The invention relates to a process for the manufacture of 1-chloro-1,1-difluoroethane in the liquid phase by reacting hydrofluoric acid with 1,1,1-trichloroethane and/or 1,1-dichloro-1-fluoroethane. The selectively is improved by using a perfluoroalkanesulphonic acid, in particular trifluoromethanesulphonic acid, as a catalyst.

FIELD OF THE INVENTION 
The present invention relates to the manufacture of 1-chloro-1, 
1-difluoroethane, CF.sub.2 Cl--CH.sub.3, by the catalytic reaction of 
1,1,1-trichloroethane, CCl.sub.3 --CH.sub.3, with hydrofluoric acid, HF, 
in the liquid phase. 
BACKGROUND OF THE INVENTION 
1-Chloro-1, 1-difluoroethane is used particularly as an intermediate in the 
synthesis of 1,1-difluoroethylene, CF.sub.2 .dbd.CH.sub.2 (itself a 
monomer of increasing importance for the industrial production of 
fluorinated polymers), but also as an aerosol propellant. It is generally 
prepared by reacting 1,1,1-trichloroethane with hydrofluoric acid in the 
liquid phase. 
In a known process (German Patent No. 2,137,806), the reaction can be 
carried out without a catalyst provided the temperature is high 
(110.degree. C.) and there is a large excess of hydrofluoric acid (molar 
ratio HF/C.sub.2 H.sub.3 Cl.sub.3 between 15 and 30). This gives a 
substantial amount of 1,1,1-trifluoroethane as a by-product and results in 
a low productivity in terms of 1-chloro-1,1-difluoroethane. Furthermore, 
the entrainment of hydrofluoric acid by the hydrochloric acid formed in 
this chlorine .rarw..fwdarw. fluorine exchange reaction makes it necessary 
to use specially adapted equipment (under a sufficient pressure) to 
recover this expensive raw material. The patent mentioned above indicates 
that the use of HSO.sub.3 F results in the formation of tars, probably due 
to the chemical instability of this catalyst (oxidation by SO.sub.3). 
Other known processes recommend the use of catalysts based on antimony or 
molybdenum derivatives. See, for example, German Patent No. 2,659,046 and 
Japanese publication Nos. 74-03965, 76-29404 and 76-39606. 
The major disadvantage of antimony derivatives is the fact that they are 
rapidly deactivated by reduction to the lower oxidation state Sb.sup.3+. 
The answer to this, which consists of continuous oxidation of the catalyst 
(with chlorine), contributes to the formation of heavy compounds (derived 
from chlorination of the CH.sub.3 group of the 1,1,1-trichloroethane). 
Furthermore, the solubility of some catalytic species (for example 
SbF.sub.3) in the reaction medium is so low that it usually causes 
physical separation of this species and renders the action of the chlorine 
ineffective. As a result, the chemical reaction is non-uniform, a large 
amount of catalyst is consumed. There is sustained corrosion due to the 
formation of superacidic compounds which are very aggressive towards the 
reactor material. Finally, the difficulty of suitably controlling the 
catalytic activity leads to the undesirable formation of a substantial 
amount of 1,1,1-trifluoroethane as a by-product. 
With molybdenum derivatives, the formation of volatile species results in a 
loss of catalyst in the gas phase of the reactor. 
The preceding references are incorporated by reference. 
SUMMARY OF THE INVENTION 
It has now been found that it is possible to overcome these disadvantages 
and carry out the reaction with a reasonable excess of hydrofluroic acid 
(molar ratio HF/CH.sub.3 -CCl.sub.3 between 2 and 5) by using an acid 
catalyst which is soluble in the reaction medium and comprises a 
perfluoroalkanesulphonic acid CF.sub.3 --(CF.sub.2).sub.n --SO.sub.3 H, 
where n can range from 0 to 7 and is preferably equal to zero (triflic 
acid, CF.sub.3 --SO.sub.3 H). 
DETAILED DESCRIPTION OF THE INVENTION 
The catalyst according to the invention is advantageously used in an amount 
of 1 to 10 mol per 100 mol of 1,1,1-trichloroethane and preferably in an 
amount of 3 to 5 mol per 100. 
The process according to the invention can be carried out batchwise or 
continuously, at a temperature which ranges from 80.degree. to 150.degree. 
C. but is preferably around 100.degree.-110.degree. C. 
The batch process is carried out in a closed reactor into which all the 
reactants are introduced at the start of the operation and in which the 
autogenous pressure increases up to a maximum value. 
In the continuous process, the reactants are pumped into the reaction 
mixture containing the catalyst, with continuous recovery of the useful 
compounds (1-chloro-1,1-difluoroethane and hydrochloric acid) and 
condensation of the heavier compounds (catalyst, hydrofluoric acid, 
1,1,1-trichloroethane, 1,1-dichloro-1-fluoroethane). The total pressure is 
maintained at a given value by means of an appropriate regulating device. 
The working pressure must be sufficient (equal to at least 15 bar and 
preferably between 15 and 20 bar) to enable the hydrochloric acid to be 
separated out by distillation and to keep the reactants in the liquid 
state. 
The 1,1-dichloro- 1-fluoroethane formed is advantageously recycled for 
conversion to 1-chloro-1,1-difluoroethane.

EXAMPLES 
The examples below, in which the percentages indicated are expressed in 
mol, illustrate the invention without implying a limitation. 
EXAMPLE 1 
3.2 g of triflic acid, 71 g of 1,1,1-trichloroethane and 23.3 g of 
hydrofluoric acid are introduced successively into an 800ml stainless 
steel autoclave (NS 22 S) fitted with a stirring system of the magnetic 
bar type. 
With the stirrer running at about 700 rpm, the reaction mixture is heated 
to 100.degree. C. by means of a heat-transfer fluid circulating in the 
jacket of the reactor. The maximum autogenous pressure reaches 31.2 bar 
(i.e., about 32 bar of absolute pressure). 
After a reaction time of one hour under these conditions, the mixture is 
cooled, with stirring. About 50 minutes are required to reach room 
temperature. 
Analysis of the hydracids and the organic compounds in the reaction mixture 
gives the following results: 
degree of conversion of the 1,1,1-trichloroethane=92.6% 
degree of conversion of the CH.sub.3 --CCl.sub.3 
to CH.sub.3 --CF.sub.3 =0.07% 
to CH.sub.3 --CF.sub.2 Cl=12.3% 
to CH.sub.3 --CFCl.sub.2 =79.2% 
ratio CF.sub.3 --CH.sub.3 /CF.sub.2 Cl--CH.sub.3 =0.6% 
EXAMPLE 2 
Example 1 is repeated but without stirring. The maximum absolute autogenous 
pressure reaches 31 bar and the following results are obtained: 
degree of conversion of the CH.sub.3 --CCl.sub.3 =89% 
degree of conversion of the CH.sub.3 --CCl.sub.3 
to CH.sub.3 --CF.sub.3 =0.13% 
to CH.sub.3 --CF.sub.2 Cl=14.5% 
to CH.sub.3 --CFCl.sub.2 =71.7% 
ratio CF.sub.3 --CH.sub.3 /CF.sub.2 Cl--CH.sub.3 =0.9% 
This last ratio shows that it is preferable to carry out the reaction with 
stirring. 
EXAMPLE 3 
Example 1 is repeated but the molar ratio HF/CH.sub.3 --CCl.sub.3 is 
modified from 2.2 to 5 by using the following amounts of reactants: 
2.8 g of triflic acid 
61.8 g of 1,1,1-trichloroethane 
46.3 g of hydrofluoric acid 
In this experiment, performed under conditions identical to those of 
Example 1 (stirring at 700 rpm; 100.degree. C.), the maximum absolute 
autogenous pressure reaches 36 bar. The results obtained are as follows: 
degree of conversion of the CH.sub.3 --CCl.sub.3 =93.5% 
degree of conversion of the CH.sub.3 --CCl.sub.3 
to CH.sub.3 --CF.sub.3 =0.4% 
to CH.sub.3 --CF.sub.2 Cl=37.2% 
to CH.sub.3 --CFCl.sub.2 =52.6% 
ratio CH.sub.3 --CF.sub.3 /CH.sub.3 --CF.sub.2 Cl =1.1% 
COMATIVE EXPERIMENT NO. 1 
The procedure is the same as for Example 1 except that no catalyst is 
added. The amounts of reactants used are as follows: 
66.8 g of 1,1,1-trichloroethane 
21.9 g of hydrofluoric acid 
The maximum absolute autogenous pressure reaches 27 bar. The following 
results are obtained: 
degree of conversion of the CH.sub.3 --CCl.sub.3 =81.2% 
degree of conversion of the CH.sub.3 --CCl.sub.3 
to CH.sub.3 --CF.sub.3 =0.03% 
to CH.sub.3 --CF.sub.2 Cl=2.9% 
to CH.sub.3 --CFCl.sub.2 =78.0% 
ratio CH.sub.3 --CF.sub.3 /CH.sub.3 --CF.sub.2 Cl=1% 
Comparison of the results of this experiment with those obtained in Example 
1 shows that the catalyst according to the invention makes it possible to 
improve the selectivity in terms of CH.sub.3 --CF.sub.2 Cl, while the 
degree of conversion of CH.sub.3 --CCl.sub.3 to CH.sub.3 --CF.sub.2 Cl is 
four times greater. 
COMATIVE EXPERIMENT NO. 2 
This experiment is performed in the presence of SbCl.sub.5 as the catalyst 
and at a temperature of 65.degree. C. with the following reactants, 
introduced in the order indicated: 
6 g of SbC.sub.5 
66.8 g of CH.sub.3 --CCl.sub.3 
21.9 g of HF 
The results obtained after one hour and with stirring at 700 rpm (maximum 
absolute pressure reached: 36 bar) are as follows: 
degree of conversion of the CH.sub.3 --CCl.sub.3 =98.5% 
degree of conversion of the CH.sub.3 --CCl.sub.3 
to CH.sub.3 --CF.sub.3 =28.4% 
to CH.sub.3 --CF.sub.2 Cl=64.4% 
to CH.sub.3 --CFCl.sub.2 =1.7% 
ratio CH.sub.3 --CF.sub.3 /CH.sub.3 --CF.sub.2 Cl=44.1% 
Although carried out at a lower temperature, disfavoring the formation of 
CH.sub.3 --CF.sub.3, this experiment clearly shows the influence of the 
nature of the catalyst on the desired selectivity in terms of CH.sub.3 
--CF.sub.2 --Cl. 
Although the invention has been described in conjunction with specific 
embodiments, it is evident that many alternatives and variations will be 
apparent to those skilled in the art in light of the foregoing 
description. Accordingly, the invention is intended to embrace all of the 
alternatives and variations that fall within the spirit and scope of the 
appended claims.