WO1993010067A1 - Process for producing 1,1,1,4,4,4-hexafluorobutane - Google Patents
Process for producing 1,1,1,4,4,4-hexafluorobutane Download PDFInfo
- Publication number
- WO1993010067A1 WO1993010067A1 PCT/JP1992/001529 JP9201529W WO9310067A1 WO 1993010067 A1 WO1993010067 A1 WO 1993010067A1 JP 9201529 W JP9201529 W JP 9201529W WO 9310067 A1 WO9310067 A1 WO 9310067A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reaction
- hydrogen
- butadiene
- hexafluorobutane
- alloy
- Prior art date
Links
Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
-
- 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
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/23—Preparation of halogenated hydrocarbons by dehalogenation
Definitions
- the present invention relates to a method for producing 1,1,1.4,4,4-hexafluorobutane.
- 1,1,1,4,4,4-Hexafluorobutane is a useful compound as a refrigerant, a blowing agent, and a solvent.
- the method for producing 1,1,1,4,4,4-hexafluorobutane is as follows: 2-chloro-1,1,1,4,4,4-hexafluorobutene-1 or 1,1,1
- An object of the present invention is to provide a method for producing 1,1,1,4,4,4-hexafluorobutane by a hydrogen source in a gaseous phase which does not cause the above problems.
- the inventors of the present invention have conducted intensive studies on an easy method for industrially producing 1,1,1,4,4,4-hexafluorobutane in high yield, and as a result, have found that 2-chloro-1,1,1. ,,, 4,4-hexafluorobutene-1 in the gas phase, Hydrogenation in the presence of a platinum or palladium alloy catalyst shows that 1,1,1,1,4,4,4-hexafluorobutane can be obtained with good selectivity and high yield. They have found and completed the present invention.
- the gist of the present invention is to provide 2-chloro-1,1,1,4,4,4-hexafluorobutene-12 with at least one metal selected from the group consisting of platinum and palladium.
- a hydrogenation catalyst comprising a JS component and an alloy comprising a second metal component which is at least one metal selected from the group consisting of silver, copper, gold, tellurium, zinc, chromium, molybdenum and thallium.
- 1,1,1,4,4,4,1 is a process for producing hexafluorobutane, which is characterized by the fact that it can be transmitted by water purple in the presence of.
- the hydrogenation catalyst contains an alloy comprising the first metal component and the second metal component as a catalytically active component.
- the weight of the second metal component is 100 weight of the first metal component: 0.01 to 500 weight%, particularly 0.1 to 300 weight, with respect to ft part. Is preferable in terms of taking advantage of the characteristics of platinum or palladium.
- Activated carbon, alumina, zirconia, titania, and the like are suitable as a carrier for the water-forming catalyst.
- concentration of the alloy supported on the carrier 0.05 to 5% by weight can be used, but 0.5 to 2% by weight is recommended.
- the particle size of the carrier has little effect on the reaction, but is preferably 0.1 to 100.
- the proportions of hydrogen and 2-chloro-1,1.1,4,4,4-hexafur; f-butene-12 (R-1326) can vary widely. However, usually at least stoichiometry :! : (That is, for 1 mole of R—1 3 2 6 (At least 2 moles of hydrogen) and remove the salt purple atoms. For one mole of R-1 32 6 significantly more than stoichiometric:!:, For example 4 moles or more of water purple may be used.
- the reaction method uses a gas phase reaction in which R-136 is flowed together with hydrogen in a gaseous state over a hydrogenation catalyst filled in a reaction tube.
- a method such as a fixed bed type gas phase reaction or a fluidized type gas phase reaction can be used.
- the pressure of the reaction is not particularly limited, and it is possible to carry out the reaction under pressure, under reduced pressure, or under normal pressure. However, since the apparatus becomes complicated under reduced pressure, it is preferable to carry out the reaction under pressure or under normal pressure.
- the reaction temperature is usually 0 to 450, preferably 50 to 300 ° C.
- the contact time is usually 0.1 to 300 seconds, preferably 1 to 30 seconds.
- R-1326 can be obtained by any method, but it is prepared by fluorinating hexachloro-1,3-butadiene in the liquid phase in the presence of fluorinated antimony chloride and aqueous fluoride. Is preferred. According to this method, R-133-26 can be produced inexpensively, in a high yield, and easily. Hexachloro-1,3-butadiene is the cheapest to use as a starting material. A compound having a structure in which hydrogen chloride or hydrogen fluoride is added to 3-butadiene can also be used.
- the amount of hydrogen fluoride charged into the reactor is the sum of the amount of hydrogen fluoride that is eliminated and the amount of hydrogen fluoride that accompanies the product.
- the amount of 1,3-butadiene to be charged into the reactor will not be supported if the amount of 1,3-butadiene is small with respect to the antimony pentachloride added in the system. .
- the amount of hexachloro-1,3-butadiene to be introduced is set to 100 times mol Zhr or less and 2 times mol / hr or more with respect to the charged antimony pentachloride.
- the reaction if n reaction temperature is desirable to set more than 5 times Monore / hr is a 4 0 ° C but proceeds were charged case F Kisakuroro 1 for S bC l 8, selectivity decreases if Kere less die the introduction amount of 3-butadiene.
- Higher reaction temperatures are also advantageous in terms of productivity and selectivity, but the reaction pressure must be kept higher according to the reaction temperature.
- the reaction be performed at a temperature in the range of 50 ° C to 150 ° C.
- reaction pressure is increased according to the reaction temperature, and an appropriate pressure can be selected in a range of 3 kg / cm 2 to 3 O kg / cm 2 in order to separate hydrogen fluoride and a product.
- an appropriate pressure can be selected in a range of 3 kg / cm 2 to 3 O kg / cm 2 in order to separate hydrogen fluoride and a product.
- the amount of fluorinated water purple is practically 5 times or more and 500 times or less with respect to antimony pentachloride. It is preferably at least 50 times mol and at least 200 times mol 0
- the raw materials hexachloro-1,3-butadiene and hydrogen fluoride are charged into the reaction system, and the generated R-1326 is extracted.
- the hydrogenation reaction can be carried out as it is, or after purifying R-1326, containing R-1326 containing impurities obtained by the above method.
- the reaction pressure was controlled between 8 kg / cm 2 and 11 kg / op 2 so that the weight of the reactor was constant.
- the distilling gas was washed with water and collected with a dry ice trap.
- the reaction was stopped when 520 g (2 mol) of hexachloro-1,3-butadiene was added. 376 g (87% yield) of R-1326 was obtained as a product.
- GLC confirmed that 97% of the product was the desired R-1326. In addition, no by-products other than the intermediate were found in the reactor.
- 16 cc of this medium was charged into a SUS 316 reaction tube having an inner diameter of 2 cn and a length of 40 cm, and heated to 110 in an electric furnace while flowing nitrogen gas. After reaching the specified temperature, the flow of nitrogen gas is stopped, and 2-chloro-1,1,1,4,4,4-hexanehexafluorobutene-1 2 previously vaporized at 2 lcc / min. Was introduced at a rate of 43 cc / min.
- the reaction temperature was 110 eC .
- the generated gas was washed with water, dried with calcium chloride, and analyzed by gas chromatography. Table 1 shows the results.
- Example 2 In the same preparation method as in Example 1, an alloy catalyst in which silver was supported at 0.1 ° C using AgNOa on platinum catalyst supported on activated carbon at 0 ° C was prepared. The reaction was performed in the manner described. Table 1 shows the results.
- Example 1 In the same preparation method as in Example 1, an alloy catalyst in which tellurium was supported at 0.degree. Using TeCl: on a platinum catalyst supported on activated carbon at a concentration of 0.5 was prepared in the same manner as in Example 1. Table 1 shows the results of the reaction.
- Example 2 In the same preparation method as in Example 1, an alloy catalyst was prepared in which gold was supported at a concentration of 0.1% using AuC as a platinum medium supported on activated carbon at 0.degree. The reaction was carried out according to the following method. Table 1 shows the results.
- Example 2 According to the same preparation method as that of Example 1, an alloy corrosion medium in which zinc was supported at a concentration of 2% using ZnC Is on platinum contact supported on activated carbon at 0.5 degree of contact was produced.
- This alloy corrosion medium (16 cc) was charged into a SUS316 reaction tube having an inner diameter of 2 cni and a length of 40 mm, and heated to 110 in an electric wire while flowing a hydrogen gas. After reaching the specified temperature, the flow of nitriding gas was stopped, and 33 cc / min of 2-chloro-1,1,1,4,4,4-hexafluorobutene-2 and hydrogen were vaporized. Introduced at a rate of 66cc / min. The reaction temperature was 110 °. The generated gas was washed with water, dried over calcium iodide, and analyzed by gas chromatography. Table 1 shows the results.
- Example 2 In the same preparation method as in Example 1, an alloy catalyst in which thallium was supported at a concentration of 2% on a platinum catalyst supported on activated carbon at a concentration of 0.5% using TlCla was prepared.
- the alloy ⁇ 16cc inner diameter 2CJD, a 13 cc was filled in a SUS316-made reaction tube of ⁇ of 40 cm, it was heated in listening to 130 e C while passing nitrogen gas. After reaching a predetermined temperature, the flow of nitrogen gas was stopped, and the previously purified 2-chloro-1,1,1,4.4,4-hexafluorobutene-1 2 was added at 27.6 cc / min. Was introduced at a rate of 55. IccZ. The reaction temperature was 130. The generated gas was washed with water, dried over calcium hanide, and analyzed by gas chromatography. Table 1 shows the results.
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/090,044 US5364991A (en) | 1991-11-22 | 1992-11-24 | Preparation of 1,1,1,4,4,4-hexafluorobutane |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP3/307597 | 1991-11-22 | ||
JP30759791 | 1991-11-22 | ||
JP32032491 | 1991-12-04 | ||
JP3/320324 | 1991-12-04 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1993010067A1 true WO1993010067A1 (en) | 1993-05-27 |
Family
ID=26565180
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1992/001529 WO1993010067A1 (en) | 1991-11-22 | 1992-11-24 | Process for producing 1,1,1,4,4,4-hexafluorobutane |
Country Status (3)
Country | Link |
---|---|
US (1) | US5364991A (ja) |
EP (1) | EP0587896A1 (ja) |
WO (1) | WO1993010067A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH08143487A (ja) * | 1994-11-24 | 1996-06-04 | Agency Of Ind Science & Technol | 弗素化アルケン誘導体および弗素化アルカン誘導体の製造方法 |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5463152A (en) * | 1994-12-08 | 1995-10-31 | E. I. Du Pont De Nemours And Company | Halofluorocarbon hydrogenolysis |
US5447896A (en) * | 1992-06-23 | 1995-09-05 | E. I. Du Pont De Nemours And Company | Hydrodehalogenation catalysts and their preparation and use |
JP3304468B2 (ja) * | 1993-01-29 | 2002-07-22 | ダイキン工業株式会社 | 1,1,1,4,4,4−ヘキサフルオロ−2−ブテン類及び1,1,1,4,4,4−ヘキサフルオロブタンの製造方法 |
GB9306334D0 (en) * | 1993-03-26 | 1993-05-19 | Univ Dundee | Catalyst |
US5817896A (en) * | 1993-03-26 | 1998-10-06 | The University Court Of The University Of Dundee | Catalytic method of replacing halogen in halocarbons |
DE4421702A1 (de) * | 1994-06-21 | 1996-01-04 | Bayer Ag | Verfahren zur Herstellung von 1,1,1,4,4,4-Hexafluorbutan in flüssiger Phase |
CN107586251A (zh) * | 2017-07-26 | 2018-01-16 | 江苏蓝色星球环保科技股份有限公司 | 一种1,1,1,4,4,4‑六氟‑2‑丁烯的制备方法 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH01146831A (ja) * | 1987-10-20 | 1989-06-08 | Bayer Ag | フツ素化c↓4〜c↓6炭化水素の製造方法 |
JPH01287044A (ja) * | 1988-01-15 | 1989-11-17 | Ausimont Spa | 1,2―ジフルオロエタンおよび1,1,2―トリフルオロエタンの製造方法 |
JPH0399026A (ja) * | 1989-09-12 | 1991-04-24 | Asahi Glass Co Ltd | ペンタフルオロエタンを製造する方法 |
EP0434408A1 (en) * | 1989-12-19 | 1991-06-26 | E.I. Du Pont De Nemours And Company | Multistep synthesis of hexafluoropropylene |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3725213A1 (de) * | 1987-07-30 | 1989-02-09 | Bayer Ag | Herstellung von polyfluorbutenen |
US5210340A (en) * | 1987-07-30 | 1993-05-11 | Bayer Aktiengesellschaft | Preparation of polyfluorobutenes |
DE4004494A1 (de) * | 1990-02-14 | 1991-08-22 | Bayer Ag | Verfahren zur herstellung von gesaettigten, fluorhaltigen und chlorfreien kohlenwasserstoffen |
-
1992
- 1992-11-24 US US08/090,044 patent/US5364991A/en not_active Expired - Lifetime
- 1992-11-24 WO PCT/JP1992/001529 patent/WO1993010067A1/ja not_active Application Discontinuation
- 1992-11-24 EP EP92923999A patent/EP0587896A1/en not_active Withdrawn
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH01146831A (ja) * | 1987-10-20 | 1989-06-08 | Bayer Ag | フツ素化c↓4〜c↓6炭化水素の製造方法 |
JPH01287044A (ja) * | 1988-01-15 | 1989-11-17 | Ausimont Spa | 1,2―ジフルオロエタンおよび1,1,2―トリフルオロエタンの製造方法 |
JPH0399026A (ja) * | 1989-09-12 | 1991-04-24 | Asahi Glass Co Ltd | ペンタフルオロエタンを製造する方法 |
EP0434408A1 (en) * | 1989-12-19 | 1991-06-26 | E.I. Du Pont De Nemours And Company | Multistep synthesis of hexafluoropropylene |
Non-Patent Citations (1)
Title |
---|
See also references of EP0587896A4 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH08143487A (ja) * | 1994-11-24 | 1996-06-04 | Agency Of Ind Science & Technol | 弗素化アルケン誘導体および弗素化アルカン誘導体の製造方法 |
Also Published As
Publication number | Publication date |
---|---|
EP0587896A1 (en) | 1994-03-23 |
EP0587896A4 (en) | 1994-03-17 |
US5364991A (en) | 1994-11-15 |
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