EP1034157A1 - Preparation de composes organiques contenant du fluor - Google Patents

Preparation de composes organiques contenant du fluor

Info

Publication number
EP1034157A1
EP1034157A1 EP98952937A EP98952937A EP1034157A1 EP 1034157 A1 EP1034157 A1 EP 1034157A1 EP 98952937 A EP98952937 A EP 98952937A EP 98952937 A EP98952937 A EP 98952937A EP 1034157 A1 EP1034157 A1 EP 1034157A1
Authority
EP
European Patent Office
Prior art keywords
azeotrope
hydrogen fluoride
haloalkene
mixture
fluorine
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP98952937A
Other languages
German (de)
English (en)
Inventor
Paul Nicholas Ewing
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ineos Fluor Holdings Ltd
Original Assignee
Imperial Chemical Industries Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from GBGB9724831.4A external-priority patent/GB9724831D0/en
Application filed by Imperial Chemical Industries Ltd filed Critical Imperial Chemical Industries Ltd
Publication of EP1034157A1 publication Critical patent/EP1034157A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/07—Preparation of halogenated hydrocarbons by addition of hydrogen halides
    • C07C17/087—Preparation of halogenated hydrocarbons by addition of hydrogen halides to unsaturated 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
    • 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
    • C07C17/386—Separation; Purification; Stabilisation; Use of additives by distillation with auxiliary compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C19/00—Acyclic saturated compounds containing halogen atoms
    • C07C19/08—Acyclic saturated compounds containing halogen atoms containing fluorine

Definitions

  • the present invention relates to a process for the preparation of fluorine-containing organic compounds by reacting a haloalkene with hydrogen fluoride, particularly to a process for the preparation of hydrofluorocarbons from fluoroalkenes, more particularly to a process for the preparation of 1,1,1,2,3,3,3-heptafluoropropane from hexafluoropropene, azeotropes or azeotrope-like mixtures of a hydrofluorocarbon/hydrogen fluoride, particularly azeotropes or azeotrope-like mixtures of l,lJ,2,3,3,3-heptafluoropropane riydrogen fluoride and azeotropes or azeotrope-like mixtures of a haloalkeneliydrogen fluoride, particularly azeotropes or azeotrope-like mixtures of hexafluoropropene/hydrogen fluoride.
  • Hydrofluorocarbons are widely used as replacements for chlorofluorocarbon compounds in a variety of applications. Such applications include use in medical applications, for example as an aerosol propellant, use as a fire suppressant, use in refrigeration applications and in other applications.
  • 1,1,1,2,3,3,3-heptafluoropropane which is known in the art as Hydro fluorocarbon 227ea and will hereinafter be referred to as "HFC 227ea" for convenience, has zero ozone depletion potential and is particularly beneficial in medical applications in the light of its combination of properties including low toxicity, non-flammability, solvent properties and boiling point.
  • hydrofluorocarbons by the hydro fluorination of a fluoroalkene to the corresponding hydrofluoroalkane, optionally in the presence of a catalyst, in the liquid phase or vapour phase.
  • Hydrogen fluoride is known for use as a hydrofiuorination agent in such hydrofluorination processes.
  • a variety of materials may be employed as catalysts in such hydrofluorination processes.
  • fluoroalkenes with hydrogen fluoride for the preparation of hydrofluorocarbons, eg HFC 227ea from hexafluoropropene
  • DE 2712732 and GB 902590 disclose the use of a chromium oxyfluoride catalyst and an activated carbon catalyst respectively.
  • WO 97/11042 and WO 96/0243 disclose the use of catalysts comprising an organic amine complexed with hydrogen fluoride and certain antimony catalysts respectively.
  • the product from such reactions typically comprises the desired fluorine-containing organic compound, organic by-products and hydrogen fluoride.
  • the haloalkene is hexafluoropropene, which will hereinafter be referred to as "HFP" for convenience
  • the product stream leaving the reactor in which HFP is reacted with hydrogen fluoride typically contains HFC 227ea, HFP, hydrogen fluoride and azeotropes thereof. It is normal practice to recover as much as possible of the hydrogen fluoride from the product stream from such hydrofluorination reactions for re-use. This may be partially achieved by distillation.
  • the stream comprising the hydrofluorocarbon hydrogen fluoride azeotrope, eg HFC 227ea/hydrogen fluoride azeotrope, .and the haloalkene/hydrogen fluoride azeotrope, eg HFP/hydrogen fluoride azeotrope, after recovery of a portion of the hydrogen fluoride by distillation, can be water-washed to allow recovery of both a mixture of organic compounds essentially free of hydrogen fluoride and aqueous hydrogen fluoride.
  • such a treatment is wasteful of hydrogen fluoride since it is normal practice for aqueous hydrogen fluoride generated in this way to be neutralised with caustic solution and/or lime and ultimately disposed of.
  • the product stream from the reaction of a haloalkene with hydrogen fluoride after recovery of a portion of the hydrogen fluoride by distillation, may be treated with a solution of alkali metal dissolved in anhydrous hydrogen fluoride as described in our patent specification WO 97/13179.
  • WO 97/13179 a solution of alkali metal dissolved in anhydrous hydrogen fluoride
  • aqueous scrubbing is an effective way of removing hydrogen fluoride from the organic compound(s) after reacting hydrogen fluoride with a haloalkene aqueous scrubbing tends to be expensive in terms of hydrogen fluoride loss from the process.
  • the separated haloalkene/hydrogen fluoride azeotrope can be recycled to the reaction vessel, can be used in another reaction or preferably at least a portion thereof is separated into a haloalkene-rich liquid phase and a hydrogen fluoride-rich liquid phase as is hereinafter more fully described.
  • a process for the preparation of a fluorine-containing organic compound by reacting a haloalkene with hydrogen fluoride wherein both the fluorine-containing organic compound and the haloalkene separately form azeotropes with hydrogen fluoride and wherein the haloalkene/hydrogen fluoride azeotrope is more volatile than the fluorine-containing organic compound/hydrogen fluoride azeotrope characterised by the Steps of: A.
  • Step C optionally separating at least a portion of the haloalkene./hydrogen fluoride azeotrope, or azeotrope-like mixture, recovered from Step B into a haloalkene-rich liquid phase and a hydrogen fluoride-rich liquid phase.
  • reaction of haloalkene with hydrogen fluoride mentioned in Step A of the process according to the first aspect of the present invention may be carried out in the liquid phase or in the vapour phase, optionally in the presence of a suitable catalyst.
  • Step C in the process according to the first aspect of the present invention is carried out separation is typically effected by allowing the haloalkene-rich liquid phase and the hydrogen fluoride-rich liquid phase to separate under gravity.
  • the product of the reaction of the haloalkene with hydrogen fluoride is typically distilled to recover a portion of the hydrogen fluoride therefrom before the mixture comprising fluorine-containing organic compound/hydrogen fluoride azeotrope or azeotrope-like mixture thereof, haloalkene/hydrogen fluoride azeotrope or azeotrope-like mixture thereof, and hydrogen fluoride is charged to the distillation column in Step A.
  • the portion of hydrogen fluoride recovered by distillation prior to Step A, where it is recovered, may be recycled to the reactor vessel.
  • the product of the reaction of the haloalkene with hydrogen fluoride is charged directly to the distillation column in Step A.
  • Any hydrogen fluoride which is present in excess of that required to form azeotropes in the fluorine-containing organic compound recovered from Step B may be recovered, for example by distillation.
  • the haloalkene/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof, recovered from Step B may be fed directly to the reactor in which the fluorine-containing organic compound is produced or to an appropriate process stream(s) thereto containing the haloalkene, for example a stream containing the mixture of the haloalkene and hydrogen fluoride.
  • the hydrogen fluoride-rich phase and/or the haloalkene-rich phase recovered therefrom may be fed directly to the reactor in which the fluorine-containing organic compound is produced or to an appropriate process stream(s) thereto containing the haloalkene, for example a stream containing the mixture of the haloalkene and hydrogen fluoride.
  • a process for the preparation of a fluorine-containing organic compound by reacting a haloalkene with hydrogen fluoride wherein both the fluorine-containing organic compound and the haloalkene separately form azeotropes with hydrogen fluoride and wherein the haloalkene/hydrogen fluoride azeotrope is more volatile than the fluorine-containing organic compound/hydrogen fluoride azeotrope
  • process comprises the steps of :
  • Step B optionally recovering at least a portion of hydrogen fluoride from the reaction products from Step A by distillation characterised by the further Steps of:
  • Step C charging the haloalkene and the mixture comprising the fluorine-containing organic compound/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof, the haloalkene/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof, and HF from the reactor in Step A or, where Step B is carried out, the haloalkene and the mixture comprising the fluorine-containing organic compound/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof, and the haloalkene./hydrogen fluoride .azeotrope, or azeotrope-like mixture thereof, from Step B to a distillation column;
  • Step E recovering the fluorine-containing organic compound substantially free from hydrogen fluoride from the distillation column in Step C; and F. optionally separating at least a portion of the haloalkene/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof, recovered in Step D into a haloalkene-rich phase and a hydrogen fluoride-rich phase.
  • the hydrogen fluoride-rich liquid phase can be recycled to a reaction vessel for the reaction of haloalkene with hydrogen fluoride or to a feed line thereto; and at least a portion of the haloalkene-rich liquid phase can be recycled to Step C.
  • the haloalkene/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof, recovered from the distillation column in Step D or the portion thereof not subjected to Step F, where Step F is carried out may be recycled to the reaction vessel for the reaction of haloalkene and hydrogen fluoride or to a feed-line thereto.
  • an azeotrope, or azeotrope-like mixture, of HFC 227ea and hydrogen fluoride According to a yet further aspect of the present invention there is provided an azeotrope, or azeotrope-like mixture, of HFP and hydrogen fluoride.
  • HFC 227ea is prepared by reacting HFP with hydrogen fluoride in the process according to the second aspect of the present invention and where Step A is carried out in the liquid phase in the presence of a catalyst, eg TaF 5 , NbF s or SbF 5 , it is suitably carried out at a temperature in the range 20 to 200°C, preferably 40 to 120°C and especially 50 to 100°C.
  • a catalyst eg TaF 5 , NbF s or SbF 5
  • the reaction in Step A is carried out at superatmospheric pressure such that the reactants are in the liquid phase for sufficient time to react to produce HFC 227ea.
  • the pressure is at least 5 bar and more preferably the pressure is 10 to 50 bar.
  • the residence time in the reactor in Step A in the process according to the second aspect of the present invention is sufficient to permit conversion of haloalkene feedstock into fluorine-containing organic compound.
  • the required residence time will be dependent on inter alia the degree of conversion required, the reactant ratio and the reaction conditions.
  • Haloalkene from Step F in the process according to the second aspect of the present invention is preferably recycled to the reactor in which the fluorine-containing organic compound is produced.
  • the feedstocks be recycled to increase the yield of the fluorine-containing organic compound from the starting material.
  • the molar ratio of hydrogen fluoride (HF) to haloalkene fed to the reactor is suitably at least 1 :1 and preferably 1.2 to 10: 1. If a lower conversion rate is required a molar ratio of HF to haloalkene of 0J up to 1 :1 may be employed.
  • Step A of the process according to the second aspect of the present invention the molar ratio of haloalkene to the catalyst is suitably not more than 100:1 and is preferably 1 to 50: 1.
  • the levels of HF, haloalkene and catalyst in Step A of the process according to the second aspect of the present invention are suitably selected such that the catalyst and reactants remain dissolved in the liquid phase under the reaction conditions employed.
  • the process according to the second aspect of the invention may be operated in batch or continuous mode as desired. Semi-batch operation may also be employed in which one or more feedstocks are fed continuously to the process and one or more other feedstocks are fed to the process in batch-wise fashion. Alternatively, the process according to the second aspect of the present invention may be carried out in the vapour phase. Suitable conditions and catalysts for use in carrying out the process according to the second aspect of the present invention in the vapour phase are more fully described in DE 2712732 and GB 902590 mentioned hereinbefore.
  • Step C of the process according to the second aspect of the present invention and in Step A of the process according to the first aspect of the present invention are preferably simultaneously charged to the distillation column, and more preferably the haloalkene is charged to the distillation column at a point thereon below the point at which the mixture is charged thereto.
  • the process according to the first or second aspect of the present invention is applicable to mixtures of hydrogen fluoride with any haloalkene and any fluorine-containing organic compound provided that the relative volatility of the haloalkene/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof, is higher than that of the fluorine-containing organic compound/hydrogen fluoride azeotrope, or azeotrope-like mixture thereof.
  • hydrofluorocarbons, hydrochlorofluorocarbons and hydrofluoroethers form azeotropes or azeotrope-like mixtures, or azeotrope-like mixtures, with hydrogen fluoride and the treatment of such mixtures is a preferred embodiment of the invention, especially the treatment of mixtures wherein the fluorine-containing organic compound is a hydrofluorocarbon, a hydrochlorofluorocarbon, a chlorofluorocarbon or a hydrofluoroether.
  • HFCs hydrofluorocarbons
  • HCFCs hydrochloro-fluorocarbons
  • fluorine-containing organic compounds which may be prepared by the process according to the first aspect of the present invention may be mentioned inter alia 1,1,1,2-tetrafluoroethane [HFC 134a], chloro-l,lJ-trifluoroethane [HCFC 133a], chlorotetrafluoroethane [HCFC 124/124a], pentafluoroethane [HFC 125], 1,1-difluoroethane [HFC 152a], 1,1,1-trifluoroethane [HFC 143a] and lJ,l,3,3-pentafluoropropane [HFC 245fa].
  • fluorine-containing organic compound prepared by the process according to the first aspect of the present invention is a hydrofluorocarbon, hydrochlorofluorocarbon or chlorofluorocarbon it will usually contain from 1 to 6 carbon atoms and preferably from 1 to 4 carbon atoms.
  • Figures 1, 2, 3 and 4 are schematic representations of plants for carrying out the process according to the second aspect of the present invention in which Figure 1 illustrates the use of Steps A, B, C, D and E, Figure 2 illustrates the use of Steps A, B, C, D, E and F, Figure 3 illustrates the use of Steps A, C, D and E and Figure 4 illustrates the use of Steps A, C, D, E and F;
  • Figure 5 is a schematic representations of a plant for carrying out the second embodiment of the process according to the first aspect of the present invention
  • Figure 6 is a temperature/composition plot for the HFC 227ea/HF binary
  • Figure 7 is a temperature/composition plot for the HFP/HF binary.
  • feed pipe (1) leads to a reactor (4), which optionally contains a fluorination catalyst.
  • Product pipe (5) from the reactor (4) is in fluid-flow communication with a first distillation column (6), which is for example a single stage flash vessel.
  • Distillation column (6) is typically operated at a pressure of 12 bars with a bottoms temperature of 70°C and a tops temperature of around 50°C.
  • Bottoms pipe (2) from distillation column (6) is in fluid-flow communication with feed-pipe (1).
  • Tops line (7) from distillation column (6) is in fluid-flow communication with a second distillation column (8), which is for example a packed column.
  • Distillation column (8) is typically operated at a pressure of around 12 bars with a tops temperature of 37°C and a bottoms temperature of around 60°C.
  • Distillation column (8) is provided with a feed line (9) below the point at which tops line (7) is attached to it, a bottoms pipe (10) and a tops pipe (3) which is in fluid-flow communication with feed-pipe (1).
  • tops pipe (3) from distillation column (8) is provided with a line (11) which is in fluid flow communication with phase separator (12).
  • Phase separator (12) is provided with a line (13) in fluid-flow communication with feed line (9) and a line (14) in fluid-flow communication with tops line (3).
  • the reactor (4) is charged through feed pipe (1) with a feed stream containing fresh hydrogen fluoride, recycled hydrogen fluoride (from bottoms line (2) and tops line (3)) and HFP/hydrogen fluoride azeotrope (from tops line (3)).
  • the product from reactor (4) (HFC 227ea, hydrogen fluoride and optionally unconverted HFP) travels through product pipe (5) to the first distillation column (6).
  • distillation column (6) hydrogen fluoride, which is recycled via bottoms line (2) to feed pipe (1), is separated from the mixture of HFC 227ea, hydrogen fluoride and unconverted HFP.
  • the mixture of HFC 227ea, residual hydrogen fluoride and HFP is fed via tops line (7) from the distillation column (6) to the second distillation column (8).
  • HFP is fed via feed line (9) to column (8).
  • a stream comprising HFP and essentially all the hydrogen fluoride content of the stream entering distillation column (8) via line (7) is removed from the top of distillation column (8) via line (3) and the product stream H .
  • FC 227ea is removed from the bottom of column (8) via bottoms lead (10).
  • a portion of the stream in pipe (3) is diverted in the liquid phase through pipe (11) to separator (12) in which a HFP-rich phase is separated from an hydrogen fluoride-rich phase.
  • the HFP-rich liquid phase is fed via line (13) to feed line (9) to distillation column (8).
  • the hydrogen fluoride-rich liquid phase from separator (12) is returned via line (14) to tops pipe (3) to feed line (1).
  • feed pipe (21) leads to a reactor (22), which optionally contains a fluorination catalyst.
  • Product pipe (23) from the reactor (22) is in fluid-flow communication with a distillation column (24), which is for example a packed column.
  • Distillation column (24) is typically operated at a pressure of around 12 bars with a tops temperature of 37°C and a bottoms temperature of around 60°C.
  • Distillation column (24) is provided with a bottoms pipe (25), a tops pipe (26), which is in fluid-flow communication with feed-pipe (21), and feed line (27) below the point at which product pipe (23) is attached to it.
  • tops pipe (26) from distillation column (24) is provided with a line
  • Phase separator (28) which is in fluid flow communication with phase separator (29).
  • Phase separator (28) which is in fluid flow communication with phase separator (29).
  • the reactor (22) is charged through feed pipe (21) with a feed stream containing hydrogen fluoride (fresh and recycled through a hydrogen fluoride-rich stream (from line (26)) and recycled HFP.
  • the product from separator (29) (HFC 227ea, hydrogen fluoride and optionally unconverted .HFP) travels through product pipe (23) to distillation column (24).
  • HFP is fed via feed line (27) to column (24).
  • a stream comprising HFP and essentially all the hydrogen fluoride content of the stream entering distillation column (24) via line (23) is removed from the top of distillation column (24) via line (26) and the product stream HFC 227ea is removed from the bottom of column (24) via bottoms lead (25).
  • a portion of the stream in pipe (26) is diverted in the liquid phase through pipe (28) to separator (29) in which a HFP-rich phase is separated from a hydrogen fluoride-rich phase.
  • the HFP-rich phase from column (24) is fed via line (31) to feed line (27) to distillation column (24).
  • the hydrogen fluoride-rich phase from separator (29) is returned via lines (30) and (26) to feed line (21).
  • distillation column (32) is provided with feed line (31) connected to a reactor (not shown), feed line (33), bottom line (34) and top line (35).
  • a mixture comprising HFC 227ea/HF azeotrope, or azeotrope-like mixture, HFP/HF azeotrope, or azeotrope-like mixture and/or HF is fed via line (31) to distillation column (32 ) and a stream comprising HFP is fed via line (33) to distillation column (32).
  • HFP/HF azeotrope, or azeotrope-like mixture is removed from distillation column (32) via top line (35) and HFC 227ea substantially free from HF is removed from distillation column (32) via bottom line (34).
  • the Example reveals that both HFP and HFC 227ea form azeotropes with .HF and, at constant pressure the boiling point of the HFP/HF azeotrope is lower than the boiling point of the HFC 227ea/HF azeotrope.
  • a temperature/composition plot for the HFC 227ea/HF binary is illustrated in Figure 6 wherein the dashed line — represents the vapour phase composition and the solid line represents the liquid phase composition. From Figure 6 it can be seen that at 174psi the HFC 227ea/HF azeotrope has a boiling point of 123°F and a composition of 42mole% HF and 58mole% HFC 227ea.
  • FIG. 7 A temperature/composition plot for the HFP/HF binaiy is illustrated in Figure 7 wherein the dashed line — represents the vapour phase composition and the solid line represents the liquid phase composition. From Figure 7 it can be seen that at 174psi the HFP/HF azeotrope has a boiling point of 98°F and a composition of 38mole% HF and 62mole% HFP.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne une préparation d'un composé organique contenant du fluor, consistant à faire réagir un haloalcène avec du fluorure d'hydrogène, dans laquelle à la fois le composé organique contenant du fluor et l'haloalcène forment séparément des azéotropes avec du fluorure d'hydrogène, et dans laquelle l'azéotrope haloalcène/fluorure d'hydrogène est plus volatile que l'azéotrope composé organique contenant du fluor/fluorure d'hydrogène.
EP98952937A 1997-11-25 1998-11-12 Preparation de composes organiques contenant du fluor Withdrawn EP1034157A1 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US6683697P 1997-11-25 1997-11-25
GBGB9724831.4A GB9724831D0 (en) 1997-11-25 1997-11-25 Preparation of fluorine-containing organic compounds
GB9724831 1997-11-25
US66836P 1997-11-25
PCT/GB1998/003408 WO1999026907A1 (fr) 1997-11-25 1998-11-12 Preparation de composes organiques contenant du fluor

Publications (1)

Publication Number Publication Date
EP1034157A1 true EP1034157A1 (fr) 2000-09-13

Family

ID=26312652

Family Applications (1)

Application Number Title Priority Date Filing Date
EP98952937A Withdrawn EP1034157A1 (fr) 1997-11-25 1998-11-12 Preparation de composes organiques contenant du fluor

Country Status (7)

Country Link
EP (1) EP1034157A1 (fr)
JP (1) JP2001524460A (fr)
CN (1) CN1284053A (fr)
AR (1) AR016699A1 (fr)
AU (1) AU747117B2 (fr)
CA (1) CA2309694A1 (fr)
WO (1) WO1999026907A1 (fr)

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Publication number Priority date Publication date Assignee Title
CA2373437A1 (fr) * 1999-05-18 2000-11-23 Ineos Fluor Holdings Limited Production de 1,1,1,2,3,3,3-heptafluoropropane
EP1291337A1 (fr) * 2001-09-07 2003-03-12 SOLVAY (Société Anonyme) Procédé pour l'obtention d'heptafluoropropane purifié
US7329786B2 (en) 2001-09-28 2008-02-12 Great Lakes Chemical Corporation Processes for producing CF3CFHCF3
CN1310858C (zh) 2001-10-31 2007-04-18 纳幕尔杜邦公司 由氟化氢和六氟丙烯生产1,1,1,2,3,3,3－七氟丙烷的气相方法
US8058486B2 (en) * 2004-04-29 2011-11-15 Honeywell International Inc. Integrated process to produce 2,3,3,3-tetrafluoropropene
US7476771B2 (en) * 2005-11-01 2009-01-13 E.I. Du Pont De Nemours + Company Azeotrope compositions comprising 2,3,3,3-tetrafluoropropene and hydrogen fluoride and uses thereof
US7385094B2 (en) 2005-11-01 2008-06-10 E.I. Du Pont De Nemours And Company Azeotrope compositions comprising tridecafluoro-3-heptene and hydrogen fluoride and uses thereof
US7709438B2 (en) * 2005-11-01 2010-05-04 E. I. Du Pont De Nemours And Company Azeotrope compositions comprising nonafluoropentene and hydrogen fluoride and uses thereof
EP2433921B1 (fr) * 2006-08-24 2014-01-15 E. I. du Pont de Nemours and Company Procédés de séparation des fluoroléfines de fluorure d'hydrogène par distillation azéotropique
EP2247560B1 (fr) 2008-02-21 2014-06-04 E. I. du Pont de Nemours and Company Procédés de séparation de 1,3,3,3-tétrafluoropropène de fluorure d'hydrogène par distillation azéotropique
US8008243B2 (en) * 2008-10-31 2011-08-30 Honeywell International Inc. Azeotrope-like compositions of 1,1,2,3-tetrachloropropene and hydrogen fluoride
HUE058177T2 (hu) * 2014-04-29 2022-07-28 Arkema Inc R-1233 elválasztása hidrogén-fluoridtól
JP7310807B2 (ja) * 2018-05-30 2023-07-19 Ａｇｃ株式会社 （ｚ）－１－クロロ－２，３，３，４，４，５，５－ヘプタフルオロ－１－ペンテンの製造方法

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DE4115025A1 (de) * 1991-05-08 1992-11-12 Hoechst Ag Verfahren zur entfernung olefinischer verunreinigungen aus 1,1,1,2,3,3,3-heptafluorpropan
GB9307923D0 (en) * 1993-04-16 1993-06-02 Ici Plc Process for the purification of 1-chloro-2,2,2-trifluroethane
US5563304A (en) * 1994-05-26 1996-10-08 E. I. Du Pont De Nemours And Company Production of 1,2-dihydro and 2,2-dihydro hexafluoropropanes and azeotropes thereof with HF

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Publication number Publication date
CA2309694A1 (fr) 1999-06-03
WO1999026907A1 (fr) 1999-06-03
AU1047799A (en) 1999-06-15
CN1284053A (zh) 2001-02-14
AU747117B2 (en) 2002-05-09
AR016699A1 (es) 2001-07-25
JP2001524460A (ja) 2001-12-04

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