• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention relates to a process for producing 2,3,3,3-tetrafluoropropene comprising the steps of: a) providing a stream A comprising at least one of the compounds selected from the group consisting of 2-chloro-3,3 3-trifluoropropene and 2,3-dichloro-1,1,1-trifluoropropane; b) in a reactor, contacting said stream A with HF in the presence or absence of a fluorination catalyst to produce a stream B comprising 2,3,3,3-tetrafluoropropene; characterized in that the electrical conductivity of said stream A supplied in step a) is less than 15 mS / cm.
    公开号:FR3078699A1
    申请号:FR1851956
    申请日:2018-03-07
    公开日:2019-09-13
    发明作者:Laurent Wendlinger；Dominique Deur-Bert；Anne Pigamo
    申请人:Arkema France SA；
    IPC主号:
    专利说明:

    Process for the production of 2,3,3,3-tetrafluoropropene
    Technical field of the invention
    The present invention relates to the production of hydrofluoroolefins. More particularly, the present invention relates to the production of 2,3,3,3-tetrafluoropropene.
    Technological background of the invention
    Halogenated hydrocarbons, in particular 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) attract attention because they offer promising behavior as refrigerants with low global warming potential.
    The processes for producing fluoroolefins are usually carried out in the presence of a starting material such as an alkane containing chlorine or an alkene containing chlorine, 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, with or without the catalyst.
    We know for example from US 2009/0240090, a gas phase process for the preparation of 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf) from 1,1,1,2,3pentachloropropane (HCC-240db ). The HCFO-1233xf thus produced is converted into 2-chloro-
    1.1.1.2- tetrafluoropropane (HCFC-244bb) in the liquid phase then the latter is converted into
    2.3.3.3- tetrafluoropropene.
    Also known from WO 2011/077192, a process for preparing 2,3,3,3tetrafluoropropene comprising in particular a step of bringing 2-chloro-3,3,3trifluoropropene into contact with HF in the gas phase in the presence of a catalyst of fluoridation.
    There is always a need for more efficient processes for producing 2,3,3,3-tetrafluoropropene.
    Summary of the invention
    The present invention relates to a process for the production of 2,3,3,3tetrafluoropropene comprising the steps:
    a) supply of a stream A comprising at least one starting compound selected from the group consisting of 2-chloro-3,3,3-trifluoropropene and 2,3-dichloro-1,1,1-trifluoropropane,
    b) in a reactor, bringing said stream A into contact with HF in the presence or absence of a catalyst to produce a stream B comprising 2,3,3,3-tetrafluoropropene, characterized in that the electrical conductivity of said stream A supplied to step a) is less than 15 mS / cm.
    The present process makes it possible to optimize and improve the production of 2,3,3,3tetrafluoropropene. An electrical conductivity value of less than 15 mS / cm of the current A before the implementation of the fluorination and / or dehydrofluorination step makes it possible to guarantee optimum efficiency of the reaction in terms of conversion and selectivity. If a catalyst is present, such a value also ensures optimum efficiency of the catalyst.
    According to a preferred embodiment, step b) is carried out in the gas phase in the presence of a catalyst.
    According to a preferred embodiment, the electrical conductivity of said current A is less than 10 mS / cm.
    According to a preferred embodiment, step b) is carried out in the presence of a chromium-based catalyst, in particular said catalyst comprises a chromium oxyfluoride or a chromium oxide or a chromium fluoride or a mixture of them.
    According to a preferred embodiment, the catalyst is based on chromium and also comprises a cocatalyst selected from the group consisting of Ni, Zn, Co, Mn or Mg, preferably the cocatalyst content is between 0, 01% and 10% based on the total weight of the catalyst.
    According to a preferred embodiment, the stream A comprises 2-chloro-3,3,3trifluoropropene, HF and optionally 1,1,1,2,2-pentafluoropropane.
    According to a preferred embodiment, stream B comprises, in addition to 2,3,3,3tetrafluoropropene, HF, HCl, unreacted 2-chloro-3,3,3-trifluoropropene and optionally 1,1,1,2 2-pentafluoropropane.
    According to a preferred embodiment, step b) is carried out at a temperature between 310 ° C and 420 ° C.
    According to a preferred embodiment, step b) is carried out in the presence of hydrofluoric acid having an electrical conductivity of less than 10 mS / cm.
    Detailed description of the present invention
    The present invention relates to a process for the production of 2,3,3,3tetrafluoropropene comprising the steps:
    a) supply of a stream A comprising at least one of the compounds selected from the group consisting of 2-chloro-3,3,3-trifluoropropene and 2,3-dichloro-1,1,1-trifluoropropane,
    b) in a reactor, bringing said stream A into contact with HF in the presence or absence of a catalyst to produce a stream B comprising 2,3,3,3-tetrafluoropropene.
    According to a preferred embodiment, the electrical conductivity of said current A supplied in step a) is less than 15 mS / cm. Advantageously, the electrical conductivity of said current A supplied in step a) is less than 14 mS / cm, preferably less than 13 mS / cm, more preferably less than 12 mS / cm, in particular less than 11 mS / cm, more particularly less than 10 mS / cm, preferably less than 9 mS / cm, advantageously less than 8 mS / cm, preferably less than 7 mS / cm, more preferably less than 6 mS / cm, particularly preferably less than 5 mS / cm. The electrical conductivity is measured using an inductive conductivity measuring cell and according to the practice known to those skilled in the art. Preferably, the measuring cell is coated with a material resistant to a corrosive medium, in particular resistant to hydrofluoric acid.
    The electrical conductivity of said current A is measured before step b). Preferably, the electrical conductivity of said current A is measured when the latter is in liquid form. Said method according to the present invention may therefore comprise a step of heating and vaporizing said stream A prior to the implementation of step b) to supply said stream A in gaseous form. Preferably, said current A used in step b) is in gaseous form when it is brought into contact with HF.
    According to a preferred embodiment, step b) is carried out in the presence of a catalyst, preferably a catalyst based on chromium. Preferably, the chromium-based catalyst can be a chromium oxide (for example CrCh, CrC> 3 or C ^ Ch), a chromium oxyfluoride or a chromium fluoride (for example OF3) or a mixture of these . 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 between 35 and 45% by weight of fluorine based on the total weight of chromium oxyfluoride. The catalyst can also comprise a co-catalyst chosen 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 catalyst. The catalyst can be supported or not. A support such as alumina, activated alumina, aluminum halides (AIF3 for example), aluminum oxyhalides, activated carbon, magnesium fluoride or graphite can be used.
    Preferably, the catalyst can have a specific surface 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.
    According to a preferred embodiment, the pressure at which step b) is implemented is atmospheric pressure or a pressure greater than this, advantageously the pressure at which step b) is implemented is greater than 1.5 bara, preferably greater than 2.0 bara, in particular greater than 2.5 bara, more particularly greater than 3.0 bara. Preferably, step b) is implemented at a pressure between atmospheric pressure and 20 bara, preferably between 2 and 18 bara, more preferably between 3 and 15 bara.
    Preferably, step b) of the present method is implemented with a contact time between 1 and 100 s, preferably between 2 and 75 s, in particular between 3 and 50 s. Preferably, the HF molar ratio and said at least one of the compounds of said stream A, ie 2-chloro-3,3,3-trifluoropropene or 2,3-dichloro-1,1,1-trifluoropropane, can vary between 1: 1 and 150: 1, preferably between 2: 1 and 125: 1, more preferably between 3: 1 and 100: 1. An oxidant, such as oxygen or chlorine, can be added during step b). The molar ratio of the oxidant to the hydrocarbon compound can be between 0.005 and 2, preferably between 0.01 and 1.5. The oxidant can be pure oxygen, air or a mixture of oxygen and nitrogen.
    According to a preferred embodiment, step b) is carried out at a temperature between 310 ° C and 420 ° C, advantageously between 310 ° C and 400 ° C, preferably between 310 ° C and 375 ° C, more preferably between 310 ° C and 360 ° C, in particular between 330 ° C and 360 ° C.
    According to a preferred embodiment, stream A comprises 2-chloro-3,3,3trifluoropropene or 2,3-dichloro-1,1,1,-trifluoropropane, HF and optionally 1,1,1,2,2pentafluoropropane.
    According to a preferred embodiment, stream B comprises, in addition to 2,3,3,3tetrafluoropropene, HF, HCl, 2-chloro-3,3,3-trifluoropropene or 2,3-dichloro-l, l, ltrifluoropropane n ' unreacted and optionally 1,1,1,2,2-pentafluoropropane.
    According to a preferred embodiment, stream B is purified, preferably by distillation, to form a first stream comprising 2,3,3,3-tetrafluoropropene, HCl and optionally 1,1,1,2,2-pentafluoropropane, and a second stream comprising HF and 2-chloro-3,3,3-trifluoropropene or 2,3-dichloro-1,1,1-trifluoropropane.
    Preferably, said stream B is distilled under conditions sufficient to form said first stream comprising 2,3,3,3-tetrafluoropropene, HCl and 1,1,1,2,2pentafluoropropane, and said second stream comprising HF and 2-chloro -3,3,3-trifluoropropene. In particular, the distillation can be carried out at a pressure of 2 to 6 bara, more particularly at a pressure of 3 to 5 bara. In particular, the temperature at the top of the distillation column is from -35 ° C to 10 ° C, preferably from -20 ° C to 0 ° C.
    According to a preferred embodiment, said stream B obtained in step b) is cooled before the purification mentioned above. In particular, said stream B obtained in step b) is cooled to a temperature below 100 ° C., then distilled to form said first stream comprising 2,3,3,3-tetrafluoropropene, HCl and 1,1,1, 2,2-pentafluoropropane, and said second stream comprising HF and 2-chloro-3,3,3-trifluoropropene or 2,3-dichloro-1,1,1 ltrifluoropropane; the temperature at the top of the distillation column is from -35 ° C to 10 ° C and the distillation is carried out at a pressure of 2 to 6 bara.
    Said stream B can be cooled, before distillation, to a temperature below 95 ° C, advantageously below 90 ° C, preferably below 85 ° C, more preferably below 80 ° C, in particular below 70 ° C, more particularly less than 60 ° C, preferably less than 55 ° C, advantageously less than 50 ° C, preferably less than 40 ° C, more preferably less than 30 ° C, so particularly preferred less than 25 ° C, more particularly preferred less than 20 ° C. Cooling the product stream obtained to such temperatures can facilitate subsequent distillation.
    The cooling of said stream B can be carried out by means of one or a plurality of heat exchangers. The cooling of said stream B can be carried out by passing it through one, two, three, four, five, six, seven, eight, nine or ten heat exchangers, preferably the number of heat exchangers is between 2 and 8, in particular between 3 and 7.
    According to a preferred embodiment, step b) is carried out in the presence of hydrofluoric acid having an electrical conductivity of less than 10 mS / cm, preferably less than 5 mS / cm. The electrical conductivity of hydrofluoric acid can be measured prior to its use in step b) of the present process. Preferably, the electrical conductivity of hydrofluoric acid is measured before step b) and the hydrofluoric acid is in liquid form during the measurement. The method can also include a step of heating and vaporizing hydrofluoric acid prior to the implementation of step b) to provide hydrofluoric acid in gaseous form. Preferably, the hydrofluoric acid is in gaseous form when it is brought into contact with said stream A.
    Preferably, the method according to the present invention is implemented continuously.
    Example
    The fluorination of HCFO-1233xf (2-chloro-3,3,3-trifluoropropene) into HFO-1234yf (2,3,3,3tetrafluoropropene) and optionally into HFC-245cb (1,1,1,2,2-pentafluoropropane ) is carried out in a multitubular reactor. The reactor contains a mass catalyst based on chromium oxide. The catalyst is activated by a series of stages including drying, fluorination, treatment in air and fluorination with recycling. This treatment in several stages makes the catalytic solid active and selective.
    The fluorination process is carried out according to the following operating conditions:
    An absolute pressure in the fluorination reactor of 5.8 bar absolute
    A molar ratio between HF and the sum of the organics supplied by the recycling loop of between 15 and 20
    Contact time 16 seconds
    A constant temperature in the reactor of 350 ° C.
    The process is carried out with a current of HCFO-1233xf having three different electrical conductivity values: 6, 10 and 35 mS / cm. The run is stopped when the conversion to 2-chloro-3,3,3-trifluoropropene is less than 50%. Table 1 below shows the values obtained.
    The electrical conductivity of the HCFO-1233xf current is measured using a cell sold by Endress + Hauser and referenced under the term InduMax P CLS 50 coated with a perfluoroalkoxy (PFA) type polymer coating resistant to a corrosive medium. containing HF.
    Table 1
    Example Electrical conductivity (mS / cm) Duration of the run to reach a conversion <50% (h) 1 (inv.) 6 400 2 (inv.) 10 240 3 (comp.) 35 40
    The results detailed in Table 1 demonstrate that a current comprising HCFO1233xf and having an electrical conductivity of less than 15 mS / cm makes it possible to maintain a sufficiently high conversion for a long period of time. In fact, a conversion greater than 50% can be maintained for more than 240 h (example 2) and even up to 400 h when the electrical conductivity is 6 mS / cm (example 1). On the contrary, the conversion to HCFO-1233xf drops sharply when the electrical conductivity is too high (example 3).
    权利要求:
    Claims (9)
    [1" id="c-fr-0001]
    1. Process for the production of 2,3,3,3-tetrafluoropropene comprising the steps of:
    a) supply of a stream A comprising at least one starting compound selected from the group consisting of 2-chloro-3,3,3-trifluoropropene and 2,3-dichloro-1,1,1 trifluoropropane;
    b) in a reactor, bringing said stream A into contact with HF in the presence or absence of a catalyst to produce a stream B comprising 2,3,3,3-tetrafluoropropene;
    characterized in that the electrical conductivity of said current A supplied in step a) is less than 15 mS / cm.
    [2" id="c-fr-0002]
    2. Method according to claim 1 characterized in that step b) is implemented in the gas phase in the presence of a catalyst.
    [3" id="c-fr-0003]
    3. Method according to any one of the preceding claims, characterized in that the electrical conductivity of said current A is less than 10 mS / cm.
    [4" id="c-fr-0004]
    4. Method according to any one of the preceding claims, characterized in that step b) is carried out in the presence of a chromium-based catalyst, in particular said catalyst comprises a chromium oxyfluoride or a chromium oxide or a chromium fluoride or a mixture thereof.
    [5" id="c-fr-0005]
    5. Method according to the preceding claim characterized in that the catalyst is based on chromium and also comprises a co-catalyst selected from the group consisting of Ni, Zn, Co, Mn or Mg, preferably the content of co-catalyst is between 0.01% and 10% based on the total weight of the catalyst.
    [6" id="c-fr-0006]
    6. Method according to any one of the preceding claims, characterized in that the stream A comprises 2-chloro-3,3,3-trifluoropropene, HF and 1,1,1,2,2-pentafluoropropane.
    [7" id="c-fr-0007]
    7. Method according to the preceding claim, characterized in that the stream B comprises, in addition to 2,3,3,3-tetrafluoropropene, HF, HCl, 2-chloro-3,3,3-trifluoropropene which has not reacted and 1, 1,1,2,2-pentafluoropropane.
    [8" id="c-fr-0008]
    8. Method according to any one of the preceding claims, characterized in that step b) is carried out at a temperature between 310 ° C and 420 ° C.
    5
    [0009]
    9. Method according to any one of the preceding claims, characterized in that the step
    b) is carried out in the presence of hydrofluoric acid having an electrical conductivity of less than 10 mS / cm.
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    法律状态:
    2019-02-13| PLFP| Fee payment|Year of fee payment: 2 |
    2019-09-13| PLSC| Publication of the preliminary search report|Effective date: 20190913 |
    2020-02-14| PLFP| Fee payment|Year of fee payment: 3 |
    2021-02-10| PLFP| Fee payment|Year of fee payment: 4 |
    2022-02-09| PLFP| Fee payment|Year of fee payment: 5 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1851956|2018-03-07|
    FR1851956A|FR3078699B1|2018-03-07|2018-03-07|PROCESS FOR PRODUCING 2,3,3,3-TETRAFLUOROPROPENE|FR1851956A| FR3078699B1|2018-03-07|2018-03-07|PROCESS FOR PRODUCING 2,3,3,3-TETRAFLUOROPROPENE|
    PCT/FR2019/050477| WO2019170989A1|2018-03-07|2019-03-04|Process for the production of 2,3,3,3-tetrafluoropropene|
    US16/976,819| US11034635B2|2018-03-07|2019-03-04|Process for the production of 2,3,3,3-tetrafluoropropene|
    CN201980013476.XA| CN111712479A|2018-03-07|2019-03-04|Production process of 2,3,3, 3-tetrafluoropropene|
    EP19715969.2A| EP3762353A1|2018-03-07|2019-03-04|Process for the production of 2,3,3,3-tetrafluoropropene|
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