Note: Descriptions are shown in the official language in which they were submitted.
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Process for Purificationof 1,1,1-Trifluoro-2-Chloroethane
The present application has been divided out of Canadian
Application Serial No. 2,066,017, filed April 14, 1992.
The present invention relates to a process for the
purification of 1,1,1-trifluoro-2-chloroethane.
The invention of the parent application relates to an
azeotropic mixture of hydrogen fluoride (hereinafter referred
to as "HF") and 1,1,1-trifluoro-2-chloroethane (hereinafter
referred to as "R-133a") and a process for the purification of
R-133a by removing HF from a mixture comprising HF and R-133a.
R-133a draws attention since it is one representative cooling
medium which can replace dichlorodifluoromethane. Also R-133a
is a suitable raw material of HFC-134a (1,1,1,2-
tetrafluoroethane) and it is a suitable raw material of
trifluoroethanol.
R-133a is generally produced by reacting a carbon
chloride such as trichloroethylene with HF. HF is removed
from a reaction mixture comprising HF and R-133a as main
components by washing the mixture with an aqueous solution.
This method is not the most suitable as a large amount of
alkali is required to neutralize the washing solution.
We found that a mixture comprising HF and R-133a as main
components is separated into two liquid phases, that is, an
upper liquid phase rich in HF and a lower liquid phase rich in
R-133a (a ratio HF/R-133a of the lower liquid phase is smaller
than that of the original mixture before the liquid
separation) when it is cooled to a temperature below 7°C, and
that HF and R-133a form an azeotropic mixture having a minimum
boiling point. The azeotropic mixture can be used as a reflux
during a distillation process in which HF and/or R-133a are
separated from a mixture comprising both, so that efficient
separation can be carried out.
In one aspect, the present invention provides a process
for the purification of one component of HF and R-133a by
cooling a mixture comprising HF and R-133a as main components
to a temperature below 7°C to separate out an upper liquid
phase rich in HF and a lower liquid phase rich in R-133a, and
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treating either liquid phase with a suitable operation, for
example distillation, adsorption, absorption and combinations
thereof, to remove preferentially the other component so that
the one component is concentrated relative to the other
component and preferably substantially separated from the
other component. Purification by concentrating one component
herein means that the concentration of one component of a
mixture comprising two components is increased relative to the
concentration of the other component of the mixture.
In one aspect, the parent invention provides an
azeotropic mixture having a minimum boiling point which
consists essentially of HF and R-133a. The boiling point of
the azeotropic mixture is about -2°C at atmospheric pressure.
In another aspect, the parent invention provides a
process for the purification of HF or R-133a by distilling a
mixture comprising HF and R-133a as main components,
preferably the upper liquid phase rich in HF or the lower
liquid phase rich in R-133a which may be obtained by the
process according to the method of the present invention
described just above so that an azeotropic mixture comprising
HF and R-133a is removed and HF or R-133a substantially free
from R-133a or HF is obtained.
Figure 1 shows a process flow sheet of one preferred
embodiment in which the present purification process is
carried out.
As described above, a two component system comprising HF
and R-133a has an azeotropic mixture having a minimum boiling
point, which azeotropic mixture was discovered by us for the
first time. When the mixture comprising HF and R-133a as the
main components is distilled at atmospheric pressure,
concentration of HF from a molar ratio HF/R-133a beyond about
65/35 is possible. In other words, at such a molar ratio, the
composition of a liquid phase is the same as that of the vapor
phase in equilibrium with the liquid phase. The molar ratio
HF/R-133a of the azeotropic mixture of the present invention
changes with system pressure. For example, when the system
pressures are 1.5 Kg/cm2G, 4.0 Kg/cm2G and 15 Kg/cm2G, the
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molar ratios (HF/R-133a) are about 60/40, about 55/45 and
about 45/55, respectively.
In addition, after cooling the mixture comprising HF and
R-133a and separation into the two phases, a concentration of
R-133a of the lower liquid phase is increased compared with
that before cooling. It has been found that when increased, a
R-133a concentration of the lower liquid phase deviates into a
R-133a concentration greater than that of the azeotropic
mixture.
Cooling the mixture comprising HF and R-133a produces the
lower liquid phase rich in R-133a and the upper liquid phase
rich in HF. Merely cooling the mixture provides the upper
liquid phase and the lower liquid phase each of which is rich
in either component compared with the original mixture before
the cooling. The concentration of R-133a in the lower liquid
phase may be further increased when the obtained lower liquid
phase is subjected to any suitable treatment, e.g. distil-
lation, extraction, absorption, adsorption or neutralization
with an alkali in which HF is preferentially removed so that
R-133a is concentrated and purified.
Since the upper liquid phase is rich in HF, it is
subjected to suitable treatment in which R-133a is
preferentially removed as in the case of the treatment of the
lower liquid phase so that HF is concentrated and purified.
Thus, mere cooling facilitates the first rough separation
step.
The temperature at which the mixture is cooled (cooling
temperature) is usually below 7°C. The mixture may not be
liquid-separated at a temperature above 7°C at any ratio of
HF/R-133a. The preferred cooling temperature is below 5°C.
At a temperature above 5°C, a composition of the upper liquid
phase is not so different from that of the lower liquid phase,
so that a density of the upper liquid phase is also not so
different from that of the lower liquid phase, which may make
the liquid separation insufficient. There is no specific
lower limitation of the cooling temperature, provided that the
temperature is higher than the solidification point of R-133a
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(about -100°C). Generally, the cooling temperature is
preferably above about -50°C. Operation at a temperature
below -50°C is uneconomical since much energy is required for
the cooling. The cooling temperature is more preferably in
the range of -20°C to 0°C.
HF may be separated from the mixture comprising R-133a
and HF by directly distilling the mixture using any type of
distillation apparatus. On such distillation, the azeotropic
mixture of HF and R-133a is used as a reflux returned to the
distillation apparatus during the distillation operation so
that a distillate of the azeotropic mixture is efficiently
obtained from the top of the distillation apparatus, and R-
133a substantially free from HF is obtained from the bottom of
the apparatus when the concentration of R-133a of the mixture
fed into the apparatus deviates into the R-133a concentration
greater than that of the azeotropic mixture.
The azeotropic distillation apparatus may be any type of
distillation apparatus which has conventional means necessary
for a usual distillation operation. For example, a
distillation column having trays or a packed column may be
preferably used. The azeotropic distillation may be carried
out in a continuous operation or in a batch operation.
In a preferred embodiment, the mixture comprising HF and
R-133a is cooled so that the mixture is divided into the upper
liquid phase rich in HF and the lower liquid phase rich in R-
133a, and then each liquid phase is subjected to the
azeotropic distillation separately. The upper liquid phase is
divided into a distillate of the azeotropic mixture of R-133a
and HF distilled from the top of the distillation apparatus
and the rest of the HF substantially free from R-133a is
withdrawn as a bottom product from the apparatus, provided
that the HF concentration of the upper liquid phase deviates
into a HF concentration which is greater than that of the HF
concentration of the azeotropic mixture. Since the R-133a
concentration of the lower liquid phase deviates into the R-
133a concentration which is larger than that of the azeotropic
mixture, the lower liquid phase is divided into a distillate
CA 02361985 2001-11-08
of the azeotropic mixture of R-133a and HF distilled from the
top of the other distillation apparatus and the rest of R-133a
substantially free from HF withdrawn as a bottom product from
the apparatus. The present invention is useful for the
5 removal of HF from a mixture produced in a reaction of
trichloroethylene with HF in a liquid phase or in a vapor
phase in the presence of a catalyst. One preferred embodiment
of the present invention will be explained below.
Figure 1 shows a flow sheet of one example of a preferred
purification plant which may be used in the present invention.
Usually the mixture obtained from the reaction is withdrawn in
a gaseous phase form. The mixture comprises R-133a, HF and
hydrogen chloride in addition to small amounts of organic
substances. Hydrogen chloride is removed from the mixture by
distillation. Then, the mixture is cooled to a temperature
below 7°C, preferably below 5°C, more preferably below
0°C
through a cooler and passed to a liquid phase separation
device 1, e.g. a decanter to form the two liquid phases.
There is R-133a substantially free from HF at the bottom of
the distillation apparatus 3, which may be withdrawn as a
bottom product.
On one hand, the lower liquid phase rich in R-133a from
the separation device 1 is supplied to a distillation
apparatus 3 and an azeotropic mixture 5 is distilled from the
top of the apparatus 3. During such distillation, a portion
of the distilled azeotropic mixture is returned, as a reflux,
to the top of the apparatus 3. The rest of the distillate is
passed to the liquid separation device 1 after cooling to a
temperature below 7°C at a cooler 11 and then the above
procedures were repeated. There remains R-133a substantially
free from HF at the bottom of the distillation apparatus 3,
which is withdrawn as a bottom product 9.
On the other hand, the upper liquid phase rich in HF in
the liquid separation device 1 may be returned to any reaction
system, if possible. Alternatively, it may be distilled in
the other distillation apparatus. In Figure 1, the upper
liquid phase is supplied to another distillation apparatus 23
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where it is divided into an azeotropic distillate 2 of HF and
R-133a and a bottom product 29 of HF substantially free from
R-133a. A portion of the distillate is returned, as a reflux
27, to the top of the distillation apparatus 23 as in the case
of distillation apparatus 3. The rest of the distillate is
cooled to a temperature below 7°C at a cooler 31 and then
returned to the liquid separation device 1. The bottom
product 29 substantially free from R-133a may be reused.
As described above, all HF is utilized while R-133a is
purified. These procedures may be carried out in a continuous
or a batch mode.
The invention will be further explained with reference to
some Examples below. The invention should not be construed to
be limited to the Examples.
Example 1
HF (40 g, 2.0 mol) and r-133a (592.5 g, 5.0 mol) were
charged into an evacuated packed column (diameter: 25 mm,
packing: McMahon packing, effective packing height: 1500 mm)
made of stainless steel. Distillation was started from a
total reflux condition and the temperature of the still
(bottom) was raised gradually. When the pressure at the top
of the column came to 1.5 Kg/cm2G and the temperature at the
top came to 19°C, a first sample was obtained from a reflux
line. The first sample was analyzed for the molar ratio of
HF/R-133a and the ratio was found to be 58/42.
The temperature of the still was raised again at the
total reflux condition, and a second sample was obtained from
the reflux line when the top pressure and the temperature cam
to 4.0 KG/cm2G and 40°C, respectively. The molar ratio of
HF/R-133a of the second sample was 55/45.
From these results, HF having its normal boiling point of
19°C higher than that of R-133a of 7°C is concentrated toward
the top of the distillation apparatus, which means that R-133a
and HF form the azeotrope mixture.
Example 2
A mixture (60 g) having the same composition as that of
the mixture of the first sample of Example 1 was charged in an
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evacuated vapor-liquid equilibrium measuring apparatus made of
stainless steel (effective volume of which was 75 ml) and
heated the whole apparatus so that a system pressure came to
1.5 KG/cm2G. After the system reached an equilibrium state,
samples were obtained from the liquid phase and the vapor
phase. (The sample from the vapor phase was obtained in the
form of liquid after condensation of the vapor phase.) As to
the second sample in Example 1, the same procedures were
repeated as in the case of the first sample except that the
system pressure has changed.
HF concentrations of the samples of each phase are shown
in Table 1. Thus, the concentration of R-133a is the balance
to make up 100 mol%.
Table 1
HF concentration Pressure
(mol%) Temperature
Sample Liquid Vapor Kg/cm2G C
Phase Phase
1 58 59 1.5 20
2 55 55 4.0 41
Clearly seen from the above date, the composition of the
liquid phase is substantially equal to that of the vapor phase
(within experimental error), and HF and R-133a form an
azeotropic mixture.
Example 3
HF and R-133a were charged into an evacuated vessel made
of a fluorine plastic at a molar ratio HF/R-133a of 60/40 and
then mixed together. The mixture was settled at 0°C to be
phase-separated. The molar ratio HF/R-133a of the separated
lower liquid phase was measured and found to be 30/70. The
molar ratio HF/R-133a of the upper liquid phase was also
measured and found to be 84/16.
Examples 4-6
Example 3 was repeated except that the phase separation
temperature was changed. The separation temperatures and the
molar ratio HF/R-133a of the lower phases are shown in Table 2
together with the results of Example 3.
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Table 2
Example Sep. Temp. HF/R-133a Ratio (lower phase)
3 0 30/70
4 -5C 20/80
5 -10C 10/90
6 5C 50/50
Note: Before the phase separation, the molar ratio
HF/R-133a was 60/40.
It is understood that the molar ratio HF/R-133a of the
lower liquid phase is remarkably reduced after the phase
separation.
Example 7
HF (150 g, 7.5 mol) and R-133a (592.5 g, 5.0 mol) were
charged into an evacuated vessel made of a fluorine plastic
(effective volume 1000 ml) and cooled to -20°C. After
cooling, the mixture of HF and R-133a was phase-separated into
a lower liquid phase and an upper liquid phase. The lower
phase recovered contained 1 g of HF (0.05 mol) and 435.5 g of
R-133a (3.68 mol). Thus, the molar ratio HF/R-133a was
1.34/98.66, and the concentration of R-133a greatly deviated
into the R-133a concentration which is greater than that of
the azeotropic mixture.
The recovered lower liquid phase (400 g) was charged in
the same distillation column as used in Example 1 and the
temperature of the column still was gradually raised to a
total reflux condition. When the top pressure of the column
reached 1.5 Kg/cmzG and the top temperature of the column
reached 20°C, a first distilled sample was obtained (2 g) from
the top of the column (reflux line), which was analyzed on its
HF/R-133a ratio. The molar ratio was found to be 60.8/39.2.
The still temperature was further raised until the top
pressure and the top temperature reached 4.0 Kg/cm2G and 41°C,
respectively. Then, another distillate sample was obtained
(2 g). The molar ratio HF/R-133a of the second sample was
found to be 56.6/43.4.
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' The system pressure was adjusted to 1.5 Kg/cmzG, again and
the distillation column was stabilized at a total reflux
condition. After the stabilization, when distillate was
withdrawn from the top of the column little by little, the top
temperature started to rise. When the top temperature became
equal to the still temperature, heating was stopped. The
total amount of the distillate withdrawn from the top was 20 g
(including amounts of the samples on the way) and about 380 g
of R-133a containing about 10 ppm of HF was obtained as the
bottom product from the still.
Example 8
HF (150 g, 7.5 mol) and R-133a (592.5 g, 5.0 mol) were
charged into an evacuated vessel made of a fluorine plastic
(effective volume 1000 ml) and cooled to -20°C. After
cooling, the mixture of HF and R-133a was liquid-separated
into a lower liquid phase and an upper liquid phase, and the
upper phase recovered contained 149 g of HF (7.45 mol) and
157 g of R-133a (1.32 mol). Thus, the molar ratio HF/R-133a
was 84.95/15.05, and the concentration of HF greatly deviated
into the HF concentration which is larger than that of the
azeotropic mixture.
The recovered upper liquid phase (300 g) was charged in
the same distillation column made of stainless steel as used
in.Example 1 and the temperature of the column still was
gradually raised to the total reflux condition. When the top
pressure of the column reached 1.5 Kg/cm2G and the top
temperature of the column reached 20°C, a first distillate
sample was obtained (2 g) from the reflux line, which was
analyzed for its HF/R-133a ratio. The molar ratio was found
to be 59.5/40.5.
The still temperature was further raised until the top
pressure and the top temperature reached 4.0 Kg/cmzG and 40°C,
respectively. Then, another distillate sample was obtained
(2 g). The molar ratio HF/R-133a was found to be 57.5/42.5.
The system pressure was adjusted to 1.5 Kg/cmzG, again and
the distillation column was stabilized at the total reflux
condition. After the stabilization, when distillate was
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withdrawn from the top of the column little by little, the top
temperature started to rise. When the top temperature became
equal to the still temperature, heating was stopped. The
total amount of the distillate withdrawn from the top was
5 about 240 g (including amounts of the samples on the way) and
about 60 g of HF containing a trace amount of R-133a was
obtained as the bottom product from the still.
