WO1993011093A1 - Production of 1,1,1-trifluoro-2-chloroethane and/or 1,1,1,2-tetrafluoroethane - Google Patents
Production of 1,1,1-trifluoro-2-chloroethane and/or 1,1,1,2-tetrafluoroethane Download PDFInfo
- Publication number
- WO1993011093A1 WO1993011093A1 PCT/JP1992/001552 JP9201552W WO9311093A1 WO 1993011093 A1 WO1993011093 A1 WO 1993011093A1 JP 9201552 W JP9201552 W JP 9201552W WO 9311093 A1 WO9311093 A1 WO 9311093A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- hydrogen fluoride
- mixture
- column
- trifluoro
- trichloroethylene
- Prior art date
Links
Classifications
-
- 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
- C07C17/093—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
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
Definitions
- the present invention provides a fluorination reaction with hydrogen fluoride (hereinafter, referred to as HF) in the presence of a fluorination catalyst, by trichloroethylene and / or 1,1,1 trifluoro-2-chloroethane (hereinafter, referred to as R-133a). )) To produce R-133a and R or 1,1,1,2-tetrafluoroethane (hereinafter referred to as R-134a) in the product, R-133a. And recycling to the reaction step to produce R-133a and / or R-134a.
- HF hydrogen fluoride
- R-133a 1,1,1 trifluoro-2-chloroethane
- R-133a is useful as an intermediate of a fluorinated organic compound.
- R-134a is used in refrigerants and foaming applications as an alternative to regulated chlorofluorocarbons, dichlorodifluoromethane.
- R-133a and R-134a are usually obtained by fluorinating trichlorethylene with HF in the gas phase in the presence of a chromium-based catalyst.
- R-134a can also be obtained by reacting R-133a in the same manner. The reaction proceeds sequentially and is represented by the following reaction formula.
- CC1 2 CHC1 + 3HF ⁇ CF 3 CH 2 C1 + 2HC1 (1)
- the reaction (2) that produces R-134a has an equilibrium, and the reverse reaction is about 100 times faster than the forward reaction. For this reason, a relatively efficient Even in the case of a phase reaction, the reaction is carried out using a large excess of HF, but it is still difficult to increase the conversion of R-133a to 30% or more. Therefore, it is necessary to separate unreacted R-133a and HF from the reaction product and recycle it to the reaction step.
- a method of washing the entire reaction product with water is described, and a method of high efficiency and a separation and circulation method has not been known at all.
- the mixture obtained in the reaction step centering on this gas phase reaction contains R-133a, R-134a, hydrogen chloride, HF and, in some cases, trichloroethylene.
- trichloroethylene is completely fluorinated and the case where R-133a is fluorinated in the reaction step, trichloroethylene is not substantially found. However, even in these cases, it is difficult to completely eliminate them, and usually about 0.1 mol% of trichlorethylene is contained.
- a small amount of water contained in the raw material is always present, albeit in a small amount. Water, even in trace amounts, reduces catalytic activity and inhibits the reaction.
- the reaction mixture is first cooled and then charged into a distillation column, and hydrogen chloride, which moves the flat mouth of reaction (2) to the left, and an azeotropic mixture of R-134a and HF as a low-boiling mixture.
- hydrogen chloride which moves the flat mouth of reaction (2) to the left
- an azeotropic mixture of R-134a and HF as a low-boiling mixture.
- R-133a, HF and possibly trichloroethylene are withdrawn from the bottom as a high-boiling mixture.
- the high-boiling mixture is vaporized by an evaporator and recovered as a circulation gas in the reaction system.
- an evaporator is required separately from the distillation column, and the equipment becomes very complicated.
- azeotropic compositions exist for R-1333, ⁇ :, trichloroethylene and HF, respectively, which are different from the azeotropic compositions of water and HF. That, under certain pressures, a mixture of HF, R-133a, and trichloroethylene of any composition has an equilibrium temperature between the boiling point of the azeotropic composition of R-133a and HF and the boiling point of HF; It has also been found that since this temperature is different from the azeotropic temperature of water and HF, a highly pure mixture of the above three compounds can be easily obtained.
- the mixture when distilling and separating the fluorination reaction mixture, the mixture can be circulated to the reaction step as it is by extracting the mixture from the middle stage of the distillation column with the gas in the above temperature range. And found that the present invention could be omitted, and completed the present invention.
- the present invention provides a reaction step of reacting trichloroethylene and / or R-133a with hydrogen fluoride in the gas phase in the presence of a fluorination catalyst to produce R-133a and R- or R-134a.
- R-133a, R-134a as the main components obtained.
- R-133a, hydrogen fluoride and possibly trichloroethylene are separated from the mixture containing hydrogen fluoride and possibly trichloroethylene and recycled to the above reaction step.
- a part or all of the mixture is distilled in a distillation column, a component rich in R-134a is extracted from the top of the column, and R-133a and hydrogen fluoride under the internal pressure of the distillation column are extracted.
- the present invention can be applied to any composition as long as it is a method of reacting trichloroethylene, R-133a or both of them with HF in a gas phase.
- the mixture obtained in the reaction step is a gas mainly composed of R-133a, R-134a, hydrogen chloride, HF and possibly trichloroethylene. These are usually cooled down to a temperature of 50 ° C to 50 ° C, and most of them are charged into a distillation column after liquid cooling.
- the method of charging the distillation column is not limited to the above-described liquid charging, and in addition to the liquid charging, the gas that could not be condensed may be charged to the distillation column at an increased pressure if necessary. If necessary, all the mixture may be charged to the distillation column without condensing, if necessary, and the reaction mixture may be charged at its own pressure in a liquid, gaseous or mixed phase state.
- the pressure in the distillation column is not particularly limited, but usually from atmospheric pressure to 20 atm. If it is lower than this, energy is required for cooling at the top of the column, and if it is higher than this, cost is required to make the distillation column pressure-resistant.
- the mixture led to the distillation column is separated into a low-boiling mixture mainly containing hydrogen chloride, R-134a and HF, and a high-boiling point mixture mainly containing R-133a, trichloroethylene and HF.
- the low-boiling mixture is withdrawn from the top of the distillation column, and the high-boiling mixture is withdrawn in gaseous form from the middle stage below the reaction mixture preparation stage and above the bottom of the column.
- the extraction temperature must be equal to or higher than the azeotropic point of R-133a and HF, lower by 5 than the boiling point of HF, and lower than the temperature. Otherwise, R-134a and water will be circulated to the reaction process.
- the boiling point of trichlorethylene is 120 ° C at 1.5 kg / cm 2 G, and normally remains at the bottom of the column as a high boiling component, but the azeotropic point with HF is 41 ° C under this pressure, so the above range Withdrawing at the temperature inside It becomes possible.
- high-purity circulating gas is obtained by leaving higher boiling substances such as water and tar at the bottom of the tower.
- this gas can be fed into the reaction system as it is as a reaction circulating gas, and the step of evaporating a high-boiling mixture conventionally extracted from the bottom of the distillation column with an evaporator or the like can be omitted.
- This simplification of the equipment can greatly reduce equipment costs compared to the past, and water and tar extracted from the bottom of the tower usually contain HF. These may be separated in another distillation column to recover only useful HF.
- composition ratio of R-133a and HF which is mainly extracted from the middle stage of the distillation column, has a large effect on the reaction, and therefore, by adding hydrogen fluoride to this distillation column, the composition ratio can be changed at will. It can be changed.
- R-133a When R-133a is obtained alone, it is also possible to extract R-133a and HF as an azeotrope from a stage above the circulation gas extraction stage.
- a distillation column with 51 vessels at the bottom and a condenser at the top (35 theoretical plates, 50-diameter column) is charged with 2 mol of R-134a, 25 mol of R-133a, and 70 mol of HF, and 9 kgZcm without extraction
- a reflux state was created to maintain a pressure of 2 G.
- the temperature at the top of the column was 39, and the composition of the reflux liquid was 95 mol% for R-134a and 5 mol% for HF, indicating an azeotropic composition.
- the gas obtained by reacting R-133a with HF and Z or with trichloroethylene and HF was cooled to 0 ° C, and only the liquid phase was pumped. Table 1 shows the respective flow rates.
- the pressure was maintained at 9 kgZcni 2 G by discharging gas from the outlet of the cooler.
- the gas that did not condense was washed with water, dried, condensed under pressure, and stored in a tank. After about 5 minutes, the gas temperature near the outlet at the third stage from the bottom of the tower reached 90 ° C, so extraction from the gas phase was started while keeping the liquid volume in the container constant.
- the extracted gas was circulated to the reactor simply by adding the consumed HF and trichloroethylene. This was continued, and two hours later, the composition of the circulating gas, the gas extracted from the top of the tower, and the liquid in the vessel were analyzed. The extraction temperature at this time was 88 ° C.
- the total amount of acids (HF and hydrogen chloride) was determined by titration after absorption with water, and the ratio of chloride ions to fluoride ions was calculated by ion chromatography to calculate the respective amounts.
- the composition of organic substances was determined by gas chromatography.
- the water content was determined by the Karl Fisher method. Table 2 shows their compositions. The water was efficiently separated, and the useful unreacted substances, HF, R-133a and trichloroethylene, which were led to the distillation column, could be recovered almost all without waste, and proved to be of very high purity. . Comparative Example 1
- Example 2 shows the composition. R-134a contamination is observed.
- Example 1 When Example 1 was further continued, after a lapse of 12 hours, the temperature of the outlet began to gradually increase.
- the composition at 95 ° C. is shown in the column of Example 2 in Table 2, and the composition at 100 ° C. is shown in the column of Comparative Example 2. Temperature outside the preferred range
- the fluorination reaction mixture is cooled and charged into the distillation column, and high-purity R-133a, trichloroethylene and trichloroethylene containing no other impurities from the lower middle stage of the column.
- a mixture of HF can be obtained.
- by circulating the extracted mixture to the reaction process only by directly heating it without a vaporizer it is possible to omit a group of evaporating apparatuses which has been conventionally required, and to simplify the equipment. Furthermore, it is possible to concentrate water tar on the bottom of the distillation column and to easily extract it from the reaction circulation system.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/090,077 US5426251A (en) | 1991-11-27 | 1992-11-27 | Process for preparing 1,1,1-trifluoro-2-chloroethane and/or 1,1,1,2-tetrafluoroethane |
DE69212484T DE69212484T2 (de) | 1991-11-27 | 1992-11-27 | Herstellung von 1,1,1-trifluoro-2-chloroethan und/oder 1,1,1,2-tetrafluoroethan |
EP92924019A EP0594859B1 (en) | 1991-11-27 | 1992-11-27 | Production of 1,1,1-trifluoro-2-chloroethane and/or 1,1,1,2-tetrafluoroethane |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP3312328A JP2661441B2 (ja) | 1991-11-27 | 1991-11-27 | 1,1,1−トリフルオロ−2−クロロエタンおよび/または1,1,1,2−テトラフルオロエタンの製法 |
JP3/312328 | 1991-11-27 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1993011093A1 true WO1993011093A1 (en) | 1993-06-10 |
Family
ID=18027916
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1992/001552 WO1993011093A1 (en) | 1991-11-27 | 1992-11-27 | Production of 1,1,1-trifluoro-2-chloroethane and/or 1,1,1,2-tetrafluoroethane |
Country Status (5)
Country | Link |
---|---|
US (1) | US5426251A (ja) |
EP (1) | EP0594859B1 (ja) |
JP (1) | JP2661441B2 (ja) |
DE (1) | DE69212484T2 (ja) |
WO (1) | WO1993011093A1 (ja) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5718807A (en) * | 1994-09-20 | 1998-02-17 | E. I. Du Pont De Nemours And Company | Purification process for hexafluoroethane products |
US5853550A (en) * | 1996-04-12 | 1998-12-29 | E. I. Du Pont De Nemours And Company | Process for separating tar from a reaction mixture |
WO2001007384A1 (en) * | 1999-07-21 | 2001-02-01 | Halocarbon Products Corporation | Production of aliphatic fluorocarbons |
CN101117305B (zh) * | 2007-04-11 | 2010-07-28 | 西安近代化学研究所 | 1,1,1,2-四氟乙烷的制备方法 |
CN112250540B (zh) * | 2020-10-14 | 2023-10-31 | 太仓中化环保化工有限公司 | 一种从精馏重组分中分离R134a、R133a和R124的方法 |
CN112174801B (zh) * | 2020-10-15 | 2022-03-29 | 江苏蓝色星球环保科技股份有限公司 | 一种一锅法联产制备羟基乙酸与1,1,1,2-四氟乙烷的方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS493965B1 (ja) * | 1968-01-29 | 1974-01-29 | ||
JPH01221338A (ja) * | 1987-07-07 | 1989-09-04 | E I Du Pont De Nemours & Co | 気相フッ素化方法 |
JPH02295938A (ja) * | 1989-05-04 | 1990-12-06 | Atochem North America Inc | ふっ化水素、1,1―ジクロロ―1―フルオロエタン及び1―クロロ―1,1―ジフルオロエタンをそれらの液状混合物から分離する方法 |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3558438A (en) * | 1968-10-30 | 1971-01-26 | Du Pont | Distillation process and apparatus |
US4944846A (en) * | 1988-08-01 | 1990-07-31 | E. I. Dupont De Nemours And Company | Process for the separation of HF via Azeotropic distillation |
EP0455748B2 (en) * | 1989-02-03 | 2003-01-15 | E.I. Du Pont De Nemours And Company | Manufacture of 1,1,1,2-tetrafluoroethane |
AU645063B2 (en) * | 1990-03-13 | 1994-01-06 | Daikin Industries, Ltd. | Process for preparing 1,1,1,2-tetrafluoroethane |
GB9007029D0 (en) * | 1990-03-29 | 1990-05-30 | Ici Plc | Chemical process |
-
1991
- 1991-11-27 JP JP3312328A patent/JP2661441B2/ja not_active Expired - Fee Related
-
1992
- 1992-11-27 US US08/090,077 patent/US5426251A/en not_active Expired - Lifetime
- 1992-11-27 WO PCT/JP1992/001552 patent/WO1993011093A1/ja active IP Right Grant
- 1992-11-27 DE DE69212484T patent/DE69212484T2/de not_active Expired - Fee Related
- 1992-11-27 EP EP92924019A patent/EP0594859B1/en not_active Expired - Lifetime
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS493965B1 (ja) * | 1968-01-29 | 1974-01-29 | ||
JPH01221338A (ja) * | 1987-07-07 | 1989-09-04 | E I Du Pont De Nemours & Co | 気相フッ素化方法 |
JPH02295938A (ja) * | 1989-05-04 | 1990-12-06 | Atochem North America Inc | ふっ化水素、1,1―ジクロロ―1―フルオロエタン及び1―クロロ―1,1―ジフルオロエタンをそれらの液状混合物から分離する方法 |
Also Published As
Publication number | Publication date |
---|---|
US5426251A (en) | 1995-06-20 |
JPH05148170A (ja) | 1993-06-15 |
JP2661441B2 (ja) | 1997-10-08 |
EP0594859A4 (en) | 1994-03-17 |
EP0594859B1 (en) | 1996-07-24 |
DE69212484T2 (de) | 1996-12-19 |
DE69212484D1 (de) | 1996-08-29 |
EP0594859A1 (en) | 1994-05-04 |
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