U.S. patent application number 15/800599 was filed with the patent office on 2018-03-01 for process for the preparation of fluoroolefin compounds.
The applicant listed for this patent is Arkema France. Invention is credited to Jean-Michel BOSSOUTROT, Pierre-Marie SEDAT.
Application Number | 20180057432 15/800599 |
Document ID | / |
Family ID | 40999895 |
Filed Date | 2018-03-01 |
United States Patent
Application |
20180057432 |
Kind Code |
A1 |
SEDAT; Pierre-Marie ; et
al. |
March 1, 2018 |
PROCESS FOR THE PREPARATION OF FLUOROOLEFIN COMPOUNDS
Abstract
The subject of the invention is a process for the preparation of
fluoroolefin compounds. It relates more particularly to a process
for manufacturing a (hydro)fluoroolefin compound comprising (i)
bringing at least one compound comprising from three to six carbon
atoms, at least two fluorine atoms and at least one hydrogen atom,
provided that at least one hydrogen atom and one fluorine atom are
located on adjacent carbon atoms, into contact with potassium
hydroxide in a stirred reactor, containing an aqueous reaction
medium, equipped with at least one inlet for the reactants and with
at least one outlet, in order to give the (hydro)fluoroolefin
compound, which is separated from the reaction medium in gaseous
form, and potassium fluoride, (ii) bringing the potassium fluoride
formed in (i) into contact, in an aqueous medium, with calcium
hydroxide in order to give potassium hydroxide and to precipitate
calcium fluoride, (iii) separation of the calcium fluoride
precipitated in step (ii) from the reaction medium and (iv)
optionally, the reaction medium is recycled after optional
adjustment of the potassium hydroxide concentration to step
(i).
Inventors: |
SEDAT; Pierre-Marie;
(Fleurieux sur l'Arbresle, FR) ; BOSSOUTROT;
Jean-Michel; (Chaponost, FR) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Arkema France |
Colombes |
|
FR |
|
|
Family ID: |
40999895 |
Appl. No.: |
15/800599 |
Filed: |
November 1, 2017 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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15337052 |
Oct 28, 2016 |
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15800599 |
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14695210 |
Apr 24, 2015 |
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15337052 |
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13144239 |
Oct 3, 2011 |
9018429 |
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PCT/FR2010/050043 |
Jan 12, 2010 |
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14695210 |
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Current U.S.
Class: |
1/1 |
Current CPC
Class: |
B01J 19/0066 20130101;
C07C 17/25 20130101; B01J 2219/00761 20130101; B01J 19/18 20130101;
C07C 17/383 20130101; C07C 17/25 20130101; C07C 21/18 20130101;
C07C 17/383 20130101; C07C 21/18 20130101 |
International
Class: |
C07C 17/25 20060101
C07C017/25; C07C 21/18 20060101 C07C021/18; C07C 17/383 20060101
C07C017/383; B01J 19/00 20060101 B01J019/00; B01J 19/18 20060101
B01J019/18 |
Foreign Application Data
Date |
Code |
Application Number |
Jan 13, 2009 |
FR |
0950157 |
Claims
1-11. (canceled)
12. A process for the manufacture of a fluoroolefin comprising: (a)
dehydrofluorinating a fluoroalkane in the presence of KOH to
produce a fluoroalkene; (b) withdrawing a reaction stream
comprising spent KOH; and (c) recovering spent KOH.
13. The process of claim 12 wherein the fluoroalkane is comprised
of a compound of formula CF.sub.3CYRCR'X.sub.nH.sub.p, in which Y
represents a hydrogen atom or a halogen atom chosen from fluorine,
chlorine, bromine or iodine and X represents a halogen atom chosen
from fluorine, chlorine, bromine or iodine; n and p are integers
and may independently take the value zero, 1 or 2 provided that
(n+p)=2, and R represents a fluorine atom when R' represents a
hydrogen atom or R represents a hydrogen atom when R' represents a
fluorine atom.
14. The process of claim 13 wherein the fluoroalkane is
1,1,1,2,3,3-hexafluoropropane (HFC-236ea) or
1,1,1,2,3-pentafluoropropane (HFC-245eb).
15. The process of claim 12 wherein the fluoroalkene is comprised
of a compound of formula CF.sub.3CY.dbd.CX.sub.nH.sub.p in which Y
represents a hydrogen atom or a halogen atom chosen from fluorine,
chlorine, bromine or iodine and X represents a halogen atom chosen
from fluorine, chlorine, bromine or iodine; n and p are integers
and may independently take the value zero, 1 or 2 provided that
(n+p)=2.
16. The process of claim 15 wherein the fluoroalkene is
2,3,3,3-tetrafluoropropene (HFO-1234yf) or
1,2,3,3,3-pentafluoropropene (HFO-1225ye).
17. The process of claim 12 wherein the dehydrofluorination occurs
using a continuously stirred tank reactor.
18. The process of claim 12 wherein the spent KOH is withdrawn from
the reactor continuously or intermittently.
19. The process of claim 12 wherein the spent KOH is purified using
at least one separation method.
20. The process of claim 19 wherein the separation method is phase
separation.
21. The process of claim 12 further comprising, optionally,
concentrating the purified KOH and recycling it back to the
dehydrofluorination reaction.
22. The process of claim 12 wherein the reaction stream further
comprises KF.
23. The process of claim 22 further comprising converting KF to KOH
in the presence of Ca(OH).sub.2.
24. The process of claim 23 further comprising, optionally,
concentrating the converted KOH and recycling it back to the
dehydrofluorination reaction.
25. A process for the manufacture of a fluoroolefin comprising: (a)
dehydrohalogenating 1,1,1,2,3,3-hexafluoropropane (HFC-236ea) or
1,1,1,2,3-pentafluoropropane (HFC-245eb) in the presence of KOH to
produce 2,3,3,3-tetrafluoropropene (HFO-1234yf) or
1,2,3,3,3-pentafluoropropene (HFO-1225ye); (b) withdrawing a
reaction stream comprising spent KOH; and (c) recovering spent
KOH.
26. The process of claim 25 wherein the dehydrohalogenation occurs
using a continuously stirred tank reactor.
27. The process of claim 25 wherein the spent KOH is withdrawn from
the reactor continuously or intermittently.
28. The process of claim 25 wherein the spent KOH is purified using
at least one separation method.
29. The process of claim 28, wherein the separation method is phase
separation.
30. The process of claim 25 further comprising, optionally,
concentrating the purified KOH and recycling it back to the
dehydrohalogenation reaction.
31. The process of claim 25 wherein the reaction stream further
comprises KF.
32. The process of claim 31 further comprising purifying KF from
the reaction stream.
33. The process of claim 25 further comprising converting KF to KOH
in the presence of Ca(OH).sub.2, optionally, concentrating the KOH
and recycling it back to the dehydrohalogenation reaction.
34. A process for the manufacture of a fluoroolefin comprising: (a)
dehydrohalogenating a haloalkane in the presence of KOH to produce
a haloalkene; (b) withdrawing a reaction stream comprising spent
KOH; and (c) recovering spent KOH.
Description
CROSS REFERENCE TO RELATED APPLICATIONS
[0001] This application is a Continuation Application of U.S.
application Ser. No. 15/337,052, filed Oct. 28, 2016; which is a
Continuation Application of U.S. application Ser. No. 14/695,210,
filed Apr. 24, 2015, now abandoned; which is a Continuation
Application of U.S. application Ser. No. 13/144,239, filed Oct. 3,
2011, issued Apr. 28, 2015 as U.S. Pat. No. 9,018,429; which is a
National Phase Application of International Application No.
PCT/FR2010/050043, filed Jan. 12, 2010, which claims priority under
35 U.S.C. .sctn. 119 to French Patent Application No. FR0950157,
filed Jan. 13, 2009.
FIELD OF THE INVENTION
[0002] The subject of the invention is a process for the
preparation of fluoroolefin compounds. The invention relates more
particularly to a process for the preparation of
hydrofluoropropenes.
TECHNOLOGICAL BACKGROUND
[0003] Hydrofluorocarbons (HFCs) and in particular
hydrofluoroolefins (HFOs), such as 2,3,3,3-tetrafluoro-1-propene
(HFO-1234yf), are compounds known for their properties of
refrigerants and heat-exchange fluids, extinguishers, propellants,
foaming agents, blowing agents, gaseous dielectrics, polymerization
medium or monomer, support fluids, agents for abrasives, drying
agents and fluids for energy production units. Unlike CFCs and
HCFCs, which are potentially dangerous to the ozone layer, HFOs do
not comprise chlorine and thus do not present a problem for the
ozone layer.
[0004] 1,2,3,3,3-Pentafluoropropene (HFO-1225ye) is a synthetic
intermediate in the manufacture of 2,3,3,3-tetrafluoro-1-propene
(HFO-1234yf).
[0005] The majority of the processes for the manufacture of
hydrofluoroolefins involve a dehydrohalogenation reaction. Thus,
the document WO 03/027051 describes a process for the manufacture
of fluoroolefins of formula CF.sub.3CY.dbd.CX.sub.nH.sub.p, in
which X and Y each represent a hydrogen atom or a halogen atom
chosen from fluorine, chlorine, bromine or iodine and n and p are
integers and can independently take the value zero, 1 or 2,
provided that (n+p)=2, which comprises bringing a compound of
formula
CF.sub.3C(R.sup.1.sub.aR.sup.2.sub.b)C(R.sup.3.sub.cR.sup.4.sub.d),
with R.sup.1, R.sup.2, R.sup.3 and R.sup.4 independently
representing a hydrogen atom or a halogen atom chosen from
fluorine, chlorine, bromine or iodine, provided that at least one
of R.sup.1, R.sup.2, R.sup.3 and R.sup.4 is a halogen atom and that
at least one hydrogen atom and one halogen atom are situated on
adjacent carbon atoms, a and b being able independently to take the
value zero, 1 or 2, provided that (a+b)=2, and c and d being able
independently to take the value zero, 1, 2 or 3, provided that
(c+d)=3, into contact with at least one alkali metal hydroxide in
the presence of a phase transfer catalyst.
[0006] This document teaches, in Example 2, that, in the absence of
a phase transfer catalyst, there is no reaction when
1,1,1,3,3-pentafluoropropane (HFC-245fa) is brought into contact
with a 50% by weight aqueous potassium hydroxide (KOH) solution at
ambient temperature and under pressure for 24 hours.
[0007] In addition, this document teaches a reaction temperature of
between -20.degree. C. and 80.degree. C.
[0008] The document WO 2008/075017 illustrates the
dehydrofluorination reaction of 1,1,1,2,3,3-hexafluoropropane
(HFC-236ea) to give 1,2,3,3,3-pentafluoropropene (HFO-1225ye) at
150.degree. C. in the presence of a 50% by weight aqueous KOH
solution. In the absence of a phase transfer catalyst, the
conversion after 3 and a half hours is 57.8% and the selectivity
for HFO-1225ye is 52.4% (Test 1). In the presence of a phase
transfer catalyst, this conversion is reached after only 2.5 hours
and the selectivity is virtually unchanged (Test 4). As indicated
in Table 2 of this document, it is necessary to use an organic
solvent in order to increase the selectivity for HFO-1225ye.
[0009] WO 2007/056194 describes the preparation of HFO-1234yf by
dehydrofluorination of 1,1,1,2,3-pentafluoropropane (HFC-245eb)
either with an aqueous KOH solution or in the gas phase in the
presence of a catalyst, in particular over a catalyst based on
nickel, carbon or a combination of these.
[0010] The document Knunyants et al., Journal of the USSR Academy
of Sciences, Chemistry Department, "Fluoroolefin Reactions", Report
13, "Catalytic Hydrogenation of Perfluoroolefins", 1960, clearly
describes various chemical reactions on fluorinated compounds. This
document describes the dehydrofluorination of
1,1,1,2,3,3-hexafluoropropane (236ea) by passing through a
suspension of KOH powder in dibutyl ether, to produce
1,2,3,3,3-pentafluoro-1-propene (HFO-1225ye) with a yield of only
60%. This document also describes the dehydrofluorination of
1,1,1,2,3-pentafluoropropane (HFC-245eb) to give 2,3,3,3
-tetrafluoro-1-propene (HFO-1234yf) by passing into a suspension of
KOH powder in dibutyl ether with a yield of only 70%.
[0011] Furthermore, FIG. 2 on page 51 of Part 2 of the nouveau
traite de chimie mine rale [New Treatise on Inorganic Chemistry] by
P. Pascal, Ed. 1963, shows the appearance of the liquid/solid
equilibria of the water and potassium hydroxide system and the
measurements are collated in the Table on page 52.
[0012] The dehydrofluorination reactions such as described above
result, besides the desired hydrofluoroolefin compound, in the
formation of water and potassium fluoride. Furthermore, the
implementation of such a reaction in continuous mode is not easy on
an industrial scale since at least three phases (gas, liquid and
solid) are involved.
[0013] The present invention provides a process for the continuous
and semi-continuous manufacture of a (hydro)fluoroolefin compound
that makes it possible to overcome the aforementioned
drawbacks.
[0014] The subject of the present invention is therefore a process
for the continuous or semi-continuous manufacture of a
(hydro)fluoroolefin compound comprising (i) bringing at least one
compound comprising from three to six carbon atoms, at least two
fluorine atoms and at least one hydrogen atom, provided that at
least one hydrogen atom and one fluorine atom are located on
adjacent carbon atoms, into contact with potassium hydroxide in a
stirred reactor, containing an aqueous reaction medium, equipped
with at least one inlet for the reactants and with at least one
outlet, in order to give the (hydro)fluoroolefin compound, which is
separated from the reaction medium in gaseous form, and potassium
fluoride, (ii) bringing the potassium fluoride formed in (i) into
contact, in an aqueous medium, with calcium hydroxide in order to
give potassium hydroxide and to precipitate calcium fluoride, (iii)
separation of the calcium fluoride precipitated in step (ii) from
the reaction medium and (iv) optionally, the reaction medium is
recycled after optional adjustment of the potassium hydroxide
concentration to step (i).
[0015] The present invention thus makes it possible to obtain an
advantageous process since, on the one hand, potassium hydroxide is
more reactive than calcium hydroxide in the dehydrofluorination
reaction and, on the other hand, calcium fluoride is a reusable
by-product. The process according to the present invention
preferably provides a (hydro)fluoroolefin compound comprising three
carbon atoms, advantageously a (hydro)fluoroolefin compound
represented by the formula (I):
CF.sub.3CY.dbd.CX.sub.nH.sub.p (I)
in which Y represents a hydrogen atom or a halogen atom chosen from
fluorine, chlorine, bromine or iodine and X represents a halogen
atom chosen from fluorine, chlorine, bromine or iodine; n and p are
integers and may independently take the value zero, 1 or 2 provided
that (n+p)=2, by bringing a compound of formula
CF.sub.3CYRCR'X.sub.nH.sub.p, in which X, Y, n and p have the same
meaning as in formula (I) and R represents a fluorine atom when R'
represents a hydrogen atom or R represents a hydrogen atom when R'
represents a fluorine atom into contact with potassium
hydroxide.
[0016] The present invention is very particularly suitable for the
manufacture of a compound of formula (Ia):
CF.sub.3--CF.dbd.CHZ (Ia)
in which Z represents a hydrogen or fluorine atom, from a compound
of formula CF.sub.3CFRCHR'Z, in which Z has the same meaning as in
formula (Ia) and R represents a fluorine atom when R' represents a
hydrogen atom or R represents a hydrogen atom when R' represents a
fluorine atom.
[0017] Thus, 2,3,3,3-tetrafluoropropene may be obtained by
dehydrofluorination of 1,2,3,3,3-pentafluoropropane with KOH and/or
1,2,3,3,3-pentafluoropropene by dehydrofluorination of
1,1,1,2,3,3-hexafluoropropane with KOH. The
1,2,3,3,3-pentafluoropropene may be in the cis and/or trans isomer
form.
[0018] The present invention may also be used for the manufacture
of 1,3,3,3-tetrafluoropropene by dehydrofluorination of
1,1,3,3,3-pentafluoropropane with KOH.
[0019] In the remainder of the text, the limits of the
concentration and temperature ranges given are included in said
ranges.
[0020] In step (i) of the process according to the present
invention, the potassium hydroxide may represent between 10 and 90%
by weight relative to the weight of the water and KOH mixture
present in the aqueous reaction medium, preferably between 20 and
86% and advantageously between 55 and 75% by weight. Depending on
the content, the potassium hydroxide may be in the form of an
aqueous solution or in the molten state. This high KOH content
leads to an increase in the conversion rate of the
hydrofluoroalkane to hydrofluoroalkene. Moreover, due to this
concentrated KOH medium, the HF formed in (i) reacts immediately
with KOH to form KF that is less corrosive than HF, which makes it
possible to use, downstream of the dehydrofluorination reactor,
carbon steel reactors that are of low cost compared to reactors
made of an inert material (UB6 or Inconel) for the
dehydrofluorination reactor. Moreover, the "trapping" of HF in the
form of KF facilitates the separation of the various products from
one another (HF having a tendency to form azeotropes with
hydrofluoroalkanes and hydrofluoroalkenes), thus, a simple
distillation is sufficient to separate the products from one
another.
[0021] The step (i) is generally carried out at a temperature such
that the water formed during the dehydrofluorination reaction is
removed, partly or completely, from the reaction medium via
entrainment of the gas stream comprising the (hydro)fluoroolefin
compound from the stirred reactor. This temperature is preferably
between 80 and 180.degree. C., advantageously between 125 and
180.degree. C., and very particularly between 145 and 165.degree.
C. The evaporation of the water during step (i) is in the direction
of increasing the conversion rate of the hydrofluoroalkane to
hydrofluoroalkene.
[0022] The dehydrofluorination reaction of step (i) may be carried
out at atmospheric pressure, but it is preferred to work at a
pressure above atmospheric pressure. Advantageously, this pressure
is between 1.1 and 2.5 bar.
[0023] The reaction of step (ii) may be carried out in a stirred
reactor or fluidized bed reactor by reacting calcium hydroxide,
preferably in a suspension in water, with the potassium fluoride
from step (i). The reaction temperature may vary to a large extent
but for economic reasons, it is preferably between 50 and
150.degree. C., for example from 75.degree. C. to 120.degree. C.
and advantageously between 90 and 120.degree. C.
[0024] When a suspension of calcium hydroxide is used in step (ii),
the calcium hydroxide represents between 2 and 40% by weight
relative to the weight of the suspension.
[0025] Advantageously, step (ii) is carried out in the reaction
medium from step (i) comprising water, potassium hydroxide and
potassium chloride. The potassium fluoride originating from step
(i) and supplying step (ii) may be dissolved or in suspension.
[0026] The potassium hydroxide represents, in the reaction medium
of step (ii), preferably between 2 and 50% by weight relative to
the weight of the water and potassium hydroxide mixture of the
medium.
[0027] When the steps (i) and (ii) are carried out in separate
reactors, it is possible to provide a dilution step of the reaction
medium between step (i) and step (ii).
[0028] The calcium fluoride precipitated in step (ii) is separated
from the reaction medium, for example by filtration and/or
settling. Prior to the filtration, it is possible to provide a
settling step. The calcium fluoride thus separated is then washed
with water.
[0029] During the settling step, it is possible to make provision
for the recycling of a portion of the suspension that is
concentrated in calcium fluoride to step (ii). Advantageously, the
content of calcium fluoride solids present in the reaction medium
of step (ii) is between 5 and 40% by weight.
[0030] After separation of the calcium fluoride, the reaction
medium with or without the calcium fluoride washing waters may be
recycled to step (i) after optional adjustment of the potassium
hydroxide content.
[0031] According to one embodiment of the invention, steps (i) and
(ii) may be carried out in the same reactor.
[0032] It may be advantageous to use an inert gas, preferably
nitrogen or hydrogen in the dehydrofluorination step.
[0033] The process according to the present invention has the
advantage of resulting in high yields even in the absence of a
phase transfer catalyst and/or an organic solvent.
[0034] The present invention also comprises the combinations of the
preferred forms regardless of the embodiment.
EXPERIMENTAL SECTION
Example 1
[0035] FIG. 1 gives the diagram for one embodiment of the present
invention. A stirred reactor (1), made of nickel, equipped with a
device for heating and measuring the temperature of the reaction
medium, containing a mixture of water and of KOH, is continuously
fed with a solution of molten KOH (2) in which the KOH is present
at 60% by weight in the water, and with
1,1,1,2,3,3-hexafluoropropane (3). The temperature is kept at
160.degree. C. and the pressure in the reactor is 1.2 bar absolute.
The gaseous products exit the reactor via an orifice (4) located in
the cover of the reactor and the water contained in the gas stream
is removed by condensation (13). The outlet (5) of the reactor (1)
is connected to the inlet of the stirred reactor (6) and therefore
provides the reactor (6) with the supply of potassium hydroxide,
which may be in suspension in the aqueous medium. A 10% by weight
suspension of calcium hydroxide in water is introduced into the
reactor (6) via the line (7). The reactor (6) is kept at a
temperature between 100 and 120.degree. C.
[0036] The outlet of the reactor (6) is connected to a filter (8)
in order to separate the calcium fluoride from the reaction medium,
then wash it with water introduced via the line (9); the aqueous
medium separated from the calcium fluoride and also the calcium
fluoride washing waters are then recycled to the reactor (1) after
adjustment of the KOH concentration; the calcium fluoride is
recovered via the line (12).
[0037] The mixture of molten KOH supplying the reactor (1) is
prepared by heating (11) an aqueous solution of 50% by weight of
KOH introduced by the line (14) for the purposes of evaporation
(removal of water (15)).
Example 2
[0038] The procedure of example 1 is followed except that the
reactor (1) is continuously supplied with
1,2,3,3,3-pentafluoropropane instead of
1,1,1,2,3,3-hexafluoropropane.
[0039] By using a KOH content higher than that from the prior art,
improved conversion rates of the hydrofluoroalkane to
hydrofluoroalkene (therefore a better productivity), a reusable
produce, CaF.sub.2, and lower manufacturing costs of the
hydrofluoroalkene are obtained.
* * * * *