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
• • 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
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/38—Separation; Purification; Stabilisation; Use of additives
  • C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
  • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
  • F25J1/0022—Hydrocarbons, e.g. natural gas
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
  • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
  • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/38—Separation; Purification; Stabilisation; Use of additives

Definitions

• the present invention relates to a process for producing 2,3,3,3-tetrafluoropropene (HFO-1234yf), especially from 1,1,1,2,3-pentachloropropane (HCC-240db) and / or 1, 1, 2,2,3-pentachloropropane (HCC-240aa), and an installation adapted to the implementation of this process.
• HFO-1234yf 2,3,3,3-tetrafluoropropene
• HCC-240db 1,1,1,2,3-pentachloropropane
• HCC-240aa 1, 1, 2,2,3-pentachloropropane
• the compound 2,3,3,3-tetrafluoropropene (HFO-1234yf) is particularly interesting in this regard.
• US 2009/0240090 discloses the reaction of 1,1,1,2,3-pentachloropropane (HCC-240db) to 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf) in the absence oxygen.
• HCFO-1233xf thus produced is converted to 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb).
• WO 2009/015317 describes the reaction of a chlorinated compound such as 1,1,2,3-tetrachloropropene (HCO-1230xa), HCC-240db or 2,3,3,3-tetrachloropropene (HCO-1230xa). 1230xf) with hydrogen fluoride (HF) in the gas phase. This process makes it possible to obtain HCFO-1233xf.
• WO 2005/108334 describes the reaction of HCC-240db with HF to give 2-chloro-1,1,1,3-tetrafluoropropane (HCFC-244db), which is then dehydrochlorinated to provide 1, 3.3 3-tetrafluoropropene (HFO-1234ze).
• WO 2010/123148 discloses the fluorination of HCC-240db to HCFO-1233xf in the absence of catalyst.
• the operating pressure necessary for the separation by distillation is greater than 5 bar, or even greater than 7 bar.
• the reactor must therefore be operated at a still higher pressure. This is problematic, since in some configurations it is desirable to operate at a relatively low pressure in the reactor.
• the invention firstly relates to a process for producing 2,3,3,3-tetrafluoropropene comprising:
• the flow of unreacted hydrogen fluoride also comprises organic compounds intermediate to the fluorination reaction and / or organic compounds resulting from side reactions.
• the flow of unreacted hydrogen fluoride is recycled to the fluorination reaction.
• the fluorination reaction is a catalytic fluorination reaction in the gas phase.
• the fluorination reaction is carried out at a pressure lower than that of the distillation of the compressed gaseous fraction and the compressed liquid fraction.
• the fluorination reaction is carried out at a pressure of 0.1 to 10 bar abs, and preferably from 0.3 to 8 bar abs; and / or the distillation is carried out at a pressure of 5 to 40 bar abs, and more preferably 7 to 25 bar abs.
• the gaseous fraction represents from 25 to 60% of the partially condensed flow
• the liquid fraction represents from 40 to 75% of the partially condensed flow, in mass proportions.
• the distillation step comprises:
• the distillation step comprises:
• the compressed gaseous fraction and the compressed liquid fraction are introduced at different locations of a distillation column.
• the stream of 2,3,3,3-tetrafluoropropene undergoes one or more additional purification steps, preferably chosen from washing, extraction, decantation and distillation.
• the halopropane and / or halopropene is a chloropropane and / or chloropropene, and is preferably selected from 1, 1, 1, 2,3-pentachloropropane, 1, 1, 2,2,3 pentachloropropane, 1,1,2,3-tetrachloropropene, 2,3,3,3-tetrachloropropene, 1,1,1-trifluoro-2-chloropropene and 1,1,1-trifluoro- dichloropropane and mixtures thereof.
• the invention also relates to an installation for producing 2,3,3,3-tetrafluoropropene comprising:
• At least one fluorination reactor fed with halopropane and / or halopropene and with hydrogen fluoride;
• distillation means supplied by the compressed gas fraction supply line and the compressed liquid fraction supply line;
• the unreacted hydrogen fluoride withdrawal line feeds the fluorination reactor.
• the installation comprises heating means on the gas fraction withdrawal line.
• the distillation means comprise a first distillation column and a second distillation column, the compressed gas fraction feed line and the compressed liquid fraction feed line feeding the first distillation column.
• the unreacted hydrogen fluoride withdrawal line is connected at the bottom of the first distillation column
• An intermediate flow withdrawal line is connected to the top of the first distillation column and feeds the second distillation column;
• the hydrochloric acid withdrawal line is connected to the top of the second distillation column;
• the 2,3,3,3-tetrafluoropropene withdrawal line is connected at the bottom of the second distillation column.
• the hydrochloric acid withdrawal line is connected to the top of the first distillation column
• An intermediate flow withdrawal line is connected to the bottom of the first distillation column and feeds the second distillation column;
• the 2,3,3,3-tetrafluoropropene withdrawal line is connected at the top of the second distillation column;
• the unreacted hydrogen fluoride withdrawal line is connected to the bottom of the second distillation column.
• the compressed gaseous fraction supply line and the compressed liquid fraction feed line feed the first distillation column at different stages thereof.
• the 2,3,3,3-tetrafluoropropene withdrawal line feeds additional purification means, preferably selected from washing, extraction, decantation and distillation means.
• the present invention overcomes the disadvantages of the state of the art. It more particularly provides a process for producing HFO-1234yf in which the fluorination reaction can be carried out at moderate pressure, in a simple and economical manner, and in particular without having to resort to a compressor capable of compressing a flow rate. too much gas.
• the gaseous fraction advantageously comprises a low HF content, the HF being predominantly in the liquid fraction.
• the design of the compressor is simplified, especially in terms of choice of materials, this compressor does not have to be in contact with a high amount of HF.
• the invention makes it possible to operate the fluorination reaction and the separation of the products resulting from the reaction at optimal and independent pressures.
• the invention provides for the injection of the liquid fraction and the gaseous fraction at different stages of a separation column, which makes it possible to optimize the design of the separation column in terms of number of theoretical stages and reflux rates to implement.
• the size of the column and the thermal power required for the condenser and the reboiler of the column can thus be minimized, as well as the size of the cold group associated with the condenser.
• Figure 1 schematically shows an installation according to a first embodiment of the invention.
• Figure 2 schematically shows an installation according to a second embodiment of the invention.
• an installation according to the invention generally comprises a fluorination reactor 6. It is also possible to use two or more reactors arranged in series. This fluorination reactor is supplied with halopropane and / or halopropene via a hydrohalocarbon feed line 4, and with HF via an HF 2 feed line.
• halopropane or halopropene it is possible in particular to use any chlorofluoropropane and / or chlorofluoropropene, or, according to a preferred embodiment, any chloropropane and / or chloropropene.
• halopropanes and halopropenes are HCC-240db, HCC-240aa, HCO-1230xa and HCO-1230xf, or alternatively HCFO-1233xf and HCFC-243db (2,3-dichloro-1,1,1- trifluoropropane). Mixtures of these compounds are also possible.
• the HCC-240db is converted into HFO-1234yf by reaction with HF in the fluorination reactor 6.
• the content of HFO-1234yf in the stream resulting from the reaction is preferably at least 0.5 mol%, especially of at least 1 mol%, and more preferably at least 2 mol% or at least 3 mol%.
• HCFO-1233xf and HFC-245cb (1, 1, 1, 2,2-pentafluoropropane) in the case of a reaction from HCC-240db.
• the fluorination reactor 6 is a catalytic reactor containing a catalyst.
• the catalyst is for example based on a metal comprising a transition metal oxide or a derivative or a halide or an oxyhalide of such a metal.
• catalysts are FeCb, chromium oxyfluoride, chromium oxides (optionally subjected to fluorination treatments), chromium fluorides and mixtures thereof.
• Other possible catalysts are carbon supported catalysts which are based on antimony and on aluminum (AlF 3 , Al 2 O 3 , alumina oxyfluoride, aluminum fluoride).
• catalysts which can be used are chromium oxyfluoride, fluoride and aluminum oxyfluoride and supported or non-supported catalysts containing a metal such as Cr, Ni, Zn, Ti, V, Zr, Mo, Ge, Sn, Pb, Mg.
• a metal such as Cr, Ni, Zn, Ti, V, Zr, Mo, Ge, Sn, Pb, Mg.
• the catalyst Prior to use, the catalyst is activated, typically with air, oxygen, or chlorine and / or with HF, under appropriate conditions.
• a mixed catalyst containing both chromium and nickel is used.
• the Cr: Ni molar ratio, in metallic elements, is generally from 0.5 to 5, for example from 0.7 to 2, for example of approximately 1.
• the catalyst may comprise, by weight, from 0.5 to 20% of chromium and from 0.5 to 20% of nickel, preferably from 2 to 10% of each metal.
• the metal may be present in metallic form or in the form of a derivative, in particular oxide, halide or oxyhalide.
• a derivative in particular oxide, halide or oxyhalide.
• These derivatives, in particular halides and halides oxides, are obtained by activation of the catalytic metal. Although activation of the metal is not necessary, it is preferred.
• the support is preferably prepared from aluminum, for example alumina, activated alumina or aluminum derivatives.
• These derivatives include aluminum halides and aluminum oxide halides, for example as described in US 4,902,838, or obtained by activation.
• the catalyst may comprise chromium and nickel in activated or unactivated form, on a support which has been subjected to activation or not.
• the catalyst may also be high surface area Cr, which is preferably unsupported.
• the catalyst may contain a low content of one or more co-catalysts such as Co, Zn, Mn, Mg and Ni salts.
• a preferred cocatalyst is Ni.
• Another preferred cocatalyst is Zn.
• Another preferred cocatalyst is Mg.
• a description of the high surface area Cr catalyst is disclosed in WO 2009/158321, p. 4 and 6.
• the process according to the invention is preferably carried out continuously, which is highly advantageous from an industrial point of view.
• a molar ratio of HF to organic compounds is used which is from 4: 1 to 100: 1, and preferably from 5: 1 to 50: 1.
• the use of superstoichiometric ratios for the fluorination reaction is taught, for example, in WO 2008/054781 and WO 2008/040969.
• the reaction can be carried out at a pressure of from 0.1 to 10 bar abs, and preferably from 0.3 to 8 bar abs.
• the reaction can be carried out at a temperature of 100 to 500 ° C, preferably 200 to 450 ° C.
• the temperature of the reactor bed may be substantially uniform or may vary along the flow, increasing or decreasing.
• the contact time (catalyst volume divided by the total flow rate of the reagents and other input compounds, adjusted according to the pressure and the reaction temperature) is typically 1 to 100 seconds, preferably 5 to 50 seconds.
• the fluorination reactor 6 is supplied with oxygen by an oxygen supply line 5.
• the molar ratio of oxygen with respect to the organic compounds is preferably from 0.005 to 2 and more preferably from 0.01 to 1.5.
• the oxygen can be introduced in quasi-pure form or in the form of air, or in the form of a nitrogen / oxygen mixture.
• a polymerization inhibitor may also be used to extend the life of the catalyst, typically at a concentration of 50 to 1000 ppm, more preferably 100 to 500 ppm. It can be chosen in particular from p-methoxyphenol, t-amylphenol, limonene, d, 1-limonene, quinones, hydroquinones, epoxides, amines and mixtures thereof. P-Methoxyphenol and t-amylphenol are preferred.
• the co-supply of polymerization inhibitor (not shown in the drawings) can make it possible to control the polymerization of chloroolefins and thus in particular to extend the life of the catalyst described in US Pat. No. 5,714,651, incorporated herein by reference. Treatment of the flux resulting from the fluorination reaction
• the flow resulting from the reaction is recovered in a line 7 of reaction gases connected at the outlet of the fluorination reactor 6.
• This flow is cooled, and partially condensed, by means of cooling and partial condensation 8 (such as exchangers and economizers ) which are fed by the line 7 of reaction gases.
• the flow temperature after cooling and partial condensation is -50 to 100 ° C, preferably -40 to 80 ° C. The chosen temperature depends on the pressure used (from vacuum to about 8 bar abs).
• a partially condensed flow transport line 9 is connected at the outlet of the cooling and partial condensation means 8. It transports the flow resulting from the reaction, after its cooling and its partial condensation.
• the partially condensed flow transport line 9 feeds a separation tank 10, which makes it possible to separate the partially condensed stream into a gaseous fraction and a liquid fraction.
• the separating flask 10 is a horizontal or vertical reservoir capable of physically separating the gases from the liquids, preferably without the addition of energy.
• the liquid fraction is recovered at the bottom of the separation flask 10 and collected by a liquid fraction withdrawal line 18.
• the gaseous fraction is recovered at the top of the separation flask 10 and collected by a gas fraction withdrawal line 1 1, 13.
• the gaseous fraction represents from 25 to 60% of the flux, and the liquid phase from 40 to 75% of the flux, in mass proportions.
• Heating means 12 are provided on the gas fraction withdrawal line 1 1, 13, in order to heat the gaseous fraction and thus avoid any condensation during the subsequent compression.
• the gas fraction withdrawal line 1 1, 13 feeds a compressor 14.
• the compressor is made of corrosion-resistant materials, such as 316L stainless steel, Hastelloy® or Inconel®.
• the pressure is preferably 5 to 40 bar abs, and more preferably 7 to 25 bar abs.
• the compressed gaseous fraction is collected by a compressed gaseous fraction feed line 15, 17 connected at the outlet of the compressor 14.
• Cooling means 16 may be provided on the compressed gaseous fraction supply line 15, 17, in the compressed gas fraction. In order to cool and possibly partially condense the compressed gaseous fraction before the separation and purification steps.
• the compressed gaseous fraction is thus cooled to a temperature of -10 to 50 ° C.
• the liquid fraction withdrawal line 18 opens onto a pump 19.
• This pump 19 makes it possible to convey the liquid fraction to the means of separation and purification, by a compressed liquid fraction feed line 20.
• the means for separating and purifying the flow resulting from the reaction mainly comprise distillation means.
• the distillation means are preferably operated at a pressure of 5 to 40 bar abs, and more preferably 7 to 25 bar abs.
• the distillation means comprise a first distillation column 21 and a second distillation column 23.
• Each distillation column is provided with a reboiler at the bottom and a condensation and reflux system at the head, in a manner known per se.
• the first distillation column 21 is fed with the flow from the reaction.
• the compressed liquid fraction supplied by the compressed liquid fraction supply line 20
• the compressed gaseous fraction supplied by the compressed gaseous fraction feed line 15, 17
• the function of the first distillation column 21 is to separate HCl and HFO-1234yf on the one hand, and HF and organic compounds (chlorinated and / or fluorinated) on the other hand.
• an intermediate flow withdrawal line 22 is connected at the top of the first distillation column 21, and an unreacted hydrogen fluoride withdrawal line 1 is connected at the bottom of the first distillation column 21.
• the intermediate stream transported in the intermediate stream withdrawal line 22 mainly contains HCl, HFO-1234yf, as well as light compounds, namely nitrogen, oxygen, carbon monoxide, carbon dioxide and other oxygenated derivatives. It may also contain HFC-245cb, resulting from the fluorination reaction, which may subsequently be recycled to the fluorination reactor, and a small amount of HF linked to the existence of azeotropes.
• the flow referred to herein as "flow of unreacted hydrogen fluoride", transported in the unreacted hydrogen fluoride withdrawal line 1, contains not only HF but also other chlorinated and / or fluorinated organic compounds, such as HCFO-1233xf and HFC-245cb, which are reaction intermediates or organic compounds derived from secondary reactions
• This stream of unreacted hydrogen fluoride is recycled to the fluorination reactor 6.
• Heating means 3 (such as exchangers and economizers) are provided on the unreacted hydrogen fluoride withdrawal line 1 in order to heat and vaporizing the stream before entering the fluorination reactor 6.
• the hydrohalocarbon feed line 4, the HF feed line 2 and / or the oxygen supply line 5 may for example be connected to the unreacted hydrogen fluoride withdrawal line 1, upstream and downstream. or downstream of the heating means 3, so that the fluorination reactor 6 is fed by a single pipe.
• the fluorination reactor 6 can be fed by the respective lines at different locations. It is also possible to provide a direct recycling line from the outlet of the fluorination reactor 6 to the inlet (or to an inlet) thereof, with appropriate means such as heating, cooling and / or compression means. .
• An energy coupling can be provided between the heating means 3 and the cooling and partial condensation means 8, so that the calories recovered during cooling and partial condensation of the gaseous flow resulting from the reaction are reused for heating and cooling. vaporization of the flow at the inlet of the fluorination reactor 6.
• the intermediate stream is separated in the second distillation column 23 in order to recover, on the one hand, the product of interest HFO-1234yf, and on the other hand the HCl with the light compounds.
• the second distillation column 23 is fed at the inlet by the intermediate flow withdrawal line 22.
• a hydrochloric acid withdrawal line 24 At the outlet of this second distillation column 23 are connected, at the head, a hydrochloric acid withdrawal line 24; and, at the bottom, a withdrawal line of 2,3,3,3-tetrafluoropropene 25.
• the HFO-1234yf flux recovered at the bottom may contain HFC-245cb, as well as a small amount of HF.
• the flow of HCI recovered overhead generally contains also the light components O2, N2, CO2 and CO (and / or other oxygenated derivatives).
• HFO-1234yf stream may be carried out if necessary, for example by washing, extracting, decanting, distilling or a combination of these operations.
• the HF and chlorinated or fluorinated organic compounds other than HFO-1234yf which are recovered during these additional steps are preferably recycled to the fluorination reactor 6 (not shown).
• FIG. 2 A second embodiment of the treatment of the flow resulting from the reaction is illustrated in FIG. 2.
• the function of the first distillation column 21 is to separate the HCI on the one hand, and the HFO-1234yf, the HF and organic compounds (chlorinated and / or fluorinated) on the other hand.
• an intermediate flow withdrawal line 27 is connected at the bottom of the first distillation column 21, and a hydrochloric acid withdrawal line 26 is connected at the top of the first distillation column 21.
• the flow of HCI recovered overhead generally contains also the light components O2, N2, CO2 and CO (and / or other oxygenated derivatives).
• the intermediate stream transported in the intermediate stream withdrawal line 27 contains mainly HFO-1234yf, HF, as well as other chlorinated and / or fluorinated organic compounds, such as HFC-245cb or HCFO-1233xf.
• the intermediate stream is separated in the second distillation column 23 in order to recover, on the one hand, the product of interest HFO-1234yf, and on the other hand the other chlorinated and / or fluorinated organic compounds.
• the second distillation column 23 is fed at the inlet by the intermediate flow withdrawal line 27.
• the stream of HFO-1234yf recovered at the top can contain HFC-245cb, as well as a small amount of HF.
• the flow of unreacted hydrogen fluoride transported in the unreacted hydrogen fluoride withdrawal line 29 contains not only HF, but also other chlorinated and / or fluorinated organic compounds, such as HCFO-1233xf and HFC-245cb, which are intermediates of the fluorination reaction or organic compounds from secondary reactions (as for the first embodiment). It is recycled to the fluorination reactor 6 in the same manner as for the first embodiment.

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