Note : Les descriptions sont présentées dans la langue officielle dans laquelle elles ont été soumises.
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This invention relates to the removal of hydrogen fluoride
(HF) gas from gaseous mixtures containing up to about 20% of HF,
based on the weight of the gaseous mixture, and other gases inert
to alkaline earth metal fluorides, in the absence of water. The
gaseous mixture is passed in contact with particulate, anhydrous
alkaline earth metal chloride in the absence of water. Preferably,
the anhydrous alkaline earth metal chloride is fluorinated by con-
tact with a dry gaseous mixture inert to alkaline earth metal chlo-
ride except for a minor proportion of HF therein. Alternatively,
a dry gas containing at least a major proportion of HF or a dry
fluorine gas can be used to obtain the particulate, anhydrous
alkaline earth metal fluoride employed in the process of this in-
vention.
After absorbing HF gas in an amount ranging up to the ab-
sorption capacity of the specified anhydrous alkaline earth metal
fluoride, the flow of the gaseous mixture is terminated or diverted
and the absorbed HF is removed from the alkaline earth metal fluo-
ride, preferably by desorption with heat. The regenerated alka-
line earth metal fluoride is then reused in the HF removal process.
Liquids, other than aqueous liquids, can be tolerated in the gaseous
mixture as long as they do not collect in the process vessels in
amounts sufficient to obscure significant amounts of the surface
area of the absorption material.
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The term "absorption" is used herein to include chemi-
sorption, adsorption and absorption although the term "absorption"
will be used hereinafter to describe the process.
The alkaline earth metal compounds employed for this in-
vention are the calcium, barium or strontium chlorides and fluo-
rides in their anhydrous form. Calcium is the preferred alkaline
earth metal and will be primarily used hereinafter to further de-
monstrate the invention. The anhydrous forms of alkaline earth
metal chlorides are prepared by drying the hydrates at temperatures
suitable to remove water of hydration.
The gaseous mixtures included herein which contain HF in
amounts up to about 20%, based on the weight of the gaseous mixture,
and other gases inert to alkaline earth metal fluorides include
mixtures of HF, hydrvgen chloride (HCl) and volatile organic gases
obtained from various manufacturing processes; HF and HCl mixtures
substantially free of other gases; HF and fluorine gas with and
without other inert gases; dry air containing traces of HF; waste
gases from petroleum alkylation processes involving anhydrous HF;
waste gases in the aluminum metal and ceramic industries containing
traces of HF; etc.
The process of this invention is especially useful for the
treatment of HF - contaminated gaseous hydrogen chloride encounter-
ed as a by-product in fluorinated hydrocarbon synthesis. More
specifically, in commercial process for the production of fluorin-
ated hydrocarbons (such as CC13F, CC12F2, CClF3, CHC12F, CHClF2, CHF3
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105'~Z9;2
CH3CClF2, CH3CC12F, CH3CF3, CC12FCClF2, CClF2CClF2, and the like
which products are useful as refrigerants, blowing agents and
aerosol propellants) involving the fluorination with HF of chlorin-
ated hydrocarbons, such as CC14, CHC13, CH3CC13, and CC12 -CC12, a
large amount of hydrogen chloride containing varying but signifi-
cant proportions of hydrogen fluoride is obtained as a by-product,
which hydrogen chloride by-product cannot be discarded for obvious
economical and ecological reasons. However, this contaminated
hydrogen chloride must be purified so that the HCl can be used in
industrial applications, for example, in oxychlorination reactions,
food processing, pickling of steel, and in the treatment of brine
used in electrolytic chlorine production, the presence of HF in such
systems being intolerable.
F. R~ Lowdermilk, U. S. ~atent 3,140,916, has suggested
one method of removing HF contamination wherein a gaseous mixture of
hydrogen chloride and hydrogen fluoride is passed through an aqueous
solution of calcium chloride, whereby the hydrogen fluoride reacts
with the calcium chloride in solution to form calcium fluoride as
a precipitated solid that is recoverable by filtration. This multi-
step aqueous technique has several serious disadvantages stemmingfrom the problems in dealing with an aqueous system comprised of
HCl, CaC12, and CaF2. This mixture is highly corrosive and the
precipitated CaF2-in-water mixture forms an abrasive slurry, both
conditions being very injurious to plant equipment. Lowdermilk
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also mentions that aluminum oxide has been used as an absorption
agent for removal of HF from HCl.
A simple and economical process for removing HF impurity
from a gaseous mixture of hydrogen chloride has been disclosed in
D. R. Merchant's Canadian Patent 991,822. This patent concerns
the method of passing gaseous HCl containing HF in contact with
substantially anhydrous, solia, particulate calcium chloride. It
was noted, during the operation of this process, that the calcium
fluoride, obtained in situ therein via the conversion of CaC12, is
endowed with the capability to absorb up to somewhat over 50% of
its own weight of HF. Moreover, this calcium fluoride maintains
the size, shape, appearance, free-flowing and other easy-handling
characteristics of the precursor calcium chloride.
W. L. Colvin, in AEC Report K 1117, discloses the use of
calcium fluoride as a sorbent for hydrogen fluoride, the said calcium
fluoride being prepared by direct fluorination of calcium sulfate.
However, he only observed a very low loading for the level break-
through of HF. With the present invention, an average loading of
about 20% of HF on CaF2 under normal operation is obtained.
Colvin likewise reports a surface area of 129 square meters/
gram for his material. This calcium fluoride material employed
herein has surface area of about 12-17 square meters/gram. Thus,
the process of this invention provides the unobvious and unexpected
result of removing more HF per unit weight of absorbent with consid-
lOS~Z92
erably less surface area.
Laboratory tests showed that naturally occurring calcium
fluoride does not have the ability to absorb a significant amount
of HF. Naturally occurring calcium fluoride could absorb only
5 to 6% by weight HF before breakthrough while the calcium fluoride
made by reacting calcium chloride and HF can absorb about 20%
HF by weight before breakthrough under the same conditions of flow,,
temperature and pressure.
The term "breakthrough", as used herein, is explained as
follows:
When HF is being absorbed by passing a gas containing
lt through an absorption medium, the outlet conc,entration of HF
in the gas is generally fairly uniform or increasing at a slow rate.
When the outlet concentration of HF in the gas begins to increase
at a rapid rate (as compared to previous rates), "breakthrough"
has occurred.
Table I below summarizes measurement made on the surface
area and absorption of HF on calcium fluoride (CaF2) prepared by
passing anhydrous HF through a bed of anhydrous calcium chloride
(CaC12) in the absence of water until the CaC12 was converted to
CaF2 as determined by analysis of the solids. The absorbed HF
was then desorbed by heat and air purge.
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TABLE I
PHYSICAL DATA
SPECIFIC % HF
SURFACE AREA ABSORBED
SAMPLE COMPOUND SQ. METERS/GRAM~ ON CaF2
I CaF2 13.5 40
II CaF2 16.5 40
III CaF2 (natural 1.8 10
fluorspar)
IV CaC12 2.0 ~ -
(anhydrous)
- Determined by the American Chemical Societies B. E. T.
Method (Brunauer, Emmet & Teller)
These results show a marked change in physical structure
of the compound CaC12 when reacted with HF to form CaF2. Also
shown in Sample III is natural fluorspar, CaF2. Its surface area
is on the order of that of the CaC12. It absorbed only 10% HF un-
der the same conditions as Samples I and II.
The HF absorbed by the "synthetic" calcium fluoride produced
as above described can be stripped off by suitable heating means,
and the thus regenerated CaF2 will again serve as an absorbent for
additional HF present in the gaseous mixture.
The HF containing gaseous mixture treated in accordance
with this invention to effect HF removal may contain from 0.3 to
about 20 weight percent HF, based on total weight of the gaseous
`` lOS;~Z9Z
mixture. The regenerative-recycle system embodied herein is par-
ticularly suited, however, to those mixtures containing moderately
large amounts of HF, e.g., from about 0.5 to about 6~0 weight
percent. In a more useful application of this process, there may
be present in admixture with an HF-containing gaseous hydrogen
chloride mixture up to about 70 but preferably up to about 60 weight
percent, based on the total weight of the gaseous mixture, of one
or more volatile halogenated hydrocarbons, i.e., chlorofluorohydro-
carbons, chlorohydrocarbons, and fluorohydrocarbons, for example,
CC14, CC13F, CC12F2, CClF3, CHC12F, CHClF2, CHF3, CHC13, CH3CClF2,
CH3CC12F, CC12FCClF2, CClF2CClF2, CC12CC12, and the like. Such
volatile halogenated hydrocarbons do not interfere with the HF
absorption and undergo no discernible change from contact with the
CaF2. The product HCl can be separated from these organic constit-
uents either by distillation to provide an anhydrous HCl gas or by
absorption in water to provide an aqueous HCl solution. In the
latter technique, the small amount of organic material that is
absorbed in the aqueous acid may be easily removed by blowing with
air or other gas or by absorption on activated carbon or molecular
sieves.
The absorption tower used in carrying out the process of
the invention can be initially charged with a suitable bed of
particulate CaF2 prepared from the substantially anhydrous calcium
chloride as described above, or in the preferred embodiment, is
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charged with the anhydrous CaC12 which is then normally converted
to the CaF2 when the feed stream of HF-containing gaseous HCl is
passed in contact therethrough. The particulate calcium fluoride
can range from powdery to granular type to pellets, that is, having
an average particle size over the broad range of 0.025 to 0.375
inch (0.0625 - 0.937 cm.). In the preferred embodiment, however,
the calcium fluoride is in pellet form, e.g., having a particle
size of from about 0.25 to about 0.375 inch (0.625 - 0.937 cm.).
The temperature at which the gaseous hydrogen chloride
mixture is contacted with the particulate CaF2 may be in the range
of about 60F (15.5C) to about 130F (54.5C), preferably from
about 70 F (21C) to 115 F (45C). It is desirable to maintain
the temperature of contact above the dew point of the gaseous mix-
ture to prevent any organics present therein from condensing in
the reactor column. Pressures may vary from essentially atmos-
pheric up to about 250 psig (18 atm.), depending on other process
conditions, Because the system is essentially anhydrous, exotic
materials of construction are not required and the absorption
tower and auxiliary piping and equipment can be of ordinary carbon
steel, corrosion thereof not being an abnormal problem.
The term "anhydrous" as used herein means a substance
containing less than 1000 and preferably less than 200 parts by
weight of water per million (p.p.m.~ parts of substance. Like-
wise, the term "in the absence of water" signifies a process carried
_ g _
~05'~Z9;~
out with a gas containing less than 1000 p.p.m. of water.
An advantage provided by this invention, in addition to
simplicity of operation and low operating costs, is the general
efficiency of absorption of HF, even at relatively high through-
put rates. For~example, afterlprocessing an HCl-organic gaseous
mixture originally containing about 18% HF in accordance with this
invention, the product gas will usually contain less than 0.05
weight percent HF, although flow rates of the feed gas may vary
over the range of from about 1.0 to about 100 pounds per hour per
square foot of particulate CaF2, measured at standard conditions
of 15 psia pressure and 70 F temperature. Stated in different
terms, the foregoing results of HF absorption are obtained using
periods of contact of the gaseous HCl mixture with the particulate
calcium fluoride (also referred to as retention time) of from 20
to about 600 seconds. The quality of the product gas (amount of
HF contamination) is, of course, influenced to some exten,t by these
flow rates.
The feed of the dry gaseous mixture to the particulate
CaF2 bed is continued until an appropriate amount of HF is absorbed
therein. This amount may be on the order of about 50% of the weight
of the CaF2 at the maximum; however, it is apparent that one factor
in absorption efficiency is the amount of free surface remaining
in the CaF2 solids; therefore, the operator who desires a compara-
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tively more pure HCl product can terminate the HCl gas feed, or
divert the feed to a fresh tower before the CaF2 has absorbed the
maximum amount. The so-called "spent" CaF2 solids are then regen-
erated by desorbing, that is, stripping the solids of absorbed HF.
This is conveniently accomplished by any of a number of conventional
methods: (1) external heating of the absorption column to around
225 to 350F; t2) heating the column to 200~F or higher and passing
an inert gas, r such as nitrogen, air or anhydrous HF through the
solids; or (3) passing an inert gas, heating to 350 F or higher,
through the solids. The desorbed HF is recovered and can be used
in hydrofluorination processes.
The "regenerated" bed of CaF2 solids after cooling is used
for another cycle of treatment of HF-containing gaseous mixtur~, and
after HF absorption has reached the desired level, as discussed above,
the regeneration cycle is repeated. The number of complete cycles
for which a specific CaF2 charge may be employed is limited by the
actual physical breakdown of the charge due to the heating and cool-
ing cycles. Therefore, the number of cycles is limited by the
allowable pressure drop of the system. At that point, the absorb-
ent CaF2 should be replaced with a fresh bed of the like or, prefer-
ably, substantially anhydrous, particulate CaC12. The spent CaF2
~OSZ~9Z
solids (which may have lost its good physical properties because of
physical degradation) is recovered from the bottom of the tower.
This can be used as a raw material for preparing hydrofluoric acid
in an H2SO4-reactor kiln.
The process of this invention is clarifled and illustrated
by the following examples:
Example I
A by-product gaseous mixture obtained from the process of
hydrofluorinating chloroform is comprised of hydrogen chloride con-
taining about 60% organics (halogenated hydrocarbons, mostly
CHClF2 with lesser amounts of CHC12F, CHC13 and CHF3) and 10.3%
hydrogen fluoride, based on the weight of HCl present. The gas
mixture is passed through a one inch diameter steel column filled
with 3.3 feet of particulate calcium fluoride, at 15 psia and 90 F,
superficial gas velocities ranging from 0.15 to 1.5 ft./min.,
equivalent to retention times on the order of 110 to 330 seconds?
The CaF2 has a particle size of 3/16" to 1/4" and is obtained from
the process of contacting anhydrous CaC12 of said particulate size
range with a stream of substantially the same composition as noted
above in the absence of water.
The HF content of the gaseous HCl mixture is reduced from
10.3~ to 0.38~, based on HCl content, equivalent to an HF removal
efficiency of 96.4~. A total of 0.36 cu. ft. of the feed gas is
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105'~Z9~2
passed through the bed until the HF absorbed therein is 14% by
weight. The calcium fluoride is regenerated (absorbed HF stripped
off) by heating the column to 350~F with electrical heating tape.
The CaF2 is then ready to treat further quantities of the feed HCl
gas mixture in like manner.
Example II
A by-product gaseous mixture obtained from the hydrofluor-
ination of methyl chloroform is comprised of HCl containing about
54~ volatile halogenated hydrocarbons (mostly CH3CClF2with lesser
amounts of CH3CC12F and CH3CF3) and 18~ HF, based on the weight of
the HCl. The gas mixture is passed through a two inch diameter
steel column containing a 2.6 ft. bed of CaF2 as embodied in this
invention. The CaF2 is made by passing the above described gaseous
mixture through anhydrous CaC12 of particle size 1/8" to 1/4"
diameter pellets. After the CaC12 is converted completely to CaF2,
the absorbed HF is driven off by suitable means and the CaF2 is
ready for reuse as an absorbent. Typical operating conditions
are as follows: pressure is 2 psig and the temperature of contact
about lOO~F. The system is subject to four cycles of operation,
the CaF2 being regenerated between the cycles by the method of
the previous example. The results are tabulated as follows:
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At the end of the fourth cycle, the CaF2 is removed from
the column as a free-flowing solid without any appreciable change in
size, shape or appearance.
EXAMPLE IV
A gaseous HCl mixture similar to that of Example II is
passed through a two ft. diameter column having a bed of 4.5 feet of
particulate CaF2 prepared by passing the gaseous HCl mixture similar
to that in Example II through anhydrous CaC12 until CaC12 is fully
converted to CaF2, then driving off the absorbed HF by suitable
means, leaving CaF2. Operation is at 100 F and 155 psig. Gas flow
ls 2 CFM with a velocity of about 0.6 ft./min. and a contact time of
450 seconds. Two cycles are run in the test with regeneration of the
CaF2 between cycles being accomplished by heating the column extern-
ally to 400F and passing a hot 350~F nitrogen purge through the
CaF2 to drive off absorbed HF. The results are summarized in the
following table:
- 15 -
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Example IV
The following table shows the results of a series of
absorption runs using a 6 inch diameter column by 5.5.ft. bed depth
of CaF2 operating on a mixture of HF, HCl, CH3CClF2, and other
chlorinated fluorocarbons in minor amounts or a mixture of HF, HCl,
CHClF2 and other chlorinated fluorocarbons in minor amounts. All
absorption tests were made on the same charge of CaF2.
- 17 -
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The data herein relating to HF content of gases and solids was
obtained by standard analytical techniques. The bed samples were
obtained by "coring" of the bed.
Example V
The following table shows the results of a series of absorp-
tion runs using a 2 ft. diameter column with a 4.5 ft. CaF2 bed
depth operating on the gases described in Example 4 above. All
absorption tests were made on the same charge of CaF2.
-- 19 --
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Example VI
Regeneration of the CaF2 used in the series of Example V
was performed as follows:
1. The 2 ft. diameter bed was heated to 350 F by applyin~
heat to the outside of the 2 ft. diameter column. They dry nitrogen,
at the rate of 1 SCFM per sq. ft. of bed area, was heated to 400F
by a tube heater and passed through the bed. The HF on the CaF2
was desorbed and collected in a chilled vessel. The CaY2 was com-
pletely desorbed with less than 0.5% HF on CaF2 remaining. This
method was used for the regenerations of the majority of the runs.
Another regeneration procedure is as follows:
2. The 2 ft. diameter CaF2 bed was heated externally by
applying heat to the outside of the 2 ft. diameter column, to 350F.
Then a vacuum of 25 inches of Hg was placed on the 2 ft. diameter
bed. The HF was desorbed from the CaF2 and recovered in a chilled
receiver. The residual HF on the CaF2 was less than 0.5% by weight.
This method was used for the last two runs of Example V. In both
these cases, the desorption was made in the same direction as the HF
was originally adsorbed on the CaF2, that is, cocurrent with the
absorption stream.
Example VII
Regeneration of the CaF2 contained in the 6 inch diameter
column was performed as follows:
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lOS'~Z9Z
The 6 inch diameter column was jacketed so that 150 psig
steam could be applied to the vessel externally. The CaF2 bed
containing absorbed HF was heated to about 350F, then air at about
150F was introduced at a rate varying from 0.25 to 1.0 SCFM per
sq. ft. of CaF2 bed area. This air was passed counter current to
the direction of the absorption of the HF , i.e., if the HF was
absorbed from the organic stream by passing the organic stream from
the bottom of the CaF2 bed through the top of the CaF2 bed, then
the desorbing air was passed from top to bottom of the CaF2 bed.
The CaF2 bed was desorbed to less than 0. 5% HF based on CaF2 weight.
Example VIII
Barium chloride dihydrate (BaC12 2H2O) was mixed with
calcium chloride dihydrate (CaC12 2H2O) in the ratio of 9 parts
BaC12 2H2O and 1 part CaC12 2H2O. A wet cake of the above was
pressed into a billet under 3000 psi hydraulic pressure. The billet
was then dried at 300F for 16 hours. The billets were then crushed,
screened, and fines less than 1/4" were discarded.
The 1/4" pieces were placed in a 2" I.D. x 24" long steel
pipe modified to allow sampling at 8" length, 16" length and the out-
let. Six hundred fifty-five grams of the above described mix were
placed in the 2" I.D. x 24" long tube. The tube was placed in a
chlorofluoro carbon gas stream containing approximately 3% by volume
HF, 36% by volume HCl, and 61% by volume organics. After 45 hours,
- the tube
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was removed and analyzed. Residence tlme was about 200 seconds.
Analysis after 45 hours showed 29.6% by weight HF absorbed on the
solids. Analysis of the solids showed no residual chlorides in
the solids (i.e., complete conversion).
The table below shows the percentage amount of hydrogen
fluoride removed from the gas stream at various times beginning at
2 hours up to 45 hours.
TABLE VI
ppm, HF
% HF
Hours Inlet Outlet Removed
2 12,000 71 99.4
12,500 84 99.3
8 13,500 1,620 87.5
18 16,000 1,710 89.3
24 17,400 1,200 93.0
37 12,300 7,800 36.6
12,300 12,000 2.5
13,000 11,400 12.0
Retention Time: 200 secs.
Grams Sample :655 (as BaC12~ CaC12)
Grams Sample~: 546.3 (as BaF2~ CaF2)
Grams HF Absorbed: 161.7
Grams HF Removed: 301.6 (total)
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~OS;~Z92
The barium fluoride pellets as prepared above may be
regenerated in accordance with one of the procedures of Example VI
or Example VII. Thereafter, the anhydrous barium fluoride may be
used in absorption runs as set forth in Examples IV or V.
- 24 -
