WO2007147988A1 - Procede de fabrication du pentafluoroethane - Google Patents
Procede de fabrication du pentafluoroethane Download PDFInfo
- Publication number
- WO2007147988A1 WO2007147988A1 PCT/FR2007/051304 FR2007051304W WO2007147988A1 WO 2007147988 A1 WO2007147988 A1 WO 2007147988A1 FR 2007051304 W FR2007051304 W FR 2007051304W WO 2007147988 A1 WO2007147988 A1 WO 2007147988A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- fraction
- catalyst
- hydrofluoric acid
- products
- perchlorethylene
- Prior art date
Links
Classifications
-
- 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
-
- 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
- C07C17/093—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
- C07C17/21—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms with simultaneous increase of the number of halogen atoms
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/582—Recycling of unreacted starting or intermediate materials
Definitions
- the present invention relates to a process for producing pentafluoroethane. More particularly, it relates to a continuous process for producing pentafluoroethane by fluorination of perchlorethylene (PER) in the gas phase in the presence of a catalyst.
- PER perchlorethylene
- One of the critical points of a gas phase fluorination process is the stability of the catalyst.
- the document EP 609123 describes a continuous process for the catalytic fluorination of perchlorethylene in the gas phase by means of hydrofluoric acid in the presence of a mixed catalyst composed of oxides, halides and / or oxyhalides of nickel and chromium deposited on a support consisting of of aluminum fluoride or a mixture of aluminum fluoride and alumina.
- Example 2 of this document The stability of the catalyst is demonstrated in Example 2 of this document with a temperature of 350 ° C., at atmospheric pressure, a HF / PER molar ratio close to 7 and a contact time of 15 seconds.
- a mixture of compounds is formed, predominantly with the compounds of the "F 120 series", namely F 121 (CHCl 2 -CCI 2 F), F 122 (CHCl 2 -CCIF 2 ), F 123 (CHCl 2 -CF 3 ), F 124 (CHFCl-CF 3 ), F 125 (CHF 2 -CF 3 ) or isomers thereof.
- the subject of the present invention is therefore a process for the manufacture of pentafluoroethane comprising (i) a step in the course of which perchlorethylene reacts with hydrofluoric acid in the gaseous phase in the presence of a catalyst, and (ii) a separation step products from the reaction stage to give a fraction (A) of light products comprising hydrochloric acid, pentafluoroethane and a fraction (B) of heavy products characterized in that the fraction (B) comprising acid unreacted hydrofluoric acid, unreacted perchlorethylene and at least one compound selected from trichlorodifluoroethane and olefinic compounds, such as F111 1 and F1 1 12a, is subjected to a catalytic pre-treatment with a molar ratio HF / organic included between 30 and 150, preferably between 60 and 130 and at a temperature between 280 and 400 ° C, preferably between 340 and 370 ° C before being recycled to the reaction step n
- the pressure is not critical for the catalytic pretreatment, it is preferred however to operate at a pressure close to that of the reaction step (i) and advantageously at a pressure greater than that of the reaction step (i). .
- the dichlorotrifluoroethane and / or chlorotetrafluoroethane formed in the reaction step may be present either in the fraction (A) or in the fraction (B) .
- Fraction (A) may also comprise hydrofluoric acid, which is azeotroped with fluorinated carbon compounds such as pentafluoroethane, dichlorotrifluoroethane and chlorotetrafluoroethane.
- the fraction (B) can be decanted to give a phase comprising essentially hydrofluoric acid and a phase comprising organic compounds. Both phases are then sent to the pre-processing step.
- the catalyst of the pre-treatment step is a fluorination catalyst.
- the catalyst of the pretreatment stage is of the same nature as that involved in the reaction step
- the HF / organic molar ratio in the reaction step (i) is preferably between 5 and 60, advantageously between 7 and 30.
- the temperature may be between 300 and 400 ° C., preferably between 330 and 370 ° C.
- the process according to the present invention is particularly suitable when the reaction stage is carried out at a pressure of between 1 and 15 bar absolute, preferably between 2 and 10 bar absolute and preferably between 5 and 9 bar absolute.
- the fraction (A) comprises dichlorotrifluoroethane and / or chlorotetrafluoroethane
- it can be subjected, after separation of the hydrochloric acid and optionally pentafluoroethane to a fluorination step during which dichlorotrifluoroethane and / or chlorotetrafluoroethane reacted (ssen). ) with hydrofluoric acid in the gas phase, in the presence of a catalyst, to give pentafluoroethane.
- Unreacted dichlorotrifluoroethane and / or chlorotetrafluoroethane and hydrofluoric acid can then be recycled.
- the HF / organic molar ratio of the fluorination step of the fraction (A) is preferably between 1 and 20 and advantageously between 2 and 10.
- This fluorination step is preferably carried out at a temperature of pressure close to the reaction step (i).
- the temperature is preferably between 300 and 400 ° C and advantageously between 330 and 370 ° C.
- Any fluorination catalyst may be suitable for the process of the present invention.
- the catalyst used preferably comprises oxides, halides, oxyhalides or inorganic salts of chromium, aluminum, cobalt, manganese, nickel, iron or zinc, and can be supported. It is preferable to use a chromium oxide (Cr 2 Os) catalyst optionally including another metal of oxidation state greater than zero and selected from Ni, Co, Mn and Zn.
- this catalyst can be supported on alumina, aluminum fluoride or aluminum oxyfluoride.
- mixed catalysts composed of oxides, halides and / or oxyhalides of nickel and chromium deposited on a support consisting of aluminum fluoride or a mixture of aluminum fluoride and aluminum fluoride. alumina as described for example in the US Pat.
- catalysts containing, by mass, from 0.5 to 20% of chromium and from 0.5 to 20% of nickel and more particularly those containing from 2 to 10% by weight, will be recommended. in mass of each of the metals in a nickel / chromium atomic ratio of between 0.1 and 5, preferably close to 1.
- oxygen may be wise to introduce low-grade oxygen with the reagents. This content may vary depending on the operating conditions between 0.02 and 2 mol% relative to the reactants entering the reactor.
- the introduction of oxygen can be continuous or sequential.
- Oxygen can also be introduced into the pretreatment stage.
- the method according to the present invention can be implemented both continuously and discontinuously, but it is preferred to operate continuously.
- the pre-treatment reactor (101) contains a catalyst and is fed with a recycled stream (11) comprising hydrofluoric acid, unreacted perchlorethylene and at least one compound chosen from trichlorodifluoroethane and olefinic compounds such as
- the reactor (101) is supplied with hydrofluoric acid also via the inlet (106).
- the reactor (102) containing a fluorination catalyst, is supplied with perchlorethylene by the inlet (107) and optionally by the stream from the reactor (101), into hydrofluoric acid by the flow leaving the reactor (101).
- reaction products (108) are then subjected to a separation series represented by (103) to give a heavy product fraction which is recycled (11 1), a fraction of light products which, after separation of HCl (109) and possibly F125 as a HF azeotrope / F125, supplies dichlorotrifluoroethane and / or chlorotetrafluoroethane (1 10) to the fluorination reactor (104) containing a catalyst.
- This reactor (104) is supplied with hydrofluoric acid by the inlet (1 15).
- the stream (110) may also contain hydrofluoric acid.
- the products of the reaction are then subjected to a separation step (105) to give a fraction of light products (1 13) comprising hydrochloric acid, pentafluoroethane and optionally hydrofluoric acid in the form of an azeotrope with the pentafluoroethane and a heavy product fraction (1 14) essentially comprising unreacted hydrofluoric acid, dichlorotrifluoroethane and / or chlorotetrafluoroethane (s) which is recycled to the reactor (104).
- a common separation device may be used for the products from the reactors (102) and (104). In this case, the products of the reaction (1 12) are returned to (103) instead of (105).
- the examples were carried out using a fluorination pilot, consisting of a fluorination reactor (102), a distillation column and optionally a pre-treatment reactor (101).
- the reactants, in the gaseous phase are fed continuously (perchlorethylene and hydrofluoric acid) into an Inconel fluorination reactor (102) containing 200 ml of catalyst.
- a distillation column makes it possible to separate the products of the reaction, such as F123, F124, F125, HCl, HF (entrained as an azeotrope with organic compounds) on the one hand, unprocessed reagents and subfluorinated products (PER, excess HF, F122, F1 1 1 1) on the other hand.
- the two phases are recycled separately to the reactor.
- the level of the organic phase is maintained constant by racking.
- the recycled stream (consisting of the two phases after decantation) is subjected to a pre-treatment in the presence of 56 ml of catalyst contained in an Inconel reactor (101).
- all of the hydrofluoric acid required for the various stages arrives in the reactor (101) and most of the perchlorethylene is introduced into the reactor (102).
- Air is introduced into the reactors (101) and (102) in an amount such that it corresponds to the molar ratio indicated below.
- compositions of the recycled HF and organic phases have stabilized at compositions close to:
- Per-pass conversion of PER percentage ratio between the PER consumed and the entering PER at the PER fluoridation reactor - The production of F123 + F124 + F125 in mmol / h.
- Example without pre-treatment The operating conditions in the PER fluorination reactor are as follows:
- the operating conditions of the pre-treatment are as follows:
- the operating conditions in the PER fluorination reactor are as follows:
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
MX2008015809A MX2008015809A (es) | 2006-06-21 | 2007-05-21 | Proceso para la produccion de pentafluoroetano. |
EP07766078A EP2029506A1 (fr) | 2006-06-21 | 2007-05-21 | Procede de fabrication du pentafluoroethane |
CN2007800208968A CN101460436B (zh) | 2006-06-21 | 2007-05-21 | 制造五氟乙烷的方法 |
US12/305,857 US8110713B2 (en) | 2006-06-21 | 2007-05-21 | Process for producing pentafluoroethane |
KR1020087030340A KR101395585B1 (ko) | 2006-06-21 | 2007-05-21 | 펜타플루오로에탄 제조 방법 |
JP2009515922A JP2009541278A (ja) | 2006-06-21 | 2007-05-21 | ペンタフルオロエタンの製造方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0605525 | 2006-06-21 | ||
FR0605525A FR2902788B1 (fr) | 2006-06-21 | 2006-06-21 | Procede de fabrication du pentafluoroethane |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2007147988A1 true WO2007147988A1 (fr) | 2007-12-27 |
Family
ID=37845328
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2007/051304 WO2007147988A1 (fr) | 2006-06-21 | 2007-05-21 | Procede de fabrication du pentafluoroethane |
Country Status (8)
Country | Link |
---|---|
US (1) | US8110713B2 (fr) |
EP (1) | EP2029506A1 (fr) |
JP (1) | JP2009541278A (fr) |
KR (1) | KR101395585B1 (fr) |
CN (1) | CN101460436B (fr) |
FR (1) | FR2902788B1 (fr) |
MX (1) | MX2008015809A (fr) |
WO (1) | WO2007147988A1 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2907449B1 (fr) * | 2006-10-20 | 2009-01-02 | Arkema France | Procede de fabrication du pentafluorethane. |
CN105461509A (zh) * | 2015-12-01 | 2016-04-06 | 仇颖超 | 一种液相生产三氯二氟乙烷的方法 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB901297A (en) * | 1960-04-12 | 1962-07-18 | Union Carbide Corp | Process for the production of pentafluoroethane |
US5300710A (en) * | 1991-03-20 | 1994-04-05 | E. I. Du Pont De Nemours And Company | Process for the manufacture of 2-chloro-1,1,1,2-tetrafluoroethane and pentafluoroethane |
EP0609123A1 (fr) * | 1993-01-27 | 1994-08-03 | Elf Atochem S.A. | Procédé de fluoration du perchloréthylène ou du pentachloréthane |
EP0760808B1 (fr) * | 1994-05-25 | 1999-04-14 | AlliedSignal Inc. | Procede a un seul etage destine a produire des hydrofluorocarbures a partir de perchloroethylene |
EP0754170B1 (fr) * | 1994-04-06 | 2001-03-14 | Imperial Chemical Industries Plc | Production de pentafluoroethane |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0687660B2 (fr) * | 1993-03-05 | 2006-05-17 | Daikin Industries, Limited | Procede de production de 1,1,1,2,2-pentafluoroethane, procede de production de 2,2-dichloro-1,1,1-trifluoroethane, et procede de purification de 1,1,1,2,2-pentafluoroethane |
GB9325756D0 (en) * | 1993-12-16 | 1994-02-16 | Ici Plc | Production of pentafluoroethane |
JP3853397B2 (ja) * | 1995-05-11 | 2006-12-06 | イネオス フラウアー ホールデイングス リミテッド | ペンタフルオロエタンの製造方法及びペンタフルオロエタンに転化するのに適当な組成物 |
-
2006
- 2006-06-21 FR FR0605525A patent/FR2902788B1/fr not_active Expired - Fee Related
-
2007
- 2007-05-21 MX MX2008015809A patent/MX2008015809A/es not_active Application Discontinuation
- 2007-05-21 JP JP2009515922A patent/JP2009541278A/ja active Pending
- 2007-05-21 US US12/305,857 patent/US8110713B2/en not_active Expired - Fee Related
- 2007-05-21 KR KR1020087030340A patent/KR101395585B1/ko not_active IP Right Cessation
- 2007-05-21 WO PCT/FR2007/051304 patent/WO2007147988A1/fr active Application Filing
- 2007-05-21 EP EP07766078A patent/EP2029506A1/fr not_active Withdrawn
- 2007-05-21 CN CN2007800208968A patent/CN101460436B/zh not_active Expired - Fee Related
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB901297A (en) * | 1960-04-12 | 1962-07-18 | Union Carbide Corp | Process for the production of pentafluoroethane |
US5300710A (en) * | 1991-03-20 | 1994-04-05 | E. I. Du Pont De Nemours And Company | Process for the manufacture of 2-chloro-1,1,1,2-tetrafluoroethane and pentafluoroethane |
EP0609123A1 (fr) * | 1993-01-27 | 1994-08-03 | Elf Atochem S.A. | Procédé de fluoration du perchloréthylène ou du pentachloréthane |
EP0754170B1 (fr) * | 1994-04-06 | 2001-03-14 | Imperial Chemical Industries Plc | Production de pentafluoroethane |
EP0760808B1 (fr) * | 1994-05-25 | 1999-04-14 | AlliedSignal Inc. | Procede a un seul etage destine a produire des hydrofluorocarbures a partir de perchloroethylene |
Also Published As
Publication number | Publication date |
---|---|
CN101460436A (zh) | 2009-06-17 |
FR2902788B1 (fr) | 2008-09-05 |
KR101395585B1 (ko) | 2014-05-16 |
US20100210884A1 (en) | 2010-08-19 |
JP2009541278A (ja) | 2009-11-26 |
EP2029506A1 (fr) | 2009-03-04 |
KR20090020608A (ko) | 2009-02-26 |
FR2902788A1 (fr) | 2007-12-28 |
US8110713B2 (en) | 2012-02-07 |
MX2008015809A (es) | 2009-03-26 |
CN101460436B (zh) | 2013-12-11 |
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