Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
  • C07C17/20—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms
  • C07C17/202—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction
  • C07C17/206—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction the other compound being HX
• • 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
  • B01J38/00—Regeneration or reactivation of catalysts, in general
  • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
  • B01J38/12—Treating with free oxygen-containing gas
• • 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
  • B01J8/04—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 the fluid passing successively through two or more beds
  • B01J8/0446—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
  • B01J8/0449—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
  • B01J8/0457—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being placed in separate reactors
• • 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
  • B01J8/04—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 the fluid passing successively through two or more beds
  • B01J8/0492—Feeding reactive fluids
• • 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
• • 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
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00327—Controlling the temperature by direct heat exchange
  • B01J2208/00336—Controlling the temperature by direct heat exchange adding a temperature modifying medium to the reactants
  • B01J2208/00353—Non-cryogenic fluids
  • B01J2208/00371—Non-cryogenic fluids gaseous
• • 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
  • 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
  • B01J2219/0295—Synthetic organic materials

Definitions

• the present invention relates to a process for the manufacture of tetrafluoropropene (HFO-1234), and in particular 2,3,3,3-tetrafluoropropene (HFO-1234yf), as well as an installation adapted to the implementation of this process.
• HFO-1234 tetrafluoropropene
• HFO-1234yf 2,3,3,3-tetrafluoropropene
• Greenhouse gases are gaseous components that absorb the infrared radiation emitted by the earth's surface, thus contributing to the greenhouse effect. Increasing their concentration in the atmosphere is one of the factors causing global warming.
• chlorofluorocarbons CFCs
• hydrochlorofluorocarbons HCFCs
• hydrofluoroolefins or hydrofluorocarbons by fluorination of hydrochloro-olefins or hydrochlorocarbons in particular.
• This fluorination is generally a catalytic fluorination using hydrofluoric acid as fluorinating agent.
• the fluorination reaction must generally be carried out at an elevated temperature (above 300 ° C.) in the gaseous phase in the presence of a solid or supported solid catalyst.
• US 8,614,361 discloses a method of making HFO-1234yf by reacting HCFO-1233xf with THF in the presence of a high oxygen content.
• US Pat. No. 8,618,338 describes a two-step process for producing fluoroolefin, in particular a first liquid-phase reaction step from 1,1,2,3-tetrachloropropene (HCO-1230xa) to obtain the intermediate. HCFO-1233xf and a second gas phase reaction from HCFO-1233xf to obtain HFO-1234yf.
• WO 2013/088195 teaches a two-step process for manufacturing HFO-1234yf, a first gas phase fluorination step of 1,1,1,2,3-pentachloropropane (HCC-240db) and / or 1, 1,2,2,3-pentachloropropane (HCC-240aa) to obtain the intermediate HCFO-1233xf, followed by a second gas phase reaction from HCFO-1233xf to obtain HFO-1234yf.
• HCC-240db 1,1,1,2,3-pentachloropropane
• HCC-240aa 1, 1,2,2,3-pentachloropropane
• WO 2012/098421 and WO 2012/098422 teach the activation and regeneration of fluorination catalysts.
• WO 2013/182816 describes a chemical reaction process for the alternating implementation of a catalytic reaction phase and a catalyst regeneration phase in a reactor.
• the document WO2016 / 001515 describes a chemical reaction process for the alternating implementation of a catalytic reaction phase and a catalyst regeneration phase in one or more reactors.
• HFO-1234 such as HFO-1234yf
• the present invention relates, in a first aspect, to a process for the manufacture of tetrafluoropropene using three reactors and comprising the steps of:
• step of regeneration of the preliminary catalyst in the third reactor is carried out in the absence of a reaction step of compound B in the presence of hydrofluoric acid in said first and second reactors.
• the method comprises:
• the step of regenerating the preliminary catalyst in the third reactor is carried out simultaneously with the regeneration step of the catalyst in the first reactor or the second reactor or both; or in the absence of a catalyst regeneration step in the first reactor or the second reactor or both.
• the first reactor and / or the second reactor may be in the regeneration phase or in the standby phase, that is to say a phase during which no flow circulates or only a flow consisting of an inert gas .
• the reaction step of a compound B in the presence of hydrofluoric acid is carried out alternately with the regeneration step.
• the reactors are made of steel and have an inner surface covered with an alloy comprising more than 30% by weight of nickel or of a fluoropolymer-type coating, preferably the alloy comprising more than 30% by weight of nickel is an Incolloy ® , Inconel ® , Monel ® or Hastelloy ® .
• the tetrafluoropropene is 2,3,3,3-tetrafluoropropene or 1,3,3,3-tetrafluoropropene.
• the compound A is chosen from tetrachloropropenes, chlorotrifluoropropenes, pentachloropropanes, dichlorotrifluoropropanes, trichlorodifluoropropanes, tetrachlorofluoropropanes, dichlorodifluoropropenes, trichlorofluoropropenes and mixtures thereof;
• compound B is chosen from chlorotrifluoropropenes, pentafluoropropanes, dichlorotrifluoropropanes, trichlorodifluoropropanes, tetrachlorofluoropropanes, dichlorodifluoropropenes, trichlorofluoropropenes and mixtures thereof;
• compound B is chosen
• compound B is selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HCFO-1233xf), 1,1,1,2,2-pentafluoropropane (HFC-245cb), and 3,3,3-trifluoro-1-propene (HCFO-1233zd).
• the regeneration flow is in the same direction or in the opposite direction, preferably in the opposite direction, with respect to the direction of introduction into the first reactor or the second reactor of a reaction flow comprising compound B and hydrofluoric acid.
• the direction of the regeneration flow is alternated at each regeneration step.
• the invention also relates to a plant for the manufacture of tetrafluoropropene, comprising three reaction reactors in the gas phase comprising a catalyst bed,
• the first reactor and the second reaction reactor in the gas phase being each configured to be fed alternately by:
• reaction flow supply device comprising a compound B and hydrofluoric acid
• a regeneration flow supply device configured to feed the reactor with a regeneration flow comprising an oxidizing agent
• the third reaction reactor in the gas phase being configured to be fed alternately by: a reaction flow supply device comprising a compound A and hydrofluoric acid and optionally an intermediate collection device connected at the outlet of the first reactor or the second reactor; said compound A being different from said compound B; and a regeneration flow supply device configured to supply the reactor with a regeneration flow comprising an oxidizing agent.
• the installation is configured such that when the first reactor is supplied by the reaction flow supply device, the second reactor is fed by the regeneration flow supply device.
• the regeneration flow supply device is connected at the top and bottom of the reactor.
• the installation is configured such that the regeneration flow supply system feeds any one of the three reactors at the foot and at the head alternately.
• the tetrafluoropropene is 2,3,3,3-tetrafluoropropene or the tetrafluoropropene is 1,3,3,3-tetrafluoropropene.
• the compound A is chosen from tetrachloropropenes, chlorotrifluoropropenes, pentachloropropanes, dichlorotrifluoropropanes, trichlorodifluoropropanes, tetrachlorofluoropropanes, dichlorodifluoropropenes, trichlorofluoropropenes and mixtures thereof;
• compound B is chosen from chlorotrifluoropropenes, pentafluoropropanes, dichlorotrifluoropropanes, trichlorodifluoropropanes, tetrachlorofluoropropanes, dichlorodifluoropropenes, trichlorofluoropropenes and mixtures thereof; preferably compound A is selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 2,3-dichloro-1
• compound B is selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HCFO-1233xf), 1,1,1,2,2-pentafluoropropane (HFC-245cb), and 3,3,3-trifluoro-1-propene (HCFO-1233zd).
• the installation comprises: a first reactor;
• first collection line and a second collection line connected at the outlet of the separation unit, the first collection line being configured to carry a stream comprising hydrochloric acid and tetrafluoropropene and the second collection line being configured to transporting a stream comprising hydrofluoric acid and compound B; an intermediate collection device connected at the outlet of the first reactor and / or the second reactor;
• a first feed device for the third reactor configured to feed the third reactor, the latter being itself fed by the preliminary reaction mixture feed device and optionally by the intermediate collection device;
• a second feed device in a reaction medium configured to alternately feed the second reactor and the first reactor, the latter being itself fed by the second collection line and optionally by a hydrofluoric acid supply device;
• a regeneration flow supply device configured to feed the first reactor and the second reactor
• a regeneration flow supply device configured to feed the third reactor
• the installation comprises:
• first collection line and a second collection line connected at the outlet of the separation unit, the first collection line being configured to carry a stream comprising hydrochloric acid and tetrafluoropropene and the second collection line being configured to transporting a stream comprising hydrofluoric acid and compound B; an intermediate collection device connected to the output of the third reactor; a first feed device of the third reactor configured to feed the third reactor, the latter being itself fed by the preliminary reaction mixture feed device and optionally by the second collection line;
• a second feed device in a reaction medium configured to feed the first reactor or the second reactor, the latter being itself fed by the intermediate collection device and optionally by a hydrofluoric acid supply device;
• a regeneration flow supply device configured to feed the first reactor and the second reactor
• a regeneration flow supply device configured to feed the third reactor
• the reactors of the installation are made of steel and have an inner surface coated with an alloy comprising more than 30% by weight of nickel or a fluoropolymer-type coating, preferably the alloy comprising more than 30% by weight of nickel is Incolloy ® , Inconel ® , Monel ® or Hastelloy ® .
• the present invention overcomes the disadvantages of the state of the art. It more particularly provides a method of manufacturing HFO-1234 (and especially HFO-1234yf) having a high yield and providing the desired product in a high degree of purity, while being more economical.
• the regeneration step can be optimized without the catalyst life being visibly affected over a period of time.
• certain reaction steps can be carried out essentially in the absence of an oxidizing agent.
• the use of reactors which only the inner surface is in an alloy as defined in the present invention makes the process economically more viable while maintaining a high resistance to corrosion.
• FIGS 1a, 1b and 1b show schematically an embodiment of an installation according to the invention with three catalytic reaction reactors in different operating configurations.
• FIGS. 2a, 2b, 2c, 2d and 2e schematically represent an embodiment of an installation according to the invention with three reactors, the third of which is in regeneration mode, in three different configurations.
• FIGS. 3a, 3b and 3c show schematically an embodiment of an installation according to the invention with three reactors comprising a regeneration flow supply device at the bottom and at the reactor head, in three different configurations.
• FIGS. 4a, 4b and 4c schematically represent an embodiment of an installation according to the invention with three reactors comprising a regeneration flow supply device at the bottom and at the reactor head and a separation unit connected to the reactor. the output of the first and second reactors, in three different configurations.
• the invention provides for producing HFO-1234 by catalytic gas phase reaction; this catalytic reaction is, according to the invention, alternated with the regeneration of the catalyst. In some embodiments, the invention provides for the production of HFO-1234 in several steps. According to a first aspect, the present invention provides a process for producing tetrafluoropropene. The process for producing tetrafluoropropene employs three reactors.
• the method according to the present invention comprises in particular a step of implementation, in the first reactor and the second reactor, of at least one step of reaction in the gas phase of a compound B in the presence of hydrofluoric acid and a catalyst; alternating with a step of regenerating the catalyst by bringing it into contact with a regeneration flow comprising an oxidizing agent.
• Said method may also comprise a step of implementation in the third reactor of a preliminary stage of manufacture of compound B, which is preferably a preliminary stage of reaction in the gas phase of a compound A in the presence of hydrofluoric acid and a preliminary catalyst, said compound A being different from said compound B, alternately with a step of regenerating the preliminary catalyst with a regeneration flow comprising an oxidizing agent.
• the step of regenerating the preliminary catalyst in the third reactor can be carried out in the absence of a reaction step of compound B in the presence of hydrofluoric acid in said first and second reactors
• said process for the manufacture of tetrafluoropropene in the three reactors comprises the steps of:
• the step of regenerating the preliminary catalyst in the third reactor being carried out in the absence of a reaction step of compound B in the presence of hydrofluoric acid in said first and second reactors.
• the first reactor and the second reactor are independently of each other is in the regeneration phase of the catalyst or in standby phase during which no flow circulates or a flow consisting of an inert gas such as nitrogen, argon or helium circulates in the reactor in question or the reactor in question is evacuated.
• compound B is meant an organic compound comprising one or more carbon atoms. This compound preferably comprises 3 carbon atoms.
• This compound B is preferably propane or propene having one or more substituents selected from F, Cl, I and Br (preferably from F and Cl).
• the compound B is a propane or propene comprising at least one fluorine atom, in particular comprising two, three, four or five fluorine atoms, more particularly three or five fluorine atoms.
• compound A is meant an organic compound comprising one or more carbon atoms, preferably 3 carbon atoms.
• Compound A is preferably propane or propene having one or more substituents selected from F, Cl, I and Br (preferably from F and Cl).
• compound A is propane or propene comprising at least one chlorine atom, two, three, four or five chlorine atoms.
• compound A has a degree of fluorination lower than that of compound B.
• the compound B may be chosen from chlorotrifluoropropenes, pentafluoropropanes, dichlorotrifluoropropanes, trichlorodifluoropropanes, tetrachlorofluoropropanes, dichlorodifluoropropenes, trichlorofluoropropenes and a mixture thereof.
• the compound A may be chosen from tetrachloropropenes, chlorotrifluoropropenes, pentachloropropanes, dichlorotrifluoropropanes and trichlorodifluoropropanes, tetrachlorofluoropropanes, dichlorodifluoropropenes, trichlorofluoropropenes and mixtures thereof.
• compound B may be selected from the group consisting of 2-chloro
• HCFO-1233xf 3,3,3-trifluoro-1-propene (HCFO-1233xf), 2,3-dichloro-1,1,1-trifluoropropane (HCFC-243db), 1,1,1,2,2-pentafluoropropane (HFC- 245cb) and 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd).
• compound A may be selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HCFO-1233xf), 1,1,1,2,3-pentachloropropane (HCC-240db ), 1,1,2,2,3-pentachloropropane (HCC-240aa), 2,3-dichloro-1,1,1-trifluoropropane (HCFC-243db), 1,1,2,3-tetrachloro-1- propene (HCO-1230xa), 2,3,3,3-tetrachloro-1-propene (HCO-1230xf), 1,1,1,3,3-pentachloropropane (HCC-240fa), 1,1,3,3 tetrachloropropene (HCO-1230za), 1,3,3,3-tetrachloropropene (HCO-1230zd), 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd), 1,1,1,3-
• compound B can be selected from the group consisting of 2-chloro
• compound A can 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).
• HFCO-1233xf 2-chloro-3,3,3-trifluoro-1-propene
• HCFCs 2,3-dichloro-1,1,1-trifluoropropane
• compound B is 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• compound B is 1-chloro-3,3,3-trifluoropropene
• Compound A is 1,1,1,2,3-pentachloropropane (HCC-240db), or 1,1,2,2,3-pentachloropropane (HCC-240aa), or a mixture of both, to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• compound A is 1,1,1,2,3-pentachloropropane (HCC-240db) or 1,1,2,2,3-pentachloropropane (HCC-240aa), or a mixture of both; and compound B is 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• compound A is 2,3-dichloro-1,1,1-trifluoropropane (HCFC-243db) to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• compound A is 2,3-dichloro-1,1,1-trifluoropropane (HCFC-243db)
• compound B is 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• Compound A is 1,1,2,3-tetrachloropropene (HCO-1230xa), or 2,3,3,3-tetrachloropropene (HCO-1230xf), or a mixture thereof. two compounds, to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• the compound A is 1,1,2,3-tetrachloropropene (HCO-1230xa), or 2,3,3,3-tetrachloropropene (HCO-1230xf), or a mixture of these two compounds
• the Compound B is 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• the compound A is 1,1,2,3-tetrachloropropene (HCO-1230xa) or 2,3,3,3-tetrachloropropene (HCO-1230xf) or 1,1,1 2,3-pentachloropropane (HCC-240db) or a mixture of two thereof or a mixture of all three; and compound B is 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), to produce 2,3,3,3-tetrafluoropropene (HFO-1234yf).
• the compound A is 1,1,3,3-tetrachloropropene (HCO-1230za) or 1,3,3,3-tetrachloro-1-propene (HCO-1230zd) or a mixture of two;
• Compound B is 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd) to produce 1,3,3,3-tetrafluoropropene (HFO-1234ze).
• compound A is 1,1,1,3,3-pentachloropropane (HCC-240fa)
• compound B is 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd) to produce 1,3,3,3-tetrafluoropropene (HFO-1234ze).
• the compound B is 1,1,1,2,2-pentafluoropropane (HFC-1)
• compound A is 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf)
• compound B is 1,1,1,2,2-pentafluoropropane (HFC-245cb) to produce 2 , 3,3,3-tetrafluoropropene (HFO-1234yf).
• the conversion of compound B to HFO-1234 may be a direct conversion or an indirect conversion (i.e. involving an intermediate product).
• the reaction of compound B with HFO-1234 is carried out in two gas phase reaction reactors having a catalyst bed.
• the reaction of compound A with compound B is carried out in a gas phase reactor comprising a preliminary catalyst bed.
• Said catalyst used in the first and second reactor may be identical to the preliminary catalyst used in the third reactor.
• the catalyst or preliminary catalyst used in the present process may for example be based on a metal comprising a transition metal oxide or a derivative or a halide or an oxyhalide of such a metal.
• a metal comprising a transition metal oxide or a derivative or a halide or an oxyhalide of such a metal.
• FeC may be mentioned, oxyfluoride chromium, chromium oxides (optionally subjected to fluorination treatments), chromium fluorides and mixtures thereof.
• Other possible catalysts are carbon supported catalysts, antimony catalysts, aluminum catalysts (for example AI F3 and Al2O3, alumina oxyfluoride and alumina fluoride).
• a chromium oxyfluoride a fluoride or an aluminum oxyfluoride, or a supported or non-supported catalyst containing a metal such as Cr, Ni, Fe, Zn, Ti, V, Zr, Mo, Ge or Sn. Pb, Mg, Sb.
• the catalyst is more preferably based on chromium and it is more particularly a mixed catalyst comprising chromium.
• a mixed catalyst comprising chromium and nickel is used for any of the reaction steps.
• the molar ratio Cr / Ni (based on the metal element) is generally 0.5 to 5, for example 0.7 to 2, for example about 1.
• the catalyst may contain from 0.5 to 20% by weight of nickel.
• the metal may be present in metallic form or in the form of a derivative, for example an oxide, halide or oxyhalide. These derivatives are preferably obtained by activation of the catalytic metal.
• the support is preferably made of aluminum, for example alumina, activated alumina or aluminum derivatives, such as aluminum halides and aluminum oxyhalides, for example described in US Pat. US 4,902,838, or obtained by the activation method described above.
• aluminum for example alumina, activated alumina or aluminum derivatives, such as aluminum halides and aluminum oxyhalides, for example described in US Pat. US 4,902,838, or obtained by the activation method described above.
• the catalyst may comprise chromium and nickel in an activated or non-activated form, on a support which has been subjected to activation or not.
• Another preferred embodiment is based on a catalyst or a preliminary mixed catalyst containing chromium and at least one co-catalyst chosen from the salts of Co, Mn, Mg and Zn, preferably Zn.
• Said cocatalyst is preferably present in a content of 1 to 10% by weight based on the weight of the catalyst.
• the catalyst or preliminary catalyst is preferably activated with air, oxygen or chlorine and / or with HF.
• the catalyst is preferably subjected to activation with air or oxygen and HF at a temperature of 100 to 500 ° C, preferably 250 to 500 ° C and more preferably 300 to 400 ° C. ° C.
• the activation time is preferably from 1 to 200 hours and more particularly from 1 to 50 hours.
• This activation may be followed by a final fluorination activation step in the presence of an oxidizing agent, HF and organic compounds.
• the molar ratio of HF / organic compounds is preferably from 2 to 40 and the molar ratio of oxidation agent / organic compounds is preferably from 0.04 to 25.
• the temperature of the final activation is preferably from 300 to 400 ° C. C and its duration preferably from 6 to 100 h.
• contact time 3 to 100 seconds, preferably 4 to 75 seconds and more particularly 5 to 50 seconds (volume of catalyst divided by the total incoming flow, adjusted to the temperature and to the operating pressure);
• a temperature (temperature of the catalyst bed) of 200 to 450 ° C., preferably of 250 to 400 ° C., and more particularly of 280 to 380 ° C.
• the duration of the reaction step is typically from 10 to 8000 hours, preferably from 50 to 5000 hours and more preferably from 70 to 1000 hours.
• An oxidizing agent preferably oxygen
• oxygen may optionally be added during the reaction.
• the oxygen / organic compounds molar ratio may be from 0.005 to 2, preferably from 0.01 to 1.5.
• the oxygen can be introduced pure or in the form of air or oxygen / nitrogen mixture. Oxygen can also be replaced by chlorine.
• reaction step of compound B or compound A in the presence of hydrofluoric acid is carried out essentially in the absence of oxygen, and preferably substantially in the absence of any oxidizing agent.
• said method also comprises:
• said method also comprises: the collection of a product stream at the end of the reaction step of compound B in the presence of hydrofluoric acid;
• the separation of the product streams respectively from the reaction step of compound A with HF or from the reaction step of compound B with HF can be carried out by a separation unit which can be a distillation column or any other suitable device. to separate, on the one hand, hydrochloric acid and tetrafluoropropene and, on the other hand, hydrofluoric acid and compound B.
• each reactor used for carrying out the reaction of compound B or compound A with HF said reaction can be alternated with catalyst regeneration phases. For example, it is possible to go from the reaction phase to the regeneration phase when the conversion of compound B falls below a predetermined threshold, for example 50%. If necessary, beforehand, a transition period consisting in decompressing the gas phase reaction is assured. It may be followed by a sweeping phase using an inert gas or by evacuation in order to completely eliminate the reagents present.
• the regeneration of the catalyst or preliminary catalyst of the present process may comprise the treatment of said catalyst with a gaseous stream containing an oxidant.
• the oxidant used in the regeneration step is oxygen or air or an oxygen / nitrogen mixture or chlorine or a chlorine / nitrogen mixture.
• the proportion of oxygen may be from 5 to about 100 mol% relative to the mixture of oxygen plus nitrogen.
• the regeneration step can be carried out with oxygen or air or an oxygen / nitrogen mixture or chlorine and HF.
• the regeneration flow contains at least 1 mol% oxygen relative to the total regeneration flow.
• the oxygen content may be from about 2 to about 98 mole percent based on the oxygen plus HF mixture, and from about 20 to about 100 mole percent, based on the oxygen plus nitrogen mixture.
• the temperature during the regeneration step may range from 250 to 500 ° C, preferably from 300 to 450 ° C, more preferably from 350 to 400 ° C.
• the regeneration step may be carried out with a contact time of 1 to 200 seconds, preferably 1 to 150 seconds, more preferably 5 to 100 seconds; and for a period of from 1 to about 1500 hours, preferably from 2 to 1000 hours, more preferably from 4 to 500 hours, most preferably from 10 to 200 hours, particularly from 15 to 150 hours.
• the regeneration step may be carried out at a pressure ranging from atmospheric pressure up to 20 bar.
• the temperature during the regeneration step may be about 250 to 500 ° C, with a contact time of about 1 to 200 s, for a period of 10 to 200 hours and a pressure ranging from atmospheric pressure to 20 bar.
• the regeneration step makes it possible to recover the initial activity of the catalyst. Several cycles can thus be chained without significantly altering the activity of the catalyst, which makes it possible to increase its service life.
• the reactor can be evacuated so as to remove the inert gases and the oxygen introduced, prior to reintroduction of the organic compounds in the presence of hydrofluoric acid.
• the step of regenerating the preliminary catalyst in the third reactor is carried out simultaneously with the step of regenerating the catalyst in the first reactor or the second reactor or both; or in the absence of a catalyst regeneration step.
• reaction step as described above is carried out alternately with the regeneration step as described above.
• the reaction and regeneration flows may be in the same direction or reversed, preferably the reaction and regeneration flows are reversed.
• the direction of the regeneration flow is alternated at each regeneration step.
• the reaction and regeneration flows can be in the same direction and then in a second regeneration phase, the reaction and regeneration flows can be reversed.
• the three reactors used in the present process may be made of steel and have an inner surface coated with an alloy comprising more than 30% by weight of nickel or a coating of fluoropolymers type, preferably the alloy comprising more than 30% by weight of nickel may be an Incolloy ®, Inconel ®, Monel ®, Hastelloy ®.
• a facility 1 is provided.
• the tetrafluoropropene manufacturing plant 1 comprises three reactors 2a, 2b and 3 of the gas phase reaction and comprises a catalyst bed 21a, 21b or 21c.
• first reactor 2a and the second reaction reactor 2b in the gaseous phase are each configured to be fed alternately by:
• reaction flow supply device 16 comprising a compound B and hydrofluoric acid
• a regeneration flow supply device 11 configured to feed the reactor with a regeneration flow comprising an oxidizing agent.
• the third reaction reactor 3 in the gas phase can be configured to be powered alternately by:
• reaction flow supply device comprising a compound A and hydrofluoric acid and optionally a collection device intermediate 19 connected at the output of the first reactor 2a or the second reactor 2b; said compound A being different from said compound B; and a regeneration flow supply device 14 configured to feed the reactor with a regeneration flow comprising an oxidizing agent.
• the reaction stream 16 or 13 may be substantially free of oxygen, and preferably any oxidizing agent.
• the regeneration flow 11 or 14 may contain at least 1 mol% oxygen relative to the total regeneration flow.
• the installation can be configured so that when the first reactor 2a is supplied by the reaction flow supply device 16, the second reactor 2b is fed by the regeneration flow supply device 11.
• the reactor outlet 2a and 2b are connected to both a flow collection device of the products resulting from the reaction and a gas flow collection device resulting from the regeneration.
• collection device or feeder means a single pipe or a set of several pipes.
• An inlet valve device 7, 8 and an outlet valve device 5, 6 are provided to allow switching between the reaction flow supply devices 16 or the regeneration flow 11 and the respective collection devices 12 and 19.
• first reactor 2a and second reactor 2b are provided to allow switching between the reaction flow supply devices 16 or the regeneration flow 11 and the respective collection devices 12 and 19.
• the regeneration flow supply device 11 or 14 is connected at the top and at the bottom of the reactor 2a, 2b or 3. This may for example be implemented by a regulator of the regeneration flow forming an integral part regeneration flow supply device 11, 14.
• Said regeneration flow control device may comprise a plurality of pipes and at least two control valves 25, 25 'or 24, 24' as illustrated for example in FIG. Figure 3a.
• the installation 1 is configured such that each of the regeneration flow supply devices 11 or 14 respectively feeds the first reactor 2a and the second reactor 2b or the third reactor 3 at the bottom and at the head alternately.
• the configuration of the valves 25, 25 'or 24, 24' of the regulator of the regeneration flow makes it possible to easily regulate the regeneration flows 11 or 14 to alternate a regeneration of a reactor at the top and a regeneration of a reactor. foot.
• the first reactor 2a, the second reactor 2b and / or the third reactor 3 can be regenerated in series, that is to say that the flow of gas resulting from the regeneration of one of the reactors 2a or 2b is fed to the other reactor 2a or 2b or the third reactor 3 and is used for the regeneration of the catalyst contained therein.
• the plant 1 is suitable for the manufacture of tetrafluoropropene, advantageously tetrafluoropropene is 2,3,3,3-tetrafluoropropene; or the tetrafluoropropene is 1,3,3,3-tetrafluoropropene.
• Compounds A and B are as described above in connection with the process for producing tetrafluoropropene.
• the installation 1 comprises:
• first collection line 15 and a second collection line 17 connected at the outlet of the separation unit 4, the first collection line 15 being configured to carry a stream comprising hydrochloric acid and tetrafluoropropene and the second line of wherein the collection 17 is configured to carry a stream comprising hydrofluoric acid and compound B;
• an intermediate collection device 19 connected at the outlet of the first reactor 2a or the second reactor 2b;
• a first feed device for the third reactor 20 configured to feed the third reactor 3, the latter being itself fed by the preliminary reaction mixture feed device 13 and optionally by the intermediate collection device 19; a second feed device in a reaction medium 16 configured to alternately feed the second reactor 2b and the first reactor 2a, the latter being itself fed by the second collection line 17 and optionally by an acid feed device hydrofluoric 10; a regeneration flow supply device 11 configured to feed the first reactor 2a and / or the second reactor 2b;
• a regeneration flow supply device 14 configured to feed the third reactor 3
• the feed device of the third reactor 20 is configured to feed the third reactor 3 with a regeneration flow comprises an oxidizing agent from the feed device in regeneration flow 14.
• the installation can include:
• a product stream collection device 19 connected at the outlet of the first reactor 2a and the second reactor 2b;
• first collection line 15 and a second collection line 17 connected at the outlet of the separation unit 4, the first collection line 15 being configured to carry a stream comprising hydrochloric acid and tetrafluoropropene and the second line of wherein the collection 17 is configured to carry a stream comprising hydrofluoric acid and compound B;
• a first feed device for the third reactor 20 configured to feed the third reactor 3, the latter being itself fed by the preliminary reaction mixture feed device 13 and optionally by the second collection line 17;
• a second feed device in a reaction medium 16 configured to feed the first reactor 2a or the second reactor 2b, the latter being itself fed by the intermediate collection device 18 and optionally by a hydrofluoric acid supply device 10 ;
• a regeneration flow supply device 11 configured to feed the first reactor 2a and / or the second reactor 2b;
• a regeneration flow supply device 14 configured to feed the third reactor 3
• the feed device of the third reactor 20 is configured to feed the third reactor 3 with a regeneration flow comprises an oxidizing agent from the feed device in regeneration flow 14.
• the second collection line 17 can feed the feed device in a reaction medium 16 configured to feed the first reactor 2a or the second reactor 2b rather than feed the feed device of the third reactor 20 configured to power the third reactor 3.
• the regeneration flow supply device configured to feed the first reactor 2a and the second reactor 2b is common to the regeneration flow supply device configured to feed the third reactor 3; that is, a single regeneration flow supply device is used to feed the three reactors.
• the regeneration flow supply device is then configured for this purpose.
• the reactors used for the manufacture of tetrafluoropropene are made of steel and have an inner surface coated with an alloy comprising more than 30% by weight of nickel or a fluoropolymer-type coating, preferably the alloy comprising more than 30% by weight of nickel is a Incolloy ®, Inconel ®, Monel ®, Hastelloy ®.
• Figure la illustrates an installation according to an embodiment of the present invention wherein a reaction step of a compound B is carried out in the first reactor 2a.
• the reactor 2b is in the regeneration phase.
• a reaction step of a compound A is carried out in the third reactor 3.
• Each of the reactors 2a, 2b and 3 respectively comprises a catalyst bed 21a, 21b or preliminary catalyst 21c.
• the first reactor 2a is supplied with reaction mixture, ie compound B and hydrofluoric acid, at the bottom via the feed device 16, the latter being supplied by a hydrofluoric acid supply device 10 and by the second collection line 17 from the separation unit 4.
• the valve 7 is positioned to allow the delivery of the reaction mixture to the first reactor 2a.
• the second reactor 2b is connected in foot to a regeneration flow supply device 11 via a valve 8.
• the valves 7 and 8 connected to the first reactor 2a and the second reactor 2b allow the passage of the reactors of a configuration in which a catalytic reaction is carried out at a configuration in which a regeneration step is performed.
• the flow of products from the first reactor 2a is conveyed to the intermediate collection device 19 via a valve 5 configured for this purpose.
• the regeneration flow exits the second reactor 2b to be routed to the gas flow collection device from the regeneration 12; this being regulated by means of the valve 6.
• the valve 22 makes it possible to regulate the flows entering the supply device of the third reactor 20.
• the supply device of the third reactor 20 can be fed by the flows coming from the intermediate collection device 19 and the preliminary reaction mixture supply device 13, or said feeder of the third reactor 20 can be fed by a regeneration flow supply device 14.
• the flow entering the third reactor 3 is brought into contact with the catalytic bed 21c.
• the flow of products from the third reactor 3 is then conveyed to the separation unit 4 by the product flow collection device of the third reactor 18.
• the valve 24 makes it possible to direct the flow of products towards the separation unit 4 or to a gas flow collection device resulting from the regeneration of the third reactor 12 '.
• the separation unit 4 comprises a first conduit 15 and a second conduit 17.
• the first collection conduit 15 is configured to carry a stream comprising hydrochloric acid and tetrafluoropropene and the second collection conduit 17 is configured to carry a flow comprising hydrofluoric acid and compound B.
• the regeneration flow in the second reactor 2b and the flow of the reaction mixture in the first reactor 2a are in the same direction.
• FIG. 1b illustrates an embodiment identical to that shown in FIG. 1a, except for the direction of the regeneration and reaction flows, ie of the reaction mixture, in the first reactor 2a and the second reactor 2b.
• the regeneration flow in the second reactor 2b and the reaction flow in the first reactor 2a are reversed.
• the regeneration flow supply device 11 feeds the second reactor 2b through the head via the valve 6 while the reaction mixture supply device 16 always feeds the first reactor by the foot thereof.
• the regeneration flow exits the second reactor 2b to be routed to the gas flow collection device from the regeneration 12 through the valve 8.
• the third reactor 3 is configured as described in Figure la.
• FIG. 1 illustrates an embodiment in which the first reactor 2a is in the regeneration phase while the second reactor 2b is in the reaction phase.
• the second reactor 2b is fed by the reaction mixture supply device 16 via the valve 8 configured for this purpose.
• the flow of products from the second reactor 2b feeds the intermediate collection device 19.
• the first reactor 2a is fed by the regeneration flow supply device 11 by the reactor head.
• the gases present in the first reactor are in this case at the bottom of the reactor to the gas flow collection device from the regeneration 12.
• the valves 5 and 7 are thus configured to allow the passage of the regeneration flow inside. of the first reactor 2a.
• the third reactor 3 is configured as described in FIG.
• FIGS. 2a, 2b, 2c, 2d and 2e illustrate embodiments in which the third reactor 3 is in the regeneration phase.
• the first reactor 2a and the second reactor 2b are not in the reaction phase.
• the first reactor 2a and the second reactor 2b are independently of each other either in the regeneration phase or in the standby phase during which no flow circulates within them.
• FIG. 2a illustrates an installation according to an embodiment in which a catalyst regeneration stage is carried out in the first reactor 2a and in the second reactor 2b.
• a step of regeneration of the preliminary catalyst is carried out in the third reactor 3.
• Each of the reactors 2a, 2b and 3 respectively comprises a catalyst bed 21a, 21b or preliminary catalyst 21c.
• the first reactor 2a and the second reactor 2b are fed at the top by a regeneration flow delivered by the regeneration flow supply device 11.
• the valves 5 and 6 are positioned so as to allow the flow of regeneration flow to be conveyed to the first reactor 2a and the second reactor 2b.
• the flow of gas resulting from the regeneration in the first reactor 2a and the second reactor 2b are evacuated towards the gas flow collection device resulting from the regeneration 12.
• the valves 7 and 8 are configured so as to allow the flow of gas to flow. gas resulting from the regeneration of the reactors 2a and 2b towards the gas flow collection device resulting from the regeneration 12.
• the third reactor 3 is supplied at the bottom by a supply device 20 comprising a regeneration flow coming from the device regeneration flow supply 14 via the valve 22 configured for this purpose.
• the regeneration flow passes through the catalytic bed 21c of the third reactor 3.
• the flow of gas from the regeneration leaves the top of the third reactor 3 to the device for collecting products from the third reactor 18.
• This flow of regeneration gas is conveyed to the device for collecting the gas flows resulting from the regeneration 12 '.
• the valve 24 is thus configured to connect the product collection device from the third reactor 18 with the gas flow collection device from the regeneration 12 '.
• the device for collecting the gas flows resulting from the regeneration 12 ' can be identical to the device for collecting the gas flows resulting from the regeneration 12.
• the device for collecting products coming from the third reactor 18 is connected to the device for collecting the gas flows resulting from the regeneration 12, the latter also being fed by the gas flows resulting from the regeneration of the first reactor 2a. and the second reactor 2b.
• FIG. 2b illustrates an embodiment of the present invention in which the second reactor 2b and the third reactor 3 are in the regeneration phase while the first reactor 2a is in the standby phase.
• the second reactor 2b is fed at the top by the regeneration flow supply device 11.
• the regeneration flow passes through the catalytic bed 21b to exit at the bottom of the second reactor 2b and is conveyed to the flow collection device. gas from the regeneration 12.
• the third reactor 3 is fed in foot by a supply device 20 comprising a regeneration flow from the regeneration flow supply device 14 via the valve 22 configured for this purpose.
• the regeneration flow passes through the catalytic bed 21c of the third reactor 3.
• the flow of gas from the regeneration leaves the top of the third reactor 3 to the device for collecting products from the third reactor 18.
• This flow of regeneration gas is conveyed to the device for collecting the gas flows resulting from the regeneration 12 '.
• the valve 24 is thus configured to connect the device for collecting products from the third reactor 18 with the device for collecting the gas flows resulting from the regeneration 12 '. No flow circulates in the first reactor 2a. Valves 5 and 7 are configured for this purpose.
• FIG. 2c illustrates a particular embodiment of the present invention in which the second reactor 2b and the third reactor 3 are in the regeneration phase while the first reactor 2a is in the standby phase, the second reactor 2a and the third reactor 3 being supplied with regeneration flow by the same regeneration flow supply device 11.
• the regeneration flow 11 is conveyed to the third reactor 3 via the supply device 20 and the valve 22 configured to this. effect.
• FIG. 2d illustrates a particular embodiment of the present invention in which the first reactor 2a, the second reactor 2b and the third reactor 3 are in the regeneration phase.
• the first reactor 2a and the second reactor 2b are regenerated in series.
• the regeneration flow 11 feeds the second reactor 2b through the reactor head via the valve 6.
• the regeneration flow is discharged at the bottom of the reactor 2b to be conveyed via the valve 8, the pipe 30 and the valve 5 to the reactor 2. head of the first reactor 2a.
• the regeneration flow is injected into the first reactor 2a to exit at the bottom of the reactor.
• the gas flow resulting from the regeneration is collected in the device for collecting the gas flows resulting from the regeneration 12.
• FIG. 2e illustrates a particular embodiment of the present invention in which the second reactor 2b and the third reactor 3 are in the regeneration phase while the first reactor 2a is in the standby phase.
• the second reactor 2b and the third reactor 3 are regenerated in series by the same regeneration flow supply device 11.
• the regeneration flow 11 is conveyed to the third reactor 3 via the feed device 20 and valves 6 and 22 configured for this purpose.
• the flow of gas resulting from the regeneration leaves at the top of the third reactor 3 towards the device for collecting products from the third reactor 18.
• This flow of regeneration gas is conveyed towards the device for collecting the gas flows resulting from the regeneration 12 .
• the valve 24 ' is thus configured to connect the product collection device from the third reactor 18 with the gas flow collection device from the regeneration 12'.
• FIG. 3a illustrates a particular embodiment of the present invention in which the second reactor 2b and the third reactor 3 are in the regeneration phase, the first reactor 2a being in the standby phase.
• the reactors can be supplied with regeneration flow either at the top or at the bottom of the reactor by a device configured to be connected both at the top and at the bottom of the reactors. This allows alternating regeneration by the reactor foot and the reactor head.
• the second reactor 2b is powered at the head by the regeneration flow supply device 11 via valves 25 and 6 configured for this purpose.
• the regeneration flow passes through the catalytic bed 21b to exit at the bottom of the second reactor 2b and is conveyed to the collection device of the gas stream from the regeneration 12 through the valves 8 and 25 '.
• the third reactor 3 is fed at the head by a supply device 20 comprising a regeneration flow from the regeneration flow supply device 14 via the valve 24 configured for this purpose.
• the regeneration flow passes through the catalytic bed 21c of the third reactor 3.
• the flow of gas from the regeneration leaves the foot of the third reactor 3 to the collection device of products from the third reactor 18.
• This flow of regeneration gas is routed to the device for collecting the gas flows resulting from the regeneration 12 '.
• the valve 24 ' is thus configured to connect the product collection device from the third reactor 18 with the gas flow collection device from the regeneration 12'. No flow circulates in the first reactor 2a.
• the third reactor 3 can be regenerated by the foot of the reactor. This is illustrated in Figure 3b.
• the first reactor 2a and the second reactor 2b are configured identically to that detailed in connection with FIG. 3a.
• the third reactor 3 is in turn powered by a feeder 20 comprising a regeneration flow from the regeneration flow supply device 14 via the valves 22 and 24 'configured for this purpose.
• the flow of gas from the regeneration is conveyed to the product collection device 18 at the reactor head.
• This flow of regeneration gas is conveyed to the device for collecting the gas flows resulting from the regeneration 12 '.
• the valve 24 is thus configured to connect the product collection device from the third reactor 18 with the gas flow collection device from the regeneration 12 '.
• FIG. 3c illustrates a particular embodiment of the present invention in which the three reactors are in the regeneration phase.
• the first reactor 2a and the second reactor 2b are supplied with regeneration flow by the regeneration flow supply device 11.
• the valves 5, 6 and 25 are configured to allow this routing.
• the first reactor 2a and the second reactor 2b are fed at the top by the regeneration flow which crosses respectively the catalytic bed 21a and 21b.
• the flow of gas resulting from the regeneration is discharged from the first reactor 2a and the second reactor 2b to the gas flow collection device from the regeneration 12.
• the valves 7, 8 and 25 ' are configured to allow this routing.
• the third reactor 3 is regenerated by the reactor foot.
• the third reactor 3 is thus powered on foot by a feed device 20 comprising a regeneration flow from the regeneration flow supply device 14 via the valves 22 and 24 'configured for this purpose.
• the flow of gas from the regeneration is conveyed to the product collection device 18 at the reactor head.
• This flow of regeneration gas is conveyed to the device for collecting the gas flows resulting from the regeneration 12 '.
• the valve 24 is thus configured to connect the product collection device from the third reactor 18 with the gas flow collection device from the regeneration 12 '.
• the device for collecting products from the third reactor 18 is connected to the device for collecting the gas flows resulting from the regeneration.
• the latter being also fed by the gas flows from the regeneration of the first reactor 2a and the second reactor 2b.
• the direction of the regeneration flow can be modified in the first reactor 2a, the second reactor 2b and / or the third reactor 3.
• the valves 5, 6, 7, 8, 22, 24, 24 ', 25 and 25' are then configured to allow the routing of the regeneration flow in the desired direction. This can be determined according to the presence or not of coke in the reactor considered, and especially where the coke is formed, ie at the bottom or at the top of the reactor.
• FIGS. 1a to 3c illustrate an installation in which the separation unit is disposed at the outlet of the third reactor so as to treat the flow of products resulting therefrom.
• Figures 4a to 4c illustrate an installation in which the separation unit is disposed at the outlet of the first reactor 2a and the second reactor 2b.
• the first reactor 2a is in the reaction phase, that is to say that a step of catalytic reaction of compound B in the presence of HF is carried out in this phase.
• the third reactor 3 is in the compound B production phase, ie the reaction of compound A with HF.
• the second reactor 2b is in the regeneration phase.
• the third reactor 3 is fed by the feed device of the third reactor 20 by a reaction mixture stream from the preliminary reaction mixture feed device 13 and the second collection line 17.
• the preliminary reaction mixture comprises the compound A and hydrofluoric acid.
• the second collection line 17 may comprise hydrofluoric acid and 2-chloro-trifluoropropene.
• a valve 22 regulates the flows from the preliminary reaction mixture feed device 13 and the second collection line 17.
• a valve 26 and an intermediate line 27 may be arranged between the second collection line 17 and the valve 22
• the valve 26 can make it possible to convey the products of the second collection line 17 to the first reactor 2a and the second reactor 2b through an intermediate pipe 28 and the feeder 16 without passing through the third reactor 3.
• the preliminary reaction mixture from the feed device of the third reactor 20 comes into contact with the preliminary catalyst contained in the catalytic bed 21c.
• the products of the reaction are conveyed via the product stream collection device of the third reactor 18 to the feed device 16 of the first reactor 2a or the second reactor 2b.
• the product flow collection device of the third reactor 18 comprises in particular compound B.
• the products from the third reactor can be mixed with hydrofluoric acid from the hydrofluoric acid supply device 10 and / or with the products conveyed by the second collection line 17 via the intermediate pipe 28 to form the reaction mixture used in the reaction stage implemented in the first reactor 2a.
• the reaction mixture is contacted in the first reactor 2a with the catalyst contained in the catalytic bed 21a.
• the products resulting from this reaction step in the first reactor 2a are conveyed to the intermediate collection device 19 and to the separation unit 4 described with reference to FIG.
• the second reactor 2b is in the regeneration phase.
• the regeneration flow is conveyed by the regeneration flow supply device 11 to the head of the second reactor 2b.
• the stream of gas resulting from the regeneration of the catalyst contained in the catalytic bed 21b is conveyed towards the device for collecting the gas flows resulting from the regeneration 12.
• the direction of the reaction flow and of the regeneration flow is reversed in this mode of production.
• FIG. 4b illustrates an embodiment in which the first reactor 2a is in the regeneration phase and the second reactor 2b implements a step of reaction of compound B with HF.
• the third reactor 3 implements a step of reaction of a compound A with HF as described in FIG. 4a.
• the flows in the first reactor 2a and the second reactor 2b are in the same direction.
• FIG. 4c illustrates an embodiment as described with reference to FIG. 4a except that the products of the second collection line 17 are conveyed to the first reactor 2a via an intermediate pipe 28 and the supply device 16 without passing through the third reactor 3.
• the invention makes it possible to optimize the manufacture of tetrafluoropropene (HFO-1234yf or
• HFO-1234ze by alternating the regeneration and fabrication cycles of tetrafluoropropene with three reactors.
• the invention also makes it possible to improve the regeneration step by alternatively to perform this alternately by the foot or the head of the reactor to avoid the accumulation of coke in the reactor.

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• 2016
  • 2016-05-19 FR FR1654445A patent/FR3051469B1/fr not_active Expired - Fee Related
• 2017
  • 2017-05-17 EP EP17731203.0A patent/EP3458437A1/de not_active Withdrawn
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