U.S. patent number 3,719,025 [Application Number 05/196,604] was granted by the patent office on 1973-03-06 for resolving gas mixtures.
This patent grant is currently assigned to Bayer Aktiengesellschaft, J. F. Mahler, Apparate-Und Ofenbau Kommandite-Gesellschaft. Invention is credited to Gerhard Heinze, Reiner Sarnes.
United States Patent |
3,719,025 |
Heinze , et al. |
March 6, 1973 |
RESOLVING GAS MIXTURES
Abstract
In the resolution of air containing water vapor by the
pressure-variation technique wherein the air is passed successively
through first and second separation zones, the water vapor being
removed from the air in the first zone and the nitrogen being
selectively removed from the balance of the air mixture in the
second zone, the air leaving the second zone being enriched in
oxygen and improvement which comprises intermittently discontinuing
passage of the air the first and second zones, reducing the
pressure in the first zone relative to the second zone by
withdrawing air from said first zone, whereby the nitrogen adsorbed
in said second zone is desorbed, passes into said first zone,
replaces the water vapor therein and the now desorbed, previously
adsorbed water vapor in the first zone is withdrawn from the first
zone, discontinuing the reduction of pressure in said first zone,
reinitiating passage of air to said first zone and from there into
said second zone, and temporarily delaying the flow of air from
said first zone into said second zone so that the pressure in said
first zone builds up prior to build-up of pressure in said second
zone. The delay of air flow can be due to a complete interruption
of flow or a throttling of flow from the first to the second zone.
Other gas mixtures may be similarly resolved.
Inventors: |
Heinze; Gerhard (Schildgen,
DT), Sarnes; Reiner (Nellingen, DT) |
Assignee: |
Bayer Aktiengesellschaft
(Leverkusen, DT)
J. F. Mahler, Apparate-Und Ofenbau Kommandite-Gesellschaft
(Esslingen, DT)
|
Family
ID: |
5787769 |
Appl.
No.: |
05/196,604 |
Filed: |
November 8, 1971 |
Foreign Application Priority Data
|
|
|
|
|
Nov 11, 1970 [DT] |
|
|
P 20 55 425.0 |
|
Current U.S.
Class: |
95/98; 95/102;
95/139 |
Current CPC
Class: |
B01D
53/0476 (20130101); B01D 2253/104 (20130101); B01D
2257/102 (20130101); B01D 2259/403 (20130101); B01D
2256/12 (20130101); B01D 2257/80 (20130101); B01D
2253/106 (20130101); B01D 53/261 (20130101); B01D
2257/504 (20130101); B01D 2253/108 (20130101); B01D
2259/402 (20130101); Y02C 20/40 (20200801); B01D
2259/40007 (20130101); Y02C 10/08 (20130101) |
Current International
Class: |
B01D
53/06 (20060101); B01D 53/047 (20060101); B01d
053/04 () |
Field of
Search: |
;55/30-32,58,74,75,179,389 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Hart; Charles N.
Claims
What is claimed is:
1. In the resolution of a gas mixture containing water vapor and at
least two additional gases by the pressure-variation technique
wherein the gas mixture is passed successively through first and
second separation zones, the water vapor being removed from the gas
mixture in the first zone and a more readily adsorbable component
being removed from the balance of the gas mixture in the second
zone, the gas leaving the second zone being enriched in the
non-adsorbed gaseous component relative to the initial gas mixture,
the improvement which comprises intermittently discontinuing
passage of the gas mixture through the first and second zones,
reducing the pressure in the first zone relative to the second zone
by withdrawing gas from said first zone, whereby the gaseous
component adsorbed in said second zone is desorbed, passes into
said first zone, replaces the adsorbed gas therein and the now
desorbed, previously adsorbed gas in the first zone is withdrawn
from the first zone, discontinuing the reduction of pressure in
said first zone, reinitiating passage of the gas mixture to said
first zone and from there into said second zone, and temporarily
delaying the flow of said gas mixture from said first zone into
said second zone so that the pressure in said first zone builds up
prior to build-up of pressure in said second zone.
2. The process according to claim 1, wherein the temporary delay of
flow of said gas mixture from said first zone to said second zone
is effected by sealing off said zones from one another until the
pressure in said first zone approaches its normal working
level.
3. The process according to claim 1, wherein the temporary delay of
flow in said gas mixture from said first zone to said second zone
is effected by throttling the flow of gas from said first zone to
said second zone until the pressure in said first zone approaches
its normal working level.
4. The process according to claim 1, wherein the gas mixture is
supplied to said first zone during adsorption at a positive
pressure up to about 15 atmospheres, the gas desorbed in said first
zone being withdrawn therefrom at about atmospheric pressure.
5. The process according to claim 1, wherein the gas mixture is
supplied to said first zone during adsorption at about atmospheric
pressure, the gas desorbed in said first zone being withdrawn
therefrom by a vacuum.
6. The process according to claim 1, wherein the gas mixture is
supplied to said first zone during adsorption at a positive
pressure up to about 15 atmospheres, the gas desorbed in said first
zone being withdrawn therefrom by a vacuum.
7. The process according to claim 1, wherein the temporary delay of
flow of said gas mixture from said first zone to said second zone
is discontinued when the pressure in said first zone reaches a
predetermined level.
8. The process according to claim 1, wherein the temporary delay of
flow of said gas mixture from said first zone to said second zone
is discontinued after a predetermined time interval.
9. The process according to claim 1, wherein said gas mixture is
air.
10. The process according to claim 1, wherein said gas mixture
contains carbon dioxide and a selective adsorbent therefor is
located in said second zone for its removal.
Description
The so-called pressure-variation process has recently been
introduced into practice for resolving, i.e. drying and separating,
gas mixtures. This adsorptive process can generally be used for
separating gas mixtures whose components differ from one another in
their affinity for adsorption. The pressure-variation process was
proposed in particular for the production of inert gases and for
dissociating air. In the following, reference is made essentially
to the production of oxygen-enriched air because this process is of
considerable commercial significance. However, the statements are
also applicable to the separation of other gas mixtures containing
water vapor.
Oxygen-enriched air is required for example for intensifying
oxidation reactions in chemical processes, for use in metallurgy,
for accelerating fermentative processes and for producing hot
flames. The advantage of adsorptive methods for producing
oxygen-enriched air is embodied in the simplicity of the processes,
which are generally carried out at ambient temperature. Since no
high-percentage oxygen or even liquid oxygen is formed in the
plants, plants of this kind can be operated in the complete absence
of danger and the safety precautions normally taken in liquid air
plants are unnecessary. By virtue of the simplicity of the
installations, it is also possible to build economically operating
units, even down to extremely low capacities.
Installations for the adsorptive enrichment of constituents of a
gas mixture on the pressure-variation principle function in the
pressure range between the inlet or entry pressure p of the gas to
be separated, which can be available either at atmospheric pressure
or at excess pressure, and the desorption pressure p' which is
produced by a vacuum pump. In the case of installations where the
gases enter under excess pressure, the desorption pressure p' can
also be atmospheric pressure, in other words the gas is allowed to
expand to atmospheric pressure in the absence of a vacuum pump.
Accordingly, pressure-variation installations can be operated in
the excess pressure - normal pressure, normal pressure - vacuum or
excess pressure - vacuum ranges. In installations for enriching the
oxygen in air, it is preferred to operate by evacuation with a
vacuum pump because the N.sub.2 -desorption at atmospheric pressure
is inadequate. Installations of this kind can consist of a single
adsorption system communicating with a storage vessel, or of two or
more parallel adsorption systems functioning in sequence so that a
constant stream of oxygen-enriched air is obtained as the product
gas. In the case of three units, the overflow, evacuation and
pressure-buildup cycles follow one another in chronological
rotation.
Adsorptive enrichment processes for oxygen are based on the
principle that different molecular sieve zeolites adsorb nitrogen
to a greater extent than they adsorb oxygen. Since only a few
percent by weight of nitrogen are adsorbed at ambient temperature,
the charging cycles are so short that the nitrogen cannot be
thermally desorbed. Accordingly, the zeolite is regenerated by
pressure reduction, optionally combined with the application of a
purge gas.
Molecular sieve zeolites only show an adequate charging capacity
for nitrogen in anhydrous form. In cases where, as is normally the
case, atmospheric air is used for separation, therefore, the
adsorbent would gradually become saturated with water vapor so that
it could not be used for separation. For this reason, one feature
common to all conventional separating processes for adsorptive
dissociation of air is that dried air is used. Stringent
requirements are imposed on the completeness of drying because the
molecular sieve zeolites used for separation are highly effective
drying agents and would gradually become saturated with water even
from air that has been dried by conventional techniques. For
example, the equilibrium load of a calcium zeolite A with a pore
width of 5 A in air with a dew point of minus 40.degree.C still
amounts to approximately 17 g of water per 100 g of anhydrous
zeolite at room temperature. Accordingly, predrying of the air
represents a difficult problem which hitherto has not been
satisfactorily solved. More particularly, the economy of the
enrichment process as a whole is largely determined by the
predrying stage of the air.
The air can adequately be predried in adsorbers filled with
molecular sieve zeolites which are thermally regenerated after
saturation with water. Unfortunately, a drying installation of this
kind with the associated regenerating apparatus is relatively
complex and also has the disadvantage that a considerable,
undesirable increase in the temperature of the air stream occurs
during the adsorptive removal of water, especially when air at
atmospheric pressure is being dried, on account of the heat of
adsorption. Unfortunately, the separating efficiency of an
adsorptive oxygen enrichment installation decreases with increasing
temperature.
For this reason, it has already been proposed (DAS 1,259,857) to
dry the air by passing it through low temperature recuperators
until its water content amounts to less than 20: p mg/Nm.sup.3 (p
is the pressure in kg/cm.sup.2). However, a process of this kind
can only be worked economically in cases where adsorptive oxygen
enrichment is to be carried out at low temperatures of, for
example, from -60.degree. to -100.degree.C.
It has also been proposed (DAS 1,259,844) to have the actual oxygen
enrichment installation for drying the air preceded by an
independently operating, adsorption installation functioning on the
pressure-variation principle which is filled with any drying agent
suitable for this purpose, for example activated alumina, and which
delivers the dried air to a storage vessel from which the actual
separating plant is fed. Apart from the outlay it involves in terms
of apparatus, a process of this kind has the disadvantage of high
energy consumption because, to regenerate the drying towers, some
of the previously compressed air has to be continuously vented to
the atmosphere.
In an experiment which has also been described, air at a pressure
of 5.3 kg/cm.sup.2 and with water content of from 3000 to 6000 ppm
was processed in an oxygen-enrichment apparatus on the
pressure-variation principle into an oxygen-rich product gas which
only contained from 2 to 6 ppm of water. In this case, the adsorber
was completely filled with molecular sieve zeolites and the entry
zone acted as a drying zone, while the rest of the filling was
available for the actual oxygen enrichment process. However, this
basically simple arrangement gives only inadequate separation based
on the energy consumed, because experience has shown that the
water-charging zone in pressure-variation systems has no sharp
limitation, but runs along the adsorber in the form of a flat
abatement zone and on the other hand zeolites precharged even with
only a few percent of water are almost completely ineffective so
far as oxygen enrichment is concerned.
Another serious disadvantage of this arrangement is that, in the
event of prolonged inoperative periods, the H.sub.2 O-charge of the
entry zone is distributed by diffusion throughout the entire
filling of the adsorber, making it unsuitable for oxygen
enrichment.
It is accordingly an object of the invention to provide a process
and apparatus for resolving gas mixtures, which is economical in
its energy requirements and simple to carry out.
These and other objects and advantages are realized in accordance
with the present invention which relates to the resolution of a gas
mixture containing water vapor and at least two additional gases by
the pressure-variation technique wherein the gas mixture is passed
successively through first and second separation zones, the water
vapor being removed from the gas mixture in the first zone and a
more readily adsorbable component being removed from the balance of
the gas mixture in the second zone, the gas leaving the second zone
being enriched in the non-adsorbed gaseous component relative to
the initial gas mixture. In accordance with the invention the
process also includes intermittently discontinuing passage of the
gas mixture through the first and second zones, reducing the
pressure in the first zone relative to the second zone by
withdrawing gas from said first zone, whereby the gaseous component
adsorbed in said second zone is desorbed, passes into said first
zone, replaces the adsorbed gas therein and the now desorbed,
previously adsorbed gas in the first zone is withdrawn from the
first zone, discontinuing the reduction of pressure in said first
zone, reinitiating passage of the gas mixture to said first zone
and from there into said second zone, and temporarily delaying the
flow of said gas mixture from said first zone into said second zone
so that the pressure in said first zone builds up prior to build-up
of pressure in said second zone.
The process according to the invention obviates the disadvantages
of earlier processes and enables the oxygen content of moist air to
be enriched without an appreciable energy requirement for drying.
The process according to the invention can be carried out as
follows for example using zeolites as adsorbents: a zeolite-filled
adsorber and an adsorber filled with a drying agent are associated
with one another and connected by a pipe provided with a throttle
means. In the course of one complete adsorption and desorption
cycle, a fairly high resistance is put up to the gas flowing
through the connecting pipe in alternating directions as it flows
from the drying agent to the zeolite (adsorption), at least during
the period of pressure increase in the zeolite adsorber from the
desorption pressure to at most the working pressure, with the
throttle means more closed than open. When the gas flows in the
opposite direction from the zeolite to the drying agent
(desorption), a lower resistance is offered to the gas stream
during the period of pressure decrease from the working pressure to
the desorption pressure with the throttle means more open than
closed.
In another advantageous embodiment, after regeneration of the
adsorption system and resumption of the flow of gas to the first
zone (zone I) the flow of gas from zone I to the second zone (zone
II) is altogether interrupted, rather than being merely throttled,
until the pressure in zone I approaches or reaches its normal
working level.
In the process according to the invention, predrying of the air and
the separation of nitrogen are carried out in a single process
stage. Although the drying agent and the adsorbent for nitrogen are
arranged in separate vessels, one dryer and one nitrogen adsorber
together form a unit through which the gases to be dried and
enriched and, in the opposite direction, the regeneration gases
flow chronologically in the same cycle. During adsorption, the
moist gas enters the dryer, gives off its moisture to the drying
agent and then flows through the separating column. During
desorption, the gas flows through the dryer in the opposite
direction from the separating column and carries the moisture
previously stored there into the open.
When the moist air flows into the dryer/adsorber combination
adjusted beforehand to a low desorption pressure, the throttle
means arranged between the two zones I and II is substantially or
completely closed so that the entry pressure p of the air is
adjusted relatively quickly in the dryer, while the increase of
pressure in the zeolite adsorber, by virtue of the throttle effect,
only takes place after some delay. The advantage of this measure is
that drying of the entry air, taken as an average over the inflow
time, takes place at a higher pressure than in the absence of the
throttle means. Since, at the same time as the pressure, the
H.sub.2 O partial pressure is also increased accordingly, greater
charging of the drying agent and hence a shorter adsorption zone
are obtained. In addition, the effective rate of flow in the dryer
is reduced which also improves the drying effect. During
desorption, the pressure would fall more rapidly in the dryer than
in the zeolite adsorber if the throttle means were substantially
closed. Basically, this would promote the desorption of water from
the drying agent because, in the event of a rapid drop in pressure,
an effectively larger quantity of regenerating gas would flow
through the drying agent. On the other hand, it is actually the
desorption stage, providing it is carried out by evacuation with a
vacuum pump, which is the principal energy-consuming stage in
oxygen enrichment processes. In order to use a minimum of energy,
therefore, the flow of gas between the zones II and I is kept as
free as possible from interference in the process according to the
invention during the desorption stage in order to reduce flow
resistances, especially for as long as the vacuum pump is
functioning effectively, i.e. during the fall in pressure from the
working pressure to the desorption pressure, at least from that
point in time at which atmospheric pressure is approximately
reached in the drying agent adsorber.
The invention will be further described with reference to the
accompanying drawings, wherein:
FIG. 1 is a schematic illustration of an apparatus in accordance
with the invention having a time-controlled throttled valve between
first and second zones;
FIG. 2 is a similar view of another embodiment with a one-way valve
in a by-pass pipe extending between the first and second zones;
FIG. 3 is a similar view of still another embodiment of valving to
delay pressure build-up in the second zone;
FIG. 4 is a schematic illustration of a system comprising two banks
of adsorption zones arranged in parallel, one undergoing desorption
while the other is undergoing adsorption; and
FIG. 5 is a schematic illustration of a system with three banks
arranged in parallel, one undergoing adsorption, one desorption and
the third pressure build-up after desorption and prior to renewed
adsorption.
Referring now more particularly to the drawings, in the simplest
case, the variable throttle means can consist of a non-return flap
which is installed in a bypass pipe to the connecting pipe as shown
in FIG. 2. In the Figure, the reference I denotes the adsorber
filled with drying agent while the reference II denotes the zeolite
adsorber for the adsorption of N.sub.2. The two adsorbers are
connected to the regulating valve 5 through the pipe 3. The
regulating valve 5 is fixedly adjusted to the required through-flow
cross section. A bypass pipe 4 with the non-return valve 6 leads
around the valve 5. When the gas is flowing from I to II
(adsorption), the non-return valve is closed, whereas when the
gases are flowing in the opposite direction (desorption) it is
automatically opened so that the total cross-sectional area of pipe
for flow of gas is larger than during adsorption.
As shown in FIG. I, however, the throttle means can also consist of
an electrically or pneumatically controlled valve 5 which is
accommodated in the connecting pipe 3 between the two zones. In
this case, the valve is actuated, i.e. more or less widely opened,
by a time-dependent regulating system. In a preferred embodiment,
the throttle valve 5 is regulated directly as a function of the
pressure difference between zones I and II, rather than by a time
control system. When the air flow into the previously evacuated
vessel in the direction from I to II, the throttle valve 5 remains
less widely open until the pressure prevailing in the zeolite
column II has approached the entry pressure of the air adjusted in
the drying column I. This method of regulation has the advantage
that any changes in the operating parameters of the installation,
such as the throughput, entry pressure, cycle time, pump
efficiency, etc., do not necessitate readjustment of the setting of
the throttle valve 5.
Another embodiment is shown in FIG. 3. A regulating valve 5 is
arranged in the connecting pipe 3 between the two zones I and II,
being completely closed during charging and completely open during
desorption. An overflow valve is installed in the bypass pipe 4
parallel to this regulating valve, remaining initially closed
during charging to produce a particularly rapid build up of
pressure in the dryer I. Only after a certain pre-adjusted pressure
has been reached does the overflow valve open, allowing the
adsorber II to fill up while maintaining the pressure in the dryer
I.
The combination of one dryer with one nitrogen adsorber according
to the invention into a unit which functions in time in the
adsorption cycle, and the principle of regulating the flow
resistance in the connecting line between both vessels by a
throttle means in the manner described above, can be applied to
oxygen enrichment plants with 2,3 or more nitrogen adsorbers. The
principle of the invention is not confined to a certain
construction of pressure-variation systems or to application within
certain pressure ranges. It can function generally at pressures of
from 5.0 Torr to 15 atmospheres. Regeneration is preferably carried
out at reduced pressures of down to 50 Torr, preferably of from 50
to 400 Torr, while gas removal is preferably carried out at
atmospheric pressure. In cases where gas mixtures under elevant
pressure are available or in cases where product gases under
elevated pressure are required, the process as a whole and the
gas-removal stage in particular, can be carried out at elevated
working pressure, i.e. up to pressures of 15 and preferably up to 6
atmospheres. In this case, regeneration is carried out either by
expansion to atmospheric pressure or even at reduced pressure.
Drying agents suitable for use in installations implementing the
process according to the invention include various adsorbents such
as, for example, silica gels, activated alumina and molecular sieve
zeolites, providing they can be reversibly charged and discharged
under the operating conditions of the pressure-variation system
which is also known as "cold regeneration." Molecular sieve
zeolites suitable for the N.sub.2 - adsorbers include natural and
synthetic zeolites providing they show sufficiently high
selectivity and absorptivity for nitrogen at the working
temperatures of the process. It is preferred to use type A zeolites
exchanged with divalent cations or faujasite in granular form.
Synthetic faujasites and type 5 A zeolites are preferably used for
removing carbon dioxide from combustion or cracked gases.
The process according to the invention is illustrated by the
following examples:
EXAMPLE 1
Throttle means as shown in FIG. 2 with the non-return valves 6a and
6b were installed in a laboratory installation of the kind shown in
FIG. 4 comprising two nitrogen adsorbers (IIa and IIb) and the
associated dryers (Ia and Ib). 7a and 7b are further non-return
flaps at the outlet end of the nitrogen adsorbers which close
during evacuation of the adsorbers. The magnetic valves 8a, 9a, 8 b
and 9b are controlled by a time relay. The air to be enriched with
oxygen is removed at the valve 10 of a compressed air line. 11 is a
water saturator in which the air is saturated with water vapor at
room temperature. 12 is a relief pressure valve which throughout
the entire system only admits an excess pressure corresponding to
the water column in 12. 13 is a non-return valve which prevents the
water from rising back from the relief pressure valve 12.
The dryers Ia and Ib are each filled with 200 g of silica gel in
bead form with a moisture indicator, so-called Blaugel. The
nitrogen adsorbers IIa and IIb each contain 477 g of a
calcium-strontium zeolite A in bead form. The vacuum pump 18 is a
gas ballast pump with an intake of 1100 liters per hour. A time
relay changes the setting of the magnetic valves 8a, 9a, 8b and 9b
every 55 seconds. In the first switching cycle, the valves 8a and
9b are opened and the valves 9a and 8b closed. As a result, air
saturated with moisture flows through pipe 16 and the magnetic
valve 8a into the previously evacuated adsorbers Ia and IIa until
the pressure is equalized. At the same time, the non-return flap 6a
closes, thus causing a fairly rapid build up of pressure in the
dryer Ia.
After atmospheric pressure has been reached in the adsorber IIa,
the non-return flap 7a opens and oxygen-rich dry product gas flows
through pipe 14 to a gasometer 15. During the same switching cycle,
the adsorbers Ib and IIb, with the non-return flap 7b closed, are
evacuated through the magnetic valve 9b and the pipe 17 by the
vacuum pump 18 which gives off nitrogen-rich moist gas to the
atmosphere. In the second switching cycle, the same operations take
place with the magnetic valves 8b and 9a opened and the magnetic
valves 8a and 9b closed, only the adsorption systems a and b
exchanging their functions. For an average rate of flow of the
entry air of 420 N-1/hour, 150 N-1/hour of dry product gas with an
oxygen content of 43 percent by volume are obtained.
The vacuum reached at the end of each switching cycle in the
nitrogen adsorber amounts to 105 Torr.
Despite complete saturation of the entry air with water, the
indicator color of the silica gel in the dryers Ia and Ib showed
that, after a few hours' operation, the charging front did not move
any further forwards, but remained stationary. When the non-return
valves 6a and 6b were forcefully prevented from closing through
jamming of the cones, the H.sub.2 O-charging zone moved through the
dryers which were not adequate for this operational state. When the
function of the non-return flaps 6a and 6b was restored, the
water-charging zone returned again and settled at the original
stationary value.
EXAMPLE 2
In an industrial installation comprising three adsorber units of
the kind shown in FIG. 5, 113 liters (90 kg) of silica gel in bead
form with so-called Blaugel as the moisture indicator were
accommodated in each of the containers 1a, b and c, while 190
liters (125 kg) of calcium zeolite A in bead form were accommodated
in each of the containers IIa, b and c. The containers Ia, b and c
were used to dry the incoming atmospheric air, while the containers
IIa, b and c were used for nitrogen adsorption and oxygen
enrichment. As in FIG. 3, one regulating valve 5a, b and c and one
overflow valve 6a, b and c was arranged between each drying-agent
container and the associated zeolite container. The valves 7a, 7b
and 7c at the head of the zeolite containers were non-return
valves. At the beginning of the cycle, the pair of containers Ia
and IIa were simultaneously evacuated through the opened valves 5a
and 9a, the pipe 17 and the vacuum pump 18. Accordingly, the
reduction in pressure in the containers Ia and IIa took place in
the same way. The vacuum pump had a delivery of approximately 500
m.sup.3 /h.
During the same period, the containers Ib and IIb which had been
previously evacuated were adjusted with atmospheric air flowing in
through pipe 16 and the opened valve 8b from an absolute pressure
of approximately 50 to 100 Torr to atmospheric pressure. The valves
5b and 9b were closed during this operation. The overflow valve 6b
was also initially closed and, as a result, caused the rapid build
up of atmospheric pressure in container Ib. After this pressure had
been reached valve 6b permitted gas to escape into container IIb so
that its pressure also rose to atmospheric whereupon valve 5b could
be opened for resumption of normal flow during adsorption.
Again during the same period, atmospheric air flowed through pipe
16 and the opened valve 8c into the container Ic and further
through the opened overflow valve 6c into the zeolite container IIc
and further through the opened non-return valve 7c and the pipe 14
into the collecting vessel 15.
The operations described above were then repeated with the
difference that the group of containers c were evacuated, the group
of containers a adjusted to atmospheric pressure by the admission
of air and the group of containers b traversed by air in order to
give off oxygen-enriched gas to the collecting vessel 15, etc.
Approximately 22 Nm.sup.3 /hr of product gas with an average oxygen
content of 60 percent by volume flowed constantly through the pipe
14 into the collecting vessel 15.
In order to monitor drying, the containers Ia, b and c were
provided with one transparent wall. Even after continuous operation
for several weeks, it was impossible to detect any local change in
the mass-transfer zone, i.e. the zone in which the Blaugel
undergoes a change in color to pink, remained stationary.
It will be appreciated that the instant specification and examples
are set forth by way of illustration and not limitation, and that
various modifications and changes may be made without departing
from the spirit and scope of the present invention.
* * * * *