PROCESS FOR PRODUCING 1,1-DICHLORO-1,2,2,2-TETRAFLUOROETHANE

Abstract: A process for producing 1,1-dichloro-1,2,2,2-­ tetrafluoroethane which comprises isomerizing 1,1,2-­ trichloro-1,2,2-trifluoroethane to form 1,1,1-trichloro-­ 2,2,2-trifluoroethane, followed by fluorination with hydrofluoric acid.

Description: The present invention relates to a process for producing 1,1-dichloro-1,2,2,2-tetrafluoroethane. For the production of 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a), a method is known wherein a haloethane such as 1,1,2-trichloro-1,2,2-trifluoroethane (CCl₂FCClF₂) is fluorinated. In this case, the reaction product will be a mixture of 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a) and 1,2-dichloro-1,1,2,2-tetrafluoroethane (R-114). This may be attributable to the facts that during the fluorination, the substitution between the fluorine atom in hydrogen fluoride and the chlorine atom in 1,1,2-trichloro-1,2,3-trifluoroethane (R-113) does not necessarily preferentially take place at the CClF₂ side and that the isomerization rate from 1,2-dichloro-1,1,2,2-tetrafluoroethane (R-114) to 1,1-dichloro-1,2,2,2-tetrafluoroehtane (R-114a) is small. Among the isomers of chlorofluorocarbons, the difference in the boiling points is rather small in many cases. This is true as between 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a) and 1,2-dichloro-1,1,2,2-tetrafluoroethane (R-114), which have the boiling points of 3.0°C and 3.8°C, respectively. Thus, the separation of the products is difficult. Accordingly, it is presently difficult to obtain a high purity product of 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a) at low costs. It is an object of the present invention to provide a novel process for producing highly pure 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a). The present invention provides a process as defined in claim 1 for producing 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a), which comprises isomerizing 1,1,2-trichloro-1,2,2-trifluoroethane (R-113) to form 1,1,1-trichloro-2,2,2-trifluoroethane (R-113a), followed by fluorination with hydrofluoric acid. Among haloethanes of the formula C₂Cl (6-n) F n wherein n is an integer of from 1 to 4, 1,1,2-trichloro-1,2,2-trifluoroethane (R-113) is most suitable as starting material especially from the economical view point since it is produced and sold in a large amount for a cleaning solvent used for the preparation of semi-conductor products. In order to obtain highly pure 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a), it is necessary to adopt a reaction route and reaction conditions under which 1,2-dichloro-1,1,2,2-tetrafluoroethane (R-114), i.e. the isomer having an extremely close boiling point, is not substantially produced as a by-product. From the study of the behavior of R-113 in the isomerization and disproportionation, it has been found that the isomerization rate from R-113 to R-113a is higher than the disproportionation rate to R-112a and R-114a. Accordingly, it has been found possible to produce highly pure R-114a at low costs by optimizing the catalyst and reaction conditions in the reaction route which comprises the isomerization of R-113, followed by the fluorination. The present inventors have conducted extensive researches on the reaction conditions including the isomerization catalysts and fluorination catalysts based on the results of the above study and have finally found a process for producing highly pure R-114a at high efficiency by using R-113 as starting material. Now, the reaction of the present invention will be described in detail. In the present invention, as the isomerization catalyst, a halide or oxide containing at least one element selected from the group consisting of Al, Cr, Mg, Ca, Sr, Ba, Fe, Ni and Co, is employed. From the viewpoint of acid resistance and maintenance of the catalytic activities, it is preferred to employ oxides such as Al₂O₃, Cr₂O₃, MgO and CaO and mixed oxides thereof, or halides such as AlCl₃ and CrCl₃. In the present invention, as the fluorination catalyst, a halide or oxide containing at least one element selected from the group consisting of Al, Cr, Mg, Ca, Sr, Ba, Fe, Ni, Co, Sb, Nb, Mn and Ta is employed. When a gas phase fluorination method is employed, it is preferred to employ oxides such as Al₂O₃ , Cr₂O₃, MgO and CaO and mixed oxides thereof. When a liquid phase fluorination method is employed, it is preferred to employ halides such as TaF₅, NbCl₅ and SbCl₅. All of the above catalysts are preferably activated with hydrogen fluoride or with a halogenated methane or halogenated ethane containing at least one fluorine atom such as R-11 or R-12, before they are used for the respective reactions. The isomerization reaction is conducted usually within a temperature range of from 50 to 550°C, preferably from 100 to 400°C, under normal or elevated pressure in the gas phase or under normal or elevated pressure in the liquid phase. The contact time is usually from 0.1 to 300 seconds, preferably from 5 to 30 seconds, in the case where the reaction is conducted in the gas phase. In a case where the reaction is conducted in the liquid phase, the retention time in the reactor is usually from 0.1 to 10,000 minutes, preferably from 10 to 1,000 minutes. In order to maintain the catalytic activities, it is preferred that oxygen or chlorine is present in an amount of from 0.1 to 10% relative to R-113. The fluorination reaction is conducted usually within a temperature range of from 50 to 550°C, preferably from 50 to 450°C, under normal or elevated pressure in the gas phase, or under elevated pressure in the liquid phase. The ratio of hydrogen fluoride to R-113a may be varied to a large extent. However, it is usual to use hydrogen fluoride in its stoichiometric amount for the substitution of the chlorine atom. Hydrogen fluoride may be used in an amount considerably larger than the stoichiometric amount relative to the total mols of the starting materials, for example, in an amount of 4 mols or larger. The contact time is usually from 0.1 to 300 seconds, preferably from 5 to 30 seconds, in the case where the reaction is conducted in the gas phase. When the reaction is conducted in the liquid phase, the retention time in the reactor is usually from 0.1 to 10,000 minutes, preferably from 10 to 1,000 minutes. As mentioned above, in order to maintain the catalytic activities, it is preferred that oxygen or chlorine is present in an amount of from 0.1 to 10% relative to R-113a. The reaction system may be of liquid phase or of gas phase. For a continuous reaction system, the apparatus can be simplified by conducting both the isomerization reaction and the fluorination reaction in gas phase. The desired product of the present invention can be separated by a usual method such as fractional distillation. By-products such as R-113a, 1,1,2,2-tetrachloro-1,2-fluoroethane (R-112) and 1,1,1,2-tetrachloro-2,2-fluoroethane (R-112a) may be recycled to the reaction system. As described in the foregoing, the present invention provides a process for producing a highly pure 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a) by the isomerization of R-113, followed by fluorination. Now, the present invention will be described in further detail with reference to Examples. However, it should be understood that the present invention is by no means restricted by such specific Examples. PREPARATION EXAMPLE 1 1,100 g of guaranteed reagent Al(NO₃)₃.9H₂O, 125 g of Cr(NO₃)₃.9H₂O and 10 g of Mg(NO₃)₂.6H₂O were dissolved in 2.5 ℓ of water. This solution and 2,000 g of a 28% ammonium hydroxide aqueous solution were added to 4 ℓ of hot water under stirring to obtain precipitates of hydroxides. The precipitates were collected by filtration, washed with deionized water and dried. Then, they were calcined at 450°C for 5 hours to obtain a powder of oxides. The powder was formed into a cylinderical catalyst having a diameter of 5 mm and a height of 5 mm by means of a tabletting machine. The catalyst thus obtained was activated by fluorination at a temperature of from 200 to 400°C in a gas mixture stream of hydrogen fluoride/nitrogen prior to the reaction. PREPARATION EXAMPLES 2 TO 4 Catalysts were prepared in the same manner as in Preparation Example 1 except that 40 g of Ba(NO₃)₂, 50 g of Sr(NO₃)₂ and 40 g of Ca(NO₃).4H₂O were used, respectively, instead of Mg(NO₃)₂.6H₂O. PREPARATION EXAMPLE 5 A catalyst was prepared in the same manner as in Preparation Example 1 except that 300 g of Fe(NO₃)₂.9H₂O₂ and 900 g of Al(NO₃)₃.9H₂O were used instead of Al(NO₃)₃.9H₂O, Cr(NO₃)₃.9H₂O and Mg(NO₃)₂.6H₂O. PREPARATION EXAMPLE 6 A catalyst was prepared in the same manner as in Preparation Example 1 except that 600 g of Fe(NO₃)₂.9H₂O₂ and 150 g of Cr(NO₃)₃.9H₂O were used instead of Al(NO₃)₃.9H₂O, Cr(NO₃)₃.9H₂O and Mg(NO₃)₂.6H₂O. PREPARATION EXAMPLE 7 A catalyst was prepared in the same manner as in Preparation Example 1 except that 150 g of Cr(NO₃)₃.9H₂O and 1,300 g of Al(NO₃)₃.9H₂O were used instead of Al(NO₃)₃.9H₂O, Cr(NO₃)₃.9H₂O and Mg(NO₃)₂.6H₂O. PREPARATION EXAMPLE 8 A catalyst was prepared in the same manner as in Preparation Example 1 except that 500 g of Cr(NO₃)₃.9H₂O and 160 g of Mg(NO₃)₂.6H₂O were used instead of Al(NO₃)₃.9H₂O, Cr(NO₃)₃.9H₂O and Mg(NO₃)₂.6H₂O. PREPARATION EXAMPLE 9 200 g of AlCl₃ was dissolved in 2 liter of water. To this solution, 1,000 g of commercially available γ-alumina was added, and the mixture was dried to remove water. Further, the dried product was activated in the same activation method as in Preparation Example 1. PREPARATION EXAMPLE 10 A catalyst was prepared in the same manner as in Preparation Example 9 except that 200 g of CrCl₃.6H₂O was used instead of AlCl₃. The catalyst was activated in the same activation method as in Preparation Example 1. PREPARATION EXAMPLE 11 A catalyst was prepared in the same manner as in Preparation Example 9 except that 200 g of MnCl₂.4H₂O was used instead of AlCl₃. The catalyst was activated in the same activation method as in Preparation Example 1. PREPARATION EXAMPLE 12 A catalyst was prepared in the same manner as in Preparation Example 9 except that 1,000 g of commercially available granular active carbon for catalyst carrier was used instead of γ-alumina. The catalyst was activated in the same activation method as in Preparation Example 1. PREPARATION EXAMPLE 13 A catalyst was prepared in the same manner as in Example 10 except that 1,000 g of commercially available granular active carbon for catalyst carrier was used instead of γ-alumina. The catalyst was activated in the same activation method as in Preparation Example 1. EXAMPLE 1 Inconel 600 U-shaped reactor tubes having an inner diameter of 2.54 cm and a length of 100 cm were used as reactors for isomerization and fluorination. A reactor packed with 200 cc of the γ-alumina catalyst activated in the same manner as in Preparation Example 1 was used as the reactor for the first isomerization reaction. A reactor packed with 200 ml of the fluorination catalyst prepared in the same manner as in Preparation Example 1 was used as the reactor for the second fluorination reaction. The first and second reactions were continuously conducted. To the first reactor, gasified 1,1,2-trichloro-1,2,2-trifluoroethane was supplied at a rate of 100 ml/min, and chlorine was supplied at a rate of 2 ml/min, and the reactor was held at 250°C. To the second reactor, hydrogen fluoride was supplied at a rate of 100 ml/min, and the reactor was held at 320°C. After removing acid components, the gas composition was analyzed by gas chromatography and ¹⁹F-NMR. The results are shown in Table 1. Gas composition at the outlet of the reactor Molar ratio (%) R-114a 72.0 R-114 1.7 R-113a 17.3 R-113 4.5 Others 4.5 EXAMPLE 2 The reaction was conducted under the same condition as in Example 1 except that the fluorination reaction temperature was changed to 350°C. After removing acid components, the gas composition was analyzed. The results are shown in Table 2. Gas composition at the outlet of the reactor Molar ratio (%) R-114a 72.2 R-114 2.1 R-113a 13.1 R-113 7.5 Others 7.1 EXAMPLES 3 TO 14 The catalysts prepared in Preparation Examples 1 to 13 and γ-alumina used in Example 1 were used as catalysts. The reactions were conducted under the same conditions as in Example 1 except that the isomerization catalyst and the reaction temperature, and the fluorination catalyst and the reaction temperature were changed as shown in Table 3. The results are shown in Table 3. Example Nos. Isomerization catalyst Reaction temp. (°C) Fluorination catalyst Reaction temp. (°C) Gas composition at the outlet of the reactor (molar ratio %) 114a 114 113a 113 Others 3 Fe₂O₃Al₂O₃ 280 Cr₂O₃MgOAl₂O₃ 320 68.0 2.5 15.5 4.8 9.2 4 Cr₂O₃BaOAl₂O₃ 300 Cr₂O₃BaOAl₂O₃ 300 68.0 2.5 15.9 3.6 10.0 5 Cr₂O₃SrOAl₂O₃ 300 Cr₂O₃SrOAl₂O₃ 300 62.0 4.4 18.8 8.5 6.3 6 Cr₂O₃CaOAl₂O₃ 300 Cr₂O₃CaOAl₂O₃ 300 70.5 5.8 14.2 5.4 4.1 7 Fe₂O₃Cr₂O₃ 300 Fe₂O₃Cr₂O₃ 300 67.8 5.9 13.7 6.4 6.2 8 Al₂O₃ 250 Fe₂O₃Cr₂O₃ 350 72.5 1.6 19.8 3.2 2.9 9 Cr₂O₃Al₂O₃ 250 Cr₂O₃Al₂O₃ 320 69.3 2.8 14.6 6.8 6.5 10 Cr₂O₃MgO 250 Cr₂O₃MgO 300 63.8 5.2 12.7 3.4 14.9 11 Al₂O₃ 250 Al₂O₃ 350 46.3 8.4 22.9 3.5 18.9 12 Al₂O₃ 250 MnCl₂/Al₂O₃ 350 48.5 7.7 21.4 6.8 15.6 13 AlCl₃/Al₂O₃ 250 CrCl₃/Al₂O₃ 350 67.8 3.3 16.1 4.3 8.5 14 AlCl₃/C 250 CrCl₃/C 350 63.8 3.7 24.1 4.2 4.2 EXAMPLE 15 Into a Hastelloy C autoclave having an internal capacity of 1 liter, 20 g of aluminium chloride and 600 ml of 1,1,2-trichloro-1,2,2-trifluoroethane were introduced and maintained at 80°C for 7 hours. After cooling, the mixture was transferred to another Hastelloy C autoclave having an internal capacity of 1 liter, and 20 g of antimony pentachloride was added thereto. The mixture was heated to 120°C. Then, hydrogen fluoride was supplied at a rate of 50 g/hr for 4 hour, and the mixture was maintained for further 4 hours. After removing acid components, the gas composition was analyzed in the same manner as in Example 1. The results are shown in Table 4. Gas composition at the outlet of the reactor Molar ratio (%) R-114a 60.0 R-114 5.2 R-113a 27.3 R-113 4.5 Others 3.0 EXAMPLE 16 An Inconel 600 U-shaped reactor tube having an inner diameter of 2.54 cm and a length of 100 cm was used as the reactor for isomerization. The reactor packed with 200 cc of the alumina catalyst activated in the same manner as in the Preparation Examples was used as the reactor for isomerization. A condenser was connected to the outlet of the reactor, and a pump was provided so that the reaction mixture was introduced into a reactor of the second fluorination reaction (a Hastelloy C autoclave having a capacity of 1 liter) containing 20 g of antimony pentachloride. The reactions were conducted continuously. To the first reactor, gasified 1,1,2-trichloro-1,2,2-trifluoroethane was supplied at a rate of 100 ml/min, and chlorine was supplied at a rate of 2 ml/min.The reaction system was maintained at 250°C. To the second reactor, hydrogen fluoride was supplied at a rate of 20 g/hr, and the system was maintained at a temperature of 120°C. After removing acid components, the gas composition was analyzed by gas chromatography and ¹⁹F-NMR. The results are shown in Table 5. Gas composition at the outlet of the reactor Molar ratio (%) R-114a 58.0 R-114 1.1 R-113a 20.8 R-113 19.4 Others 0.7 EXAMPLE 17 Into a Hastelloy C autoclave having an internal capacity of 1 liter, 20 g of aluminium chloride powder and 600 ml of 1,1,2-trichloro-1,2,2-trifluoroethane were introduced and maintained at 80°C for 7 hours. After cooling, the crude reaction solution was subjected to filtration. The successive fluorination reaction was conducted by using an Inconel 600 U-shaped tube having an inner diameter of 2.54 cm and a length of 100 cm as the reactor. The reactor packed with 200 ml of the fluorination catalyst prepared in the same manner as in Preparation Example 1 was used for fluorination. The crude reaction solution of the first reaction was gasified and supplied to the second reactor at a rate of 100 ml/min, chlorine supplied at a rate of 2 ml/min, and hydrogen fluoride was supplied at a rate of 100 ml/min. The reaction system was held at 320°C. After removing acid components, the gas composition was analyzed by gas chromatography and ¹⁹F-NMR. The results are shown in Table 6. Gas composition at the outlet of the reactor Molar ratio (%) R-114a 68.8 R-114 4.7 R-113a 12.3 R-113 11.2 Others 3.0 COMPARATIVE EXAMPLE 1 An Inconel 600 U-shaped reactor tube having an inner diameter of 2.54 cm and length of 100 cm was used as the reactor for fluorination. The reactor packed with 200 ml of the catalyst prepared in the same manner as in Preparation Example 1, was used as the reactor for fluorination. To the reactor, gasified 1,1,2-trichloro-1,2,2-trifluoroethane was supplied at a rate of 100 ml/min, chlorine was supplied at a rate of 2 ml/min, and hydrogen fluoride was supplied at a rate of 100 ml/min. The reaction system was held at 320°C. After removing acid components, the gas composition was analyzed. The results are shown in Table 7. Gas composition at the outlet of the reactor Molar ratio (%) R-114a 15.3 R-114 61.1 R-113a 1.5 R-113 8.5 Others 13.6 As is evident from the foregoing Examples, the present invention provides an advantage that 1,1-dichloro-1,2,2,2-tetrafluoroethane (R-114a) which used to be hardly available as a high purity product, can readily be produced in good yield from R-113 used as starting material.

Claims: A process for producing 1,1-dichloro-1,2,2,2-tetrafluoroethane, which comprises isomerizing 1,1,2-trichloro-1,2,2-trifluoroethane in the presence of an isomerization catalyst comprising a halide or oxide of at least one element selected from the group consisting of Al, Cr, Mg, Ca, Sr, Ba, Fe, Ni and Co, to form 1,1,1-trichloro-2,2,2-trifluroroethane, followed by fluorination with hydrofluoric acid in the presence of a fluorination catalyst comprising a halide or oxide of at least one element selected from the group consisting of Al, Cr, Mg, Ca, Sr, Ba, Fe, Ni, Co, Sb, Nb, Mn and Ta. The process according to Claim 1, wherein the isomerization is conducted at a temperature of from 50 to 550°C under normal or elevated pressure in the gas phase or under normal or elevated pressure in the liquid phase. The process according to Claim 1, wherein the fluorination is conducted at a temperature of from 50 to 550°C under normal or elevated pressure in the gas phase, or under elevated pressure in the liquid phase.

Inventors: MORIKAWA, SHINSUKE, SAMEJIMA, SHUNICHI, TATEMATSU, SHIN, YOSHITAKE, MASARU
Applicants: ASAHI GLASS COMPANY LTD.
Application year: 1988
Main classification: C07C22
IPC codes: B01J27, B01J23, C07C19, C07C17, C07B61, B01J21, C07C67, B01J37