Patentamt 975 JEuropaischesEuropean Patent Office Publication number: 0163 B1 Office europeen des brevets

EUROPEAN PATENT SPECIFICATION

Date of publication of patent specification: 10.08.88 mt.ci.4: C 07 C 51/21, C 07 C 53/18, C 07 C 51/58, C 07 C 53/48 Application number: 85105653.1

Date of filing: 08.05.85

Process for producing and trif luoroacetyl chloride.

COMPANY LTD. Priority: 15.05.84 JP 95537/84 Proprietor: ASAHI GLASS 15.05.84 JP 95538/84 No. 1-2, Marunouchi 2-chome 15.05.84 JP 95539/84 Chiyoda-ku, Tokyo (JP)

Date of publication of application: Inventor: Gotoh, Isao 11.12.85 Bulletin 85/50 3050-25, Kawashima-cho Asahi-ku, Yokohama-shi Kanagawa-ken (JP) Inventor: Yoneda, Hajime Publication of the grant of the patent: 1846-1, Goi Ichihara-shi 10.08.88 Bulletin 88/32 Chiba-ken (JP) Inventor: Kumai, Seisaku 2-12-5, Minamioi Shinagawa-ku Designated Contracting States: Tokyo (JP) BECHDEFRGBITLINL Inventor: Ueno, Tohru Green-Haimu Izumino 27-104 6205-1, Izumi-cho Totsuka-ku References cited: Yokohama-shi Kanagawa-ken (JP) US-A-3 151 051

CD CHEMICAL ABSTRACTS, vol. 100, no. 11, Representative: Wachtershauser, Giinter, Dr. March 12, 1984, page 507, abstract no. 85270u, Tal29 in Columbus, Ohio, US D-8000 Miinchen 2 (DE)

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Note: Within nine months from the publication of the mention of the grant of the European patent, any person may give notice to the European Patent Office of opposition to the European patent granted. Notice of opposition shall Q. be filed in a written reasoned statement. It shall not be deemed to have been filed until the opposition fee has been Ill paid. (Art. 99(1 ) European patent convention). Courier Press, Leamington Spa, England. 0 163 975 Description

The present invention relates to a process for producing trifluoroacetic acid (hereinafter referred to simply as "TFA") and trifluoroacetyl chloride (hereinafter referred to simply as "TFAC") by reacting 5 continuously 1,1-dichloro-2,2,2-trifluoroethane (hereinafter referred to simply as "R— 123"), oxygen and . TFAC is useful as a starting material for the production of agricultural chemicals or medicines, and TFA is useful not only as a starting material for the production of agricultural chemicals or medicines, but also as a solvent for various reactions or as a catalyst for e.g. esterification or condensation. Heretofore, for the 10 production of these compounds, there have been known (1) a method for the production of TFA by electrolytically fluorinating acetyl fluoride (U.S. Patent No. 4,022,824), (2) a method for the production of TFAC by reacting 1,1,1-trifluoro-2,2,2-trichloroethane with sulfur trioxide in the presence of a (Japanese Unexamined Patent Publication No. 501649/1981), or (3) a method for the production of TFAC by reacting R — 123 containing water in a small amount of less than 0.1% by weight with oxygen in the 15 presence of active radiation. However, in the electrolytic fluorination, the separation of trifluoroacetyl fluoride as the intermediate product from is costly. In the method wherein a mercury salt is employed, the reagent requires careful handling, and the method is accordingly industrially disadvantageous. In the method wherein active radiation is employed, the glass material of the radiation source will be devitrified by hydrofluoric acid produced in a small amount as a by-product, and can not be 20 USed for a long period of time. Thus, the conventional methods have some drawbacks. The present applicants have previously proposed a process which overcomes the drawbacks of the conventional methods. Namely, the process comprises thermally oxidizing R — 123 in the presence of water to obtain TFA and TFAC (Japanese Unexamined Patent Publication No. 159440/1983). The present invention is an improvement over the process previously proposed by the applicants, 25 whereby the conversion of R— 123, the selectivity for TFA and TFAC and the reaction time have been improved. Namely, the present invention provides a process for producing trifluoroacetic acid and trifluoroacetyl chloride from 1,1-dichloro-2,2,2-trifluoroethane, oxygen and water as starting materials, characterized in that the starting materials are reacted in a vapor phase in a reactor of perfect mixing type to avoid local 30 heating, under a condition not to liquefy the starting materials and reaction products, while continuously supplying the starting materials and continuously withdrawing the reaction products, so as to obtain a reaction mixture comprising trifluoroacetyl chloride as the main product and trifluoroacetic acid as an accompanying product. Now, the present invention will be described in detail with reference to the preferred embodiments. 35 in the accompanying drawings. Figure 1 is a flow sheet illustrating one embodiment of the process for the vapor phase reaction of R — 123, oxygen and water. Figure 2 is a flow sheet illustrating one embodiment of the hydrolytic process to convert TFAC to TFA. The vapor phase reaction of R — 123, oxygen and water is represented by the following formula: 40 2CF3CHCI2 + 02 + H2O -» CF3COOH + CF3COCI + 3HCI

In the vapor phase oxidation reaction, the thermal decomposition reaction of R — 123 and various accompanying side-reactions are likely to take place, thus leading to the formation of e.g. HF. Further, during the preparation of R— 123 as the starting material, it is likely that CF2CICFHCI (R— 123a) as an isomer 45 of R— 123, which is hardly separable from R— -123, will be included in the starting material R— 123. In an extreme case, R— 123a will be included in an amount as high as 15% by weight. Consequently, hydrofluoric acid and hydrochloric acid are likely to form also by the oxidation reaction of R— 123a, as follows:

2CF2CICFHCI + O2 -» CF2CICOCl + CF2CIC0F + HF + HCI so On the other hand, in the case where TFA or TFAC is to be obtained by the oxidation of R — 123 (which usually contains a small amount of the isomer R— 123a as mentioned above), it is known that water functions catalytically, and in the absence of water, the oxidation reaction of R— 123 hardly takes place. However, the presence of water facilitates the corrosion of the apparatus by hydrofluoric acid or 55 hydrochloric acid formed as a by-product as mentioned above. Particularly, hydrofluoric acid is highly corrosive even in the absence of water, whereby the glass covering the radiation source as disclosed in Japanese Examined Patent Publication No. 24416/1983 will not be durable for use for a long period of time. -The same publication teaches that a glass or quartz light source will be damaged by hydrofluoric acid formed as a by-product during a liquid phase oxidation reaction of R — 123. The present inventors have - 60 found that the same applies to the vapor phase oxidation reaction. Thus, in the oxidation reaction of R — 123 where water is used catalytically, it is impossible to use active radiation or an industrial scale in which glass material not durable to corrosion is required. Even in the vapor phase oxidation reaction where the presence of water is limited to a minimum amount, it is likely that water precipitates during the reaction process, whereby corrosion by hydrofluoric acid can not be avoided. 65 Whereas, in the process of the present invention, no active radiation is required, and the entire reactor 0 163 975 may be made of, for instance, Hastelloy, whereby the danger of corrosion can be prevented, and an industrial operation for a long period of time is possible. Further, the presence of water is not required to be the minimum, since the danger of corrosion is minimum, and it is possible to improve the selectivity for TFA by adding water in an amount sufficient for the catalytic activity. 5 In the process of the present invention, the reaction is conducted under pressure at a high temperature of at least 200°C and at an extremely high rate with the retention time in the reactor of within 10 minutes. Accordingly, in order to increase the conversion and improve the selectivity for TFA and TFAC by suppressing side-reactions, it is important to uniformly mix the reactants and maintain the temperature and concentrations at constant levels. The oxidation reaction of R — 123 is an exothermic reaction wherein 10 water is used as a catalyst. Accordingly, local superheating is likely to occur in the reactor, and side- reactions are likely to take place due to e.g. the thermal decomposition, thus leading to a deterioration of the selectivity for TFA or TFAC. In order to avoid such local superheating, a stirrer may be provided in the reactor as shown at 3 in Figure 1. In a vertical reactor as shown at 1 in Figure 1, stirring vanes may be provided in one or a few vertically separated rows, and in a 50 liter reactor, for instance, stirring is is conducted at a speed of at least 100 rpm, preferably at least 150 rpm, whereby the heat can effectively be dissipated. In order to maintain the entire reactor to a constant temperature level, a jacket may be provided as shown at 2 in Figure 1 for the heat exchange with an external heat medium, or the heat exchange between the starting materials and the reaction products may also be employed. The reaction temperature in the vapor phase continuous reaction of the present invention is selected within a range of from 250 to 20 400°C, preferably from 260 to 320°C when a reaction pressure of from about 25 to about 35 kg/cm2 is employed. If the temperature is lower than the above range, the reaction rate tends to decrease, or in an extreme case, no reaction takes place. On the other hand, if the temperature exceeds the above range, side- reactions such as thermal decomposition reactions are likely to take place, such being undesirable. According to the process of the present invention, a reactor of perfect mixing type is employed, 25 whereby the temperature and concentration can be maintained at a constant level by the perfect mixing. For this purpose, in addition to the above-mentioned stirring and heat exchange operations, it is preferred to employ a method wherein the starting materials for the reaction are supplied to a lower portion of a vertical reactor as shown at 1 in Figure 1, and the reaction product is withdrawn from an upper portion. Further, as shown in Figure 1, R — 123 is preferably supplied at a position higher than the position for the 30 supply of oxygen or water, whereby R — 1 23 can more uniformly be mixed with oxygen and water, and thus the conversion of R — 123 and the selectivity will be improved. If the mixing of the starting materials is incomplete, unreacted R — 123 will accumulate, whereby there is a danger of explosion due to an instantaneous oxidation reaction of the large amount of accumulated R — 123. Also in this respect, it is important to conduct the mixing operation thoroughly. In order not to permit R — 123 to remain unreacted, 35 the amount of the oxygen relative to R — 123 should preferably be at least the theoretical amount, and it should preferably be not higher than two mols per mol of R — 123 to avoid explosion. Thus, the amount of oxygen supplied is selected within a range of from 0.5 to 2 mols, preferably from 1 to 2 mols, per mol of R— 123. The present inventors have found that if the starting materials or the reaction products are liquefied 40 even in a very small amount in the reactor, liquid drops will deposit on the wall of the reactor, and corrosive substances such as HCI or HF formed as by-products will be dissolved in the liquid drops and will corrode the wall of the reactor, thus leading to undesirable results. A metal chloride forms as the result of the corrosion of the wall of the reactor, and the chloride acts as a negative catalyst to adversely affect or terminate the oxidation reaction, whereby there is a possible danger of explosion by instantaneous 45 oxidation of unreacted R— 123. R— 123 as the starting material and HCI and HF formed as by-products are in a gaseous state at room temperature. Although the reaction temperature of the present invention is as high as about 300°C, the starting materials and reaction products are likely to be liquefied since the reaction pressure is as high as about 20 to about 40 kg/cm2. Particularly, water which is liquid at room temperature, is susceptible to liquefaction in the reactor. Accordingly, an excess supply of water should be avoided. In so the oxidation reaction of R— 123, water is believed not only to act as catalyst but also to have a function to hydrolyze trifluoroacetyl chloride formed by the oxidation of R — 123 and convert it to trifluoroacetic acid. Accordingly, the amount of water is preferably such that it is at least the minimum amount required for the catalyst and at most the amount where water does not liquefy and deposit on the wall of the reactor. The amount of the water is usually selected within a range of from 0.01 to 0.5 mol per mol of R— 123. It is 55 important not to permit the liquefaction of even a very small amount of the starting materials or the reaction products in the reactor, or to complete the oxidation reaction of the starting materials or disperse and withdraw the reaction products with the accompanying gas, prior to the deposition of the liquefied starting materials or reaction products onto the wall of the reactor. The liquefaction of the starting material gas can effectively be prevented by preheating it at a temperature of from 1 50 to 200cC prior to the supply so to the reactor. With respect to R — 123 which is supplied in the largest amount and thus is most likely to liquefy, it is preferred to supply to the reactor at a position higher than the position for the supply of oxygen and water, as shown in Figure 1 , and in the vicinity of vanes of the stirrer to well disperse and complete the oxidation reaction. For the oxidation reaction of R — 1 23 in a perfect mixing state as in the present invention where the temperature and concentration are constant, a vertical single-tower reactor for continuous 55 0 163 975 operation may be employed in which the retention time of the gas in the reactor will be from 2 to 20 minutes. The reaction mixture withdrawn from the reactor as shown at 4 in Figure 1, is subjected to a separation operation by distillation to obtain desired TFA and TFAC. TFAC can readily be hydrolyzed to TFA. 5 Accordingly, it is conceivable that in order to obtain only TFA in good yield, water may be added to the reaction mixture containing TFAC, in an excess amount required for the hydrolysis of TFAC to convert all TFAC to TFA. However, TFA forms an azeotropic mixture with water, and it is hardly separable by distillation. Thus, the above-mentioned operation in which unreacted water remains after the hydrolysis of TFAC, is not desirable. for to In view of such a problem, the present inventors have conducted extensive researches a process to efficiently convert TFAC to TFA, and have found the following interesting facts (1) and (2). (1) Although it is difficult to remove water from water-containing TFA by distillation, it is possible to obtain TFA which contains no substantial water, by contacting TFAC to water-containing TFA to consume water for the hydrolysis of TFAC. When hydrolyzed, TFAC is readily converted to TFA, and remaining TFAC 75 can readily be separated from TFA by the difference in the boiling points. (2) In the above (1), water-containing TFA can readily be converted to TFA which contains no substantial water. Thus, the operation for the conversion of all TFAC to TFA by reacting TFAC with an excess amount of water, i.e. the operation for the formation of water-containing TFA, is no longer disadvantageous. be 20 On the basis of these discoveries, the present inventors have found a process whereby only TFA can obtained in good yield. Namely, present invention also provides a process for producing trifluoroacetic acid, which comprises subjecting 1,1-dichloro-2,2,2-trifluoroethane, oxygen and a small amount of water to a vapor phase reaction to continuously obtain a reaction mixture comprising trifluoroacetyl chloride as the main product of 25 and trifluoroacetic acid as an accompanying product, reacting the reaction mixture with a large amount water without subjecting it to a separation operation, whereby the trifluoroacetyl chloride is hydrolyzed and converted to trifluoroacetic acid, and withdrawing this trifluoroacetic acid together with the above- mentioned trifluoroacetic acid as the accompanying product. The method for reacting the reaction mixture containing TFA and TFAC with a large amount of water in 30 without subjecting it to a separation operation, is preferably conducted by hydrolysis as shown Figure 2, .which comprises a step of converting all TFAC to TFA With an excess amount of water, and a step of removing water from the resulting water-containing TFA by means of TFAC. The reaction mixture supplied at 4 in Figure 2 is composed mainly of TFA, TFAC, hydrochloric acid and unreacted oxygen. All operations in the flow sheet shown in Figure 2 may be conducted at a normal 35 temperature under atmospheric pressure. The above-mentioned hydrochloric acid and oxygen supplied from 4, will be sent in a gaseous state, via a first conversion-to-acetic acid tower 1 1, a first separation tank 12, a conduit 16, a first cooling tower 13, a conduit 19, a second conversion-to-acetic acid tower 21, a second separation tank 22, a conduit 26 and a second cooling tower 23 and discharged out of the system at 29, and thus they will be separated from desired TFA. Gaseous components at room temperature under other than the 40 atmospheric pressure in a TFAC-containing reaction mixture obtained by a method oxidation reaction of R — 123, are likewise discharged via the same route as above. The rate of the hydrolysis of TFAC is faster than the reaction rate of these gases with water, whereby there is no possibility that these gases to be removed, will remain by being liquefied or hydrolyzed. TFAC to be hydrolyzed will pass on a gaseous state through the same route as the above-mentioned 45 hydrochloric acid, but it is entirely hydrolyzed to TFA until it passes through the second cooling tower 23. Water for the hydrolysis is continuously supplied in an excess amount relative to TFAC accompanied by e.g. hydrochloric acid, and TFAC is hydrolyzed in the second separation tank 22, and converted to a TFA solution. The converted TFA solution and the remaining unreacted water are recycled via conduits 24 and 25. Those recycled via the conduit 24 is introduced into the second cooling tower 23, where a very small be 50 amount of TFAC which was not hydrolyzed in the second separation tank 22 and which is likely to accompanied by e.g. hydrochloric acid, is converted to TFA by water in the TFA solution, and then returned to the second separation tank 22 via a conduit 27. TFA is liquid at room temperature under atmospheric pressure, and therefore is not likely to rise through a conduit 26 as accompanied by e.g. hydrochloric acid. However, if it is so accompanied, it will be liquefied in the second cooling tower 23 and returned to the 55 second separation tank 22 via the conduit 27, whereby TFA will not be discharged out of the system as a loss. On the other hand, those recycled via the conduit 25, is introduced to the second conversion-to-acetic acid tower 21, subjected to hydrolysis and returned to the second separation tower. Such a recycling operation is continuously conducted, whereby a TFA solution containing from 1 to 10% by weight of water will be accumulated in the second separation tower 22. Having thus described the flow of the right hand 60 side half of Figure 2 including the second conversion-to-acetic acid tower 21 , the second separation tank 22 and the second cooling tower 23, the entire flow will be referred to as step B. The TFA solution containing a very small amount of water filled in the second separation tank 22, is intermittently transferred to the first separation tank 12. The TFA solution containing a very small amount of water in the first separation tank 12, is recycled via conduits 14 and 15. The solution recycled via the 65 conduit 14 is introduced into the first cooling tower 13, where TFAC accompanied by e.g. hydrochloric acid 0 163 975 and not hydrolyzed in the first conversion-to-acetic acid tower 11 or the first separation tank 12, is converted to TFA by water in the TFA solution, and then returned to the first separation tank 12 via the conduit 17. Those recycled via the conduit 15 is introduced into the first conversion-to-acetic acid tower 11, subjected to the hydrolysis of TFAC in the reaction mixture 4, and then returned to the first separation tank s 12. The first cooling tower has a role of liquefying TFA and returning it to the first separation tank 12 in the same manner as the second cooling tower in the step B. Such a recycling operation is continuously conducted, whereby a TFA solution having a water content of about 0.01 % by weight will accumulate in the first separation tank 12. Having thus described the flow of the left hand side half of the Figure 2 including the first conversion-to-acetic acid tower 11, the first separation tank 12 and the first cooling tower 13, the io entire flow will be referred to as step A. TFAC which was not hydrolyzed, is transferred to the second conversion-to-acetic acid tower 21 in the step B via the conduit 19, and eventually converted entirely to TFA by an excess amount of water introduced through a conduit 30. To the second conversion-to-acetic acid tower, not only such TFAC, but also TFAC supplied from 4 in Figure 2 or the reaction mixture may be introduced. The TFA solution 15 containing from about 1 to about 10% by weight of water accumulated in the second separation tank 22, may be supplied into the first separation tank 12 via a conduit 18 after the TFA solution in the first separation tank 12 having a water content of about 0.01% by weight has been withdrawn to the distillation step via the conduit 28. The amount of the supply of the TFA solution containing about 1 to about 10% by weight of water into the first separation tank 1 2, may be determined based on the amount of TFA from the 20 hydrolysis of TFAC or the accumulated amount of TFA as the reaction product (hereinafter referred to as a freshly accumulated TFA amount). Namely, the amount of the supply is such that the first separation tank 12 is filled with a freshly accumulated TFA amount during a period of time in which the water content in the TFA solution in the first separation tank 12 changes, for instance, from 5% by weight to 0.01% by weight. Of course, it is not necessarily required to conduct the operation to such extent that the first separation tank is 25 filled with the liquid 100%, and the withdrawal to the distillation system may be operated when about 80% of the tank has been filled. The reaction mixture containing TFAC is continuously introduced into the first conversion-to-acetic acid tower. In the case where the water content in the TFA solution is large, the hydrolysis of TFAC is believed to take place primarily in the first conversion-to-acetic acid tower. As the water content decreases, 30 the hydrolysis of TFAC tends to occur in the first separation tank. In the case where the temperature of the TFAC-containing reaction mixture supplied from 4 is high the TFA solution is passed to the first conversion- to-acetic acid tower to conduct not only the hydrolysis but also the cooling operation. Otherwise, TFA in the first separation tank is likely to be vaporized by the supplied TFAC or its mixture and discharged from the step A. 35 The amount of water supplied from the conduit 30 is an amount required to certainly convert the entire amount of TFAC supplied from the step A to TFA. The position for the supply of water is not necessarily at the intermediate point between the second conversion-to-acetic acid tower and the second separation tank as shown in Figure 1, and water may be supplied from the upper portion of the second conversion-to-acetic acid tower. In any case, it is preferred to convert all TFAC to TFA with a minimum supply of water. The 40 water content in the TFA solution required not to let TFAC escape out of the system, is at least from 1 to 10% by weight. TFAC flowing from the conversion-to-acetic acid tower to the separation tank is preferably introduced deep into the TFA solution, while stirring the solution, in order to bring TFAC in good contact with water in the TFA solution. A packed tower is preferably employed as the conversion-to-acetic acid tower or the cooling tower, so that the contact of gas-liquid can adequately be conducted. 45 The above-mentioned step A means a step of obtaining TFA which contains no substantial water, and the step B means a step in which TFAC is reacted with an excess amount of water to hydrolyze all TFAC to TFA and thereby to obtain water-containing TFA. When the water-containing TFA obtained in the step B is used in the step A after the TFA containing no substantial water obtained in the step A was withdrawn, a water-removal operation will be conducted in this step A to obtain TFA containing no substantial water. so However, it is also possible that the water-containing TFA obtained in the step B is used in this step B without transferring it to the step A, and the supply of the reaction mixture containing TFAC is switched from the step A to this step B to conduct the reaction, whereby the water-removal operation may be conducted in the step B. In this case, in the step B, the operation for the step A is conducted, and at the same time, in the step A after the withdrawal of TFA containing no substantial water, the operation of the 55 step B is conducted. Namely, the step B described earlier is changed to the step A, whereby the water- containing TFA is, in effect, used in the step A without being transferred. Namely, the supply of the reaction .mixture containing TFAC is switched from the first conversion-to-acetic acid tower 1 1 in Figure 2 to the second conversion-to-acetic acid tower 21, whereby the earlier step A is used as a new step B, and the earlier step B is used as a new step A. 60 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 these specific Examples.

Example 1 Into a 50 liter vertical reactor as shown at 1 in Figure 1 equipped with a stirrer having vertically 65 separated two sets of stirring vanes as shown at 3 in Figure 1 and a jacket-type heat exchanger as shown at 0 163 975

2 in Figure 1, R— 123, water and oxygen were continuously supplied and reacted. The supply of R — 123 was 103 mol/hr. R — 123 was supplied to the reactor at a position lower than the position for the withdrawal of the reaction products and higher than the position for the supply of water and oxygen. These starting materials were supplied at a position in the vicinity of the lower stirring vanes. Further, R— 123 and water were preheated. The reaction condition, the conversion of R— 1 23 and the selectivity for TFA and TFAC are shown in Table 1. The conversion and selectivity were obtained by analyzing the reaction products by means of 19F— NMR and gas chromatography. The temperature difference in the reactor was determined as the difference in the temperature as between the center of the upper stirring vanes and the center of the lower stirring vanes. 10 Table 1

Examples 12 3 15 Molar ratio of water/R-123 0.1 0.2 0.075

Molar ratio of oxygen/R-123 1.0 1.0 1.0 20 Preheating temperature (°C) 180 175 180

Reaction temperature (°C) 300 260 300

25 Reaction pressure (kg/cm ) 30 30 30 Retention time (min. ) 8.4 7.2 8.4

Temperature difference 4 4 5 30 in the reactor (°C)

Rotational speed of the 150 120 160 stirring vanes (r.p.m.)

35 Liquid drops (mol/hr) 0 0 0

Conversion (%) 95 91 95

Selectivity for TFAC (%) 68 65 68 40 Selectivity for TFA (%) 26 28 24

45 Comparative Example 1 Into a Hastelloy C autoclave having an internal capacity of 200 cc and equipped with a mechanical stirring device, 10.5 g (0.067 mol) of R — 123 and 0.12 g (0.0067 mol) of water were charged, and heated to 290°C, whereby the pressure was 15 kg/cm2. Oxygen was supplied thereto and the pressure was raised to 30 kg/cm2 and maintained at that level for 5 minutes. Then, the content was collected in a trap cooled by 50 liquefied nitrogen. The trap was further immersed in a dry ice-ethanol bath to remove unreacted oxygen and the formed hydrochloric acid. Then, the reaction solution was analyzed by 19F— NMR and gas chromatography. As a result, it was found that the conversion of R — 123 was 52%, the selectivity for TFA was 22%, and the selectivity for TFAC was 68%.

55 Comparative Example 2 The reaction was conducted in the same manner as Comparative Example 1 except that the reaction time was extended to 8 minutes to increase the conversion of R — 123. As the result, it was found that the conversion of R — 123 was 53%, the selectivity for TFA was 20%,. and the selectivity for TFAC was 64%. Namely, there was no substantial change in the conversion, but the selectivity was poorer. 60 Example 2 Into a 50 liter vertical reactor equipped with a stirrer and a jacket-type heat exchanger, 103 mol/hr of CF3CHCI2, 10.3 mol/hr of H2O and 103 mol/hr of O2 were continuously supplied, and the continuous vapor phase reaction of the present invention was conducted. The reaction temperature was 300°C, the pressure 65 was 30 kg/cm2, and the retention time was 8.4 minutes. The reaction products thereby obtained were 0 163 975

analyzed by 19F— NMR and gas chromatography, whereby it was found that the conversion of CF3CHCI2 was 95%, the selectivity for CF3COOH was 26%, and the selectivity for CF3COCI was 68%. Then, the hydrolysis of the reaction products was conducted by two steps A and B. In the step A, 25.4 mol/hr of CF3COOH and 66.5 mol/hr of CF3COCI were continuously supplied in a recycling manner to 1197 mol of 5 CF3COOH containing 5% by weight of H20, and water removal was conducted, whereby the water content became not higher than 0.01% by weight upon expiration of 24 hours. On the other hand, in the step B, 1596 mol of H2O was used for the hydrolysis of CF3COCI which was continuously supplied from the step A in a recycling manner, whereby 1197 mol of CF3COOH containing 5% by weight of H20 was obtained after expiration of 24 hours. '0 The amount of CF3COCI which was not hydrolyzed in the step A and which was supplied to the step B, was almost negligible until the water content in CF3COOH in the step A reached about 1% by weight, and rapidly increased as the water content approached 0.01% by weight.

Example 3 '5 The reaction and analysis were conducted in the same manner as in Example 2 except that the amount of supply of H2O was changed to 20.6 mol/hr, the reaction temperature was changed to 260°C, and the retention time was changed to 7.2 minutes. As the results, it was found that the conversion of CF3CHCI2 was 91 %, the selectivity for CF3COOH was 28%, and the selectivity for CF3COCI was 65%. Then, the hydrolysis of the reaction products was conducted in two steps A and B. In the step A, 26.2 mol/hr of CF3COOH and 20 60.9 mol/hr of CF3C0CI were supplied continuously in a recycling manner to 858 mol of CF3C00H containing 10% by weight of H2O, and water removal was conducted, whereby the water content became not higher than 0.01 % by weight upon expiration of 24 hours. On the other hand, in the step B, 1462 mol of H20 was used for the hydrolysis of CF3COCI supplied continuously in a recycling manner from the step A, whereby 858 mol of CF3COOH containing 10% by weight of H2O was obtained upon expiration of 24 hours. 25 The amount of CF3COCI which was not hydrolyzed in the step A and which was supplied to the step B, was almost negligible until the water content in CF3COOH in the step A reached about 1 % by weight and rapidly increased as the water content approached 0.01 % by weight, in the same manner as in Example 2.

30 Claims

1. A process for producing trifluoroacetic acid and trifluoroacetyl chloride from 1,1-dichloro-2,2,2-tri- fluoroethane, oxygen and water as starting materials, characterized in that the starting materials are reacted in a vapor phase in a reactor of perfect mixing type to avoid local heating, under a condition not to 35 liquefy the starting materials and reaction products, while continuously supplying the starting materials and continuously withdrawing the reaction products, so as to obtain a reaction mixture comprising trifluoroacetyl chloride as the main product and trifluoroacetic acid as an accompanying product. 2. The process according to Claim 1, wherein the oxygen is supplied in an amount within a range of from 1 to 2 mols per mol of 1,1-dichloro-2,2,2-trifluoroethane. 40 3. The process according to Claim 1, wherein the water is supplied in an amount within a range of from 0.01 to 0.5 mol per moi of 1,1-dichloro-2,2,2-trifluoroethane. 4. The process according to Claim 1, wherein the reaction is conducted at a temperature within a range of from 260 to 320°C. 5. The process according to Claim 1, wherein the reaction is conducted under a pressure within a range 45 of from 25 to 35 kg/cm2. 6. The process according to Claim 1, wherein 1,1-dichloro-2,2,2-trifluoroethane and the water are preheated to a temperature within a range of from 150 to 200°C and then subjected to the reaction. 7. The process according to Claim 1, wherein the reactor of perfect mixing type is a vertical reactor equipped with a stirrer. so 8. The process according to Claim 1, wherein 1,1-dichloro-2,2,2-trifluoroethane is supplied to the reactor at a position lower than the position for the withdrawal of the reaction products and higher than the positions for the supply of oxygen and water. 9. The process according to Claim 7, wherein the position for the supply of 1,1-dichloro-2,2,2-trifluoro- ethane, the oxygen or the water to the reactor is in the vicinity of vanes of the stirrer. 55 10. A process for producing trifluoroacetic acid, which comprises subjecting 1,1-dichloro-2,2,2- trifluoroethane, oxgyen and a small amount of water to a vapor phase reaction to continuously obtain a reaction mixture comprising trifluoroacetyl chloride as the main product and trifluoroacetic acid as an accompanying product, reacting the reaction mixture with a large amount of water without subjecting it to a separation operation, whereby the trifluoroacetyl chloride is hydrolyzed and converted to trifluoroacetic so acid, and withdrawing this trifluoroacetic acid together with the above-mentioned trifluoroacetic acid as the accompanying product. 11. The process according to Claim 10, wherein the hydrolysis of the trifluoroacetyl chloride to trifluoroacetic acid is conducted in two steps A and B, said step A comprising contacting trifluoroacetyl chloride to water-containing trifluoroacetic acid to obtain trifluoroacetic acid containing substantially no 65 water, and said step B comprising reacting trifluoroacetyl chloride with excess water to obtain water- 0 163 975

containing trifluoroacetic acid, which is recycled for use in the step A. 12. The process according to Claim 11, wherein the water content of the water-containing trifluoro- acetic acid obtained in said step B is from 1 to 10% by weight. 5 Patentanspriiche

1. Verfahren zur Herstellung von Trifluoressigsaure und Trifluoroacetylchlorid aus 1,l-Dichlor-2,2,2- trifluorathan, Sauerstoff und Wasser als Ausgangsmaterialien, dadurch gekennzeichnet, daB man die Ausgangsmaterialien in einer Dampfphase in einem Reaktor vom Typ mit perfekter Vermischung umsetzt, to urn lokale Aufheizungen zu vermeiden, und zwar unter Reaktionsbedingungen, bei denen keine Verflussigung der Ausgangsmaterialien und Reaktionsprodukte stattfindet, wobei man die Ausgangsmaterialien kontinuierlich einspeist und die Reaktionsprodukte kontinuierlich abzieht, um auf diese Weise ein Reaktionsgemisch zu erhalten, welches Trifluoracetyl.chlorid als Hauptprodukt und Trifluor- essigsaure als ein Nebenprodukt enthalt. 15 2. Verfahren gemaB Anspruch 1, wobei der Sauerstoff in einer Menge im Bereich von 1 bis 2 Mol pro Mol des 1,1-Dichlor-2,2,2-trifluorathan eingespeist wird.. 3. Verfahren gemaB Anspruch 1, wobei das Wasser in einer Menge im Bereich von 0,01 bis 0,5 Mol pro Mol des 1,1-Dichlor-2,2,2-Trifluorathan eingespeist wird. 4. Verfahren gemaB Anspruch 1, wobei die Reaktion bei einer Temperatur im Bereich von 260 bis 320°C 20 durchgefiihrt wird. 5. Verfahren gemaB Anspruch 1, wobei die Reaktion unter einem Druck im Bereich von 25 bis 35 kg/ cm2 durchgefuhrt wird. 6. Verfahren gemaB Anspruch 1, wobei 1,1-Dichior-2,2,2-trifluorathan und das Wasser auf eine Temperatur im Bereich von 150 bis 200°C vorerhitzt werden und anschlieBend der Reaktion zugefiihrt 25 werden. 7. Verfahren gemaB Anspruch 1, wobei der Reaktor vom Typ mit perfekter Vermischung ein vertikaler Reaktor ist, der mit einem Ruhrer ausgrustet ist. 8. Verfahren gemaB Anspruch 1, wobei 1,1-Dichlor-2,2,2-trifluorathan in den Reaktor eingespeist wird an einer Position, die tiefer liegt als die Position fur das Abziehen der Reaktionsprodukte und hoher als die 30 Positionen fur das Einspeisen von Sauerstoff und Wasser. 9. Verfahren gemaB Anspruch 7, wobei die Position fur die Einspeisung des 1,1-Dichlor-2,2,2-trifluor- athan, des Sauerstoffs und des Wassers in den Reaktor in der Nahe der Ruhrerblatter liegt. 10. Verfahren zur Herstellung von Trifluoressigsaure, umfassend die Umsetzung von 1,1-Dichlor-2,2,2- trifluorathan, Sauerstoff und einer geringen Menge Wasser in einer Dampfphasenreaktion, um 35 kontinuierlich ein Reaktionsgemisch zu erhalten, welches Trifluoracetylchlorid als das Hauptprodukt und Trifluoressigsaure ais ein Nebenprodukt enthalt, Umsetzung des Reaktionsgemisches mit einer groBen Menge an Wasser, ohne es zuvor einer Trennoperation zu unterziehen, wobei das Trifluoracetylchlorid hydrolysiert wird und in Trifluoressigsaure umgewandelt wird, und Abziehen dieser Trifluoressigsaure zusammen mit der obenerwahnten als Nebenprodukt anfallenden Trifluoressigsaure. 40< 11. Verfahren gemaB Anspruch 10, wobei man die Hydrolyse des Trifluoracetylchlorids zu Trifluoressigsaure in zwei Stufen A und B durchfuhrt, wobei die erwahnte Stufe A die Kontaktierung des Trifluoracetylchlorids mit wasserhaltiger Trifluoressigsaure umfaBt, um Trifluoressigsaure zu erhalten, welche im wesentlichen kein Wasser enthalt und wobei die erwahnte Stufe B die Umsetzung von Trifluor- acetylchlorid mit uberschussigem Wasser umfaBt, um wasserhaltige Trifluoressigsaure zu erhalten, 45 welche fur die Verwendung in der Stufe A zuruckgefuhrt wird. 12. Verfahren gemaB Anspruch 11, wobei der Wassergehalt der wasserhaltigen Trifluoressigsaure, welche in der erwahnten Stufe B erhalten wird, von 1 bis 10 Gew.% betragt.

Revendications 50 1. Procede de fabrication d'acide trifluoracetique et de chlorure de trifluoracetyle a partir de dichloro- 1,1 trifluoro-2,2,2 ethane, d'oxygene et d'eau en tant que matieres de depart, caracterise par le fait que I'on fait reagir les matieres de depart, en phase vapeur, dans un reacteur du type a melangeage parfait pour eviter une surchauffe locale, dans des conditions a ne pas liquefier les matieres de depart et les produits de 55 la reaction, tout en introduisant en continu les matieres de depart et en soutirant en continu les produits de la reaction, de facon a obtenir un melange reactionnel comprenant du chlorure de trifluoracetyle en tant que produit principal et de I'acide trifluoracetique en tant que produit d'accompagnement. 2. Procede selon la revendication 1, dans lequel on introduit I'oxygene en une quantite se situant dans la plage de 1 a 2 moles par de dichloro-1,1 trifluoro-2,2,2 ethane. 60 3. Procede selon la revendication 1, dans lequel on introduit I'eau en une quantite se situant dans la plage de 0,01 a 0,5 mole par mote de dichloro-1,1 trifluoro-2,2,2 ethane. 4. Procede selon la revendication 1, dans lequel on conduit la reaction a une temperature se situant dans la plage allant de 260 a 320°C. 5. Procede selon la revendication 1, dans lequel on conduit la reaction sous une pression se situant 65 dans la plage de 25 a 35 kg/cm2. 0 163 975 6. Procede selon la revendication 1, dans lequel on prechauffe le dichloro-1,1 trifluoro-2,2,2 ethane et I'eau, a une temperature se situant dans la plage de 150 a 200°C, puis on les soumet a la reaction. 7. Procede selon la revendication 1, dans lequel le reacteur du type a melangeage parfait est un reacteur vertical equipe d'un agitateur. 5 8. Procede selon la revendication 1, dans lequel on introduit le dichloro-1,1 trifluoro-2,2,2 ethane dans le reacteur en une position inferieure a la position de soutirage des produits de la reaction et superieure aux positions d'introduction de I'oxygene et de I'eau. 9. Procede selon la revendication 7, dans lequel la position d'introduction du dichloro-1,1 trifluoro-2,2,2 ethane, de I'oxygene ou de I'eau dans le reacteur se situe au voisinage de pales de I'agitateur. 10 10. Procede de fabrication d'acide trifluoracetique, qui consiste a soumettre du dichloro-1,1 trifluoro- 2,2,2 ethane, de I'oxygene et une petite quantite d'eau a une reaction en phase vapeur, afin d'obtenir en continu un melange reactionnel comprenant du chlorure de trifluoracetyle en tant que produit principal et de I'acide trifluoracetique en tant que produit d'accompagnement, a faire reagir le melange reactionnel avec une grande quantite d'eau sans le soumettre a une operation de separation, ce par quoi le chlorure de 15 trifluoracetyle est hydrolyse et converti en acide trifluoracetique, et a soutirer cet acide trifluoracetique conjointement avec I'acide trifluoracetique mentionne ci-dessus en tant que produit d'accompagnement. 11. Procede selon la revendication 10, dans lequel on conduit I'hydrolyse du chlorure de trifluoracetyle en acide trifiuoracetique en deux etapes A et B, ladite etape A consistant a mettre en contact le chlorure de trifluoracetyle avec de I'acide trifluoracetique contenant de I'eau, afin d'obtenir de I'acide trifluoracetique 20 ne contenant sensiblement pas d'eau, et ladite etape B consistant a faire reagir le chlorure de trifluoracetyle avec de I'eau en exces, afin d'obtenir de I'acide trifluoracetique contenant de I'eau, qui est recycle pour etre utilise a I'etape A. 12. Procede selon la revendication 11, dans lequel lateneuren eau de I'acide trifluoracetique contenant de I'eau obtenu a ladite etape B va de 1 a 10% en poids. 25

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