low-fluorine compounds. .
• the above variables can be balanced against each other to maximize the formation of chlorinated products.
• the product of the chlorodefluorination reactions typically comprises HCl and unreacted HF, unconverted raw material, and halogenated saturated hydrocarbon compounds having a lower fluorine content than the raw material as a result of the substitution of one or more several fluorine substituents with chlorine.
• reaction products obtained by the detailed methods can be separated in any of the first five embodiments by conventional techniques, such as with combinations including, but not limited to, washing, decantation or distillation.
• Some of the products of the various embodiments of this invention can form one or more azeotropes with each other or with HF.
• the methods disclosed in the present invention may further include a step of regenerating said catalyst composition in the presence of a regeneration stream comprising an air / oxidant flow.
• the oxidant may be oxygen, air, a mixture of oxygen and nitrogen, chlorine or a mixture of chlorine and nitrogen.
• the proportion of oxygen may range from 5 to 100 mol% relative to the mixture of oxygen and nitrogen.
• the regeneration step may be carried out in the presence of a regeneration stream containing (a) oxygen or air or an oxygen / nitrogen mixture or chlorine and (b) HF.
• the regeneration flow will contain at least 1 mol% oxygen relative to the total regeneration flow.
• the proportion of oxygen can range from 2 to 98 mol% relative to the total amount expressed in moles of oxygen and HF, and from 20 to 100 mol% relative to the total amount expressed in moles of oxygen and of oxygen. nitrogen.
• the regeneration step is carried out at a temperature of 250 to 500 ° C, preferably 300 to 450 ° C, more preferably 350 to 400 ° C.
• the regeneration step can be carried out with a contact time of 1 to 200 s, preferably from 1 to 150 s, more preferably from 5 to 100 s, and for a duration of 1 to 1500 h, preferably from 2 to 1000 h, more preferably 4 to 500 h, ideally 10 to 200 h and in particular 15 to 150 h.
• the regeneration step can be carried out under a pressure ranging from atmospheric pressure to 20 bara.
• the regeneration step can be carried out at a temperature of 250 to 500 ° C, with a contact time of 1 to 200 s, for 10 to 200 h and under a pressure between atmospheric pressure and 20 bara. .
• the methods disclosed in the present invention may further include the step of activating said catalyst composition in the presence of an air / oxidant stream.
• the catalyst is subjected to an activation step with air, oxygen or chlorine and / or HF.
• the catalyst is preferably subjected to activation with air or oxygen, and HF at a temperature between 100 and 500 ° C, preferably between 250 and 500 ° C and in particular between 300 and 400 ° C.
• the activation time is preferably from 1 to 200 hours and in particular from 1 to 50 hours. This activation can be followed by a final step of fluorination activation in the presence of an oxidant, HF and hydrocarbon compounds.
• the HF / hydrocarbon compound molar ratio ranges from 2 to 40, and the oxidative / hydrocarbon compound molar ratio ranges from 0.04 to 25.
• the temperature of the final fluorination activation stage may range from 300 to 400 ° C. preferably for a period of 6 to 100 hours.
• the present invention may also provide a method of modifying the distribution of chlorine in a hydrocarbon compound in the presence of said catalyst composition.
• the chlorine content of the hydrocarbon compound is reduced by dehydrochlorinating said hydrocarbon compound in the presence of said catalyst composition, said hydrocarbon compound being a chlorinated hydrocarbon compound.
• Suitable chlorinated hydrocarbon compounds as raw materials for the dehydrochlorination process are typically saturated.
• the saturated chlorinated hydrocarbon compounds include those of the general formula C n H a Cl d , where n is an integer between 2 and 6, a is an integer between 1 to 12, d is an integer between 1 to 13, and the sum of a and d is 2n + 2.
• contact time from 1 to 100 seconds, preferably from 2 to 75 seconds, in particular from 3 to 50 seconds;
• pressure between atmospheric pressure and 20 bara, preferably from 2 to 18 bara, more preferably from 3 to 15 bara;
• temperature preferably of the catalytic bed, of 200 to 450 ° C, preferably of 250 to 400 ° C, more preferably of 280 ° C to 380 ° C.
• the process may be carried out for a period of 10 to 8000 h, preferably 50 to 5000 h, more preferably 70 to 1000 h.
• the product of the dehydrochlorination reaction is HCl and the unsaturated fluorinated hydrocarbon compound resulting from the loss of HCl of the initial reagent.
• the method of modifying the distribution of chlorine in a hydrocarbon compound can be carried out simultaneously with a method of modifying the fluorine distribution in another hydrocarbon compound, for example by increasing or decreasing the fluorine content in said other hydrocarbon compound as detailed above with reference to the first and second embodiments.
• the fluorine content of a first hydrocarbon compound is increased by reacting said first hydrocarbon compound with hydrogen fluoride in the gas phase in the presence of said catalytic composition, the first hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or unsaturated hydrocarbon and decreasing the fluorine content of a second hydrocarbon compound by dehydrofluorinating said second hydrocarbon compound in the presence of said catalyst composition, said second hydrocarbon compound being a fluorinated hydrocarbon compound.
• the first hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon is defined above with reference to the first embodiment.
• the second hydrocarbon compound is defined above with reference to the second embodiment.
• the fluorination of the first hydrocarbon compound and the dehydrofluorination of the second hydrocarbon compound are preferably carried out simultaneously.
• a temperature (of the catalyst bed) between 200 and 450 ° C, preferably between 250 and 400 ° C, more preferably between 280 ° C and 380 ° C.
• the process can be carried out over a period of between 10 and 8000 h, preferably between 50 and 5000 h, more preferably between 70 and 1000 h.
• An oxidant such as oxygen or chlorine, can be added during the process.
• the molar ratio of the oxidant to the hydrocarbon compound may be between 0.005 and 2, preferably between 0.01 and 1.5.
• the oxidant may be pure oxygen, air or a mixture of oxygen and nitrogen.
• a temperature preferably of the catalytic bed, between 200 and 450 ° C, preferably between 250 and 400 ° C, more preferably between 280 ° C and 380 ° C.
• the process can be carried out over a period of between 10 and 8000 h, preferably between 50 and 5000 h, more preferably between 70 and 1000 h.
• the corrosion coupons were installed for 400 days in a fluorination reactor alternating fluorination reactions in the presence of hydrofluoric acid, a catalyst of chromium oxyfluoride and 1,1,1,2,3-pentachloropropane ( Temperature of 350 ° C, 4 bara) and catalyst regeneration reactions.
• the coupon A consists of a material comprising more than 99% by weight of nickel.
• the coupon B consists of a material comprising 32% by weight of nickel.
• the coupon C consists of a material comprising 11% by weight of nickel.
• the corrosion rate of coupons A-C is determined after 400 days by microscopic observation. The data are shown in Table 1 below.
• the metal coupon A corresponding to a material M2 according to the present application and comprising more than 99% by weight of nickel has a very high stability over time, even under severe operating conditions.

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