Process for producing oxygen enriched product stream

A two bed pressure swing adsorption process is disclosed having high yield and high production rate. The process utilizes fine or normal size zeolite sieve material and relatively short cycle times. A power saving can be obtained by sequencing the various steps of the process to provide substantially continuous use of a vacuum pump.

BACKGROUND OF THE INVENTION 
This invention relates to a process for obtaining an oxygen enriched gas 
from a mixed gas containing principally oxygen and nitrogen as gas 
components, such as air, by means of pressure swing adsorption (PSA). 
Pressure swing adsorption systems and process have been widely used to 
produce oxygen enriched streams from mixed gases, including air, and a 
multitude of such systems and processes have been utilized. 
It is advantageous, in such systems, to utilize a relatively short time 
cycle for carrying out the process inasmuch as shorter times obtain good 
utilization of the sieve material used to adsorb one of the components. 
The short cycle times generally employ a finer particle size of sieve 
material to reduce diffusive resistance. Typical examples of short cycle 
times are shown and described in U.S. Pat. Nos. 4,194,891 and 4,194,892. 
Oxygen production increased with the process in the aforementioned patents 
however the yield was fairly low, e.g., 10-20% yields. 
Conventional vacuum PSA processes do produce a higher oxygen yield (50-60%) 
however the production rate is somewhat low. The normal production rate of 
conventional three bed PSA processes is not particularly high; as an 
example, typically, the bed size factor is about 2000-2600 kg of zeolite 
per metric ton of oxygen produced per day. 
Optimally, one would obviously like to obtain the high production rate 
typified by faster cycle times and finer sieve particles along with the 
high yield typlified by conventional three bed systems yet have a process 
that is inexpensive and relatively simple in operation. 
SUMMARY OF THE INVENTION 
The PSA process of the present invention achieves an enriched oxygen 
product that has a high oxygen yield as well as high production rate by 
solving the disadvantages of the prior art while minimizing cost and 
maintaining simplicity of operation. 
The system uses short cycle times to gain good usage of the sieve material 
but requires only two beds, thus greatly simplifying the prior three-bed 
processes that heretofore were needed for high yields. 
As will be shown, one of the further features is the power saving by 
continuous or nearly continuous utilization of a vacuum pump with a two 
adsorption column system. This is accomplished by carrying out part or all 
of the equalization procedure, during which an oxygen-enriched stream from 
the outlet end of a first column is supplied to the outlet end of a second 
column, while desorbing nitrogen rich gas from the inlet end of the first 
column. By this means, the vacuum pump is run during at least part of the 
equalization procedure as well as during the remaining steps. Since the 
vacuum pump is running continuously or almost continuously during the 
overall cycle, its use, and thus its power consumption, is optimized. 
Thus, the two bed PSA process having high yield and production rate is 
achieved using relatively, fine particles of zeolite sieve material, such 
as 20-35 mesh size and even with larger particles such as 8-12 mesh size 
at short cycle times less than 40 seconds, preferably about 25-30 seconds. 
The range of pressure swing uses vacuum of less than 300 torr and 
preferably to 200 torr for desorption and maximum product pressure less 
than 5 psig and preferably less than 3 psig. 
In a first embodiment of the invention the process is carried out in a 
total of six steps per each complete cycle. In steps one to three the 
first column is continuously evacuated by means of a vacuum pump and in 
steps four to six the second column is evacuated with the vacuum pump. 
Thus, in this embodiment the vacuum pump is utilized throughout the entire 
cycle. In steps one and four, which are pressure equalization steps, gas 
is passed from the column undergoing evacuation to the other column; in 
steps two and five, the column not undergoing evacuation receives backfill 
gas from the product reservoir; and in steps three and six, the column not 
undergoing evacuation receives feed gas and produces product while product 
gas is used to purge the column undergoing evacuation. 
In a second embodiment of the invention the process is carried out in a 
total of eight steps per each complete cycle. In steps one to four the 
first column is continuously evacuated by means of a vacuum pump and in 
steps five to eight the second column is continuously evacuated with the 
vacuum pump. Accordingly, in this embodiment also, the vacuum pump is 
utilized throughout the entire cycle. In steps one and five, which are 
pressure equalization steps, gas is passed from the column undergoing 
evacuation to the other column; in steps two and six, the column not 
undergoing evacuation receives backfill gas from the product reservoir; in 
steps three and seven, the column not undergoing evacuation receives feed 
gas and produces product; and in steps four and eight the column not 
undergoing evacuation continues to receive feed gas and produce product 
while product gas is used to purge the column undergoing evacuation. In 
other words, the cycle of this embodiment is identical to the cycle of the 
first embodiment except that this embodiment contains a step in which the 
column not undergoing evacuation produces product while the other column 
undergoes evacuation without purge. The cycle of this embodiment is more 
efficient than the cycle of the first embodiment. 
In a third embodiment of the invention the process is carried out in a 
total of ten steps per each complete cycle. In steps two to five the first 
column is continuously evacuated by means of a vacuum pump and in steps 
seven to ten the second column is continuously evacuated with the vacuum 
pump. Thus, in this embodiment the vacuum pump is utilized during eight of 
the ten steps of the operating cycle. In steps one and six, which are 
pressure equalization steps, gas is passed from the column which has just 
completed production to the other column; in steps two and seven, which 
are also pressure equalization steps, gas is passed from the column 
undergoing evacuation to the other column; in steps three and eight, the 
column not undergoing evacuation receives backfill gas from the product 
reservoir; in steps four and nine, the column not undergoing evacuation 
receives feed gas and produces product; and in steps five and ten the 
column not undergoing evacuation continues to receive feed gas and produce 
product while product gas is used to purge the column undergoing 
evacuation. Thus, the cycle of this embodiment is identical to the cycle 
of the second embodiment except that this embodiment contains an 
equalization step without evacuation. The advantage of this embodiment is 
that there is less disturbance of the bed that provides gas during the 
equalization procedure since this bed does not undergo depressurization 
from both ends during the early part of the equalization procedure when 
the pressure differential between the beds is at a maximum.

DESCRIPTION OF THE PREFERRED EMBODIMENT 
The cycle of the first embodiment of the present invention will 
specifically be described with reference to the schematic flow diagram 
shown on FIG. 1 and the column cycle of FIG. 2. 
Considering first FIGS. 1 and 2A-2F, there is shown a system for producing 
an enriched oxygen gas stream continuously generated from a gas containing 
principally oxygen and nitrogen, such as air. Each of the two adsorption 
columns A and B contains an adsorbent capable of selectively adsorbing 
nitrogen. 
In all process embodiments of the invention the adsorption columns are 
packed with relatively fine particles of zeolite, i.e. about 8-35 mesh and 
preferably about 12-20 mesh. Typical zeolite sieve material is available 
in the form of beads or pellets from various zeolite manufacturers. 
Control of each of the steps of the process, embodiments can be regulated 
by conventional means, e.g., a timer to control solenoid operated valves 
of standard commercial design. 
In step 1 of the first embodiment (shown in FIG. 2A), valves 1A and 2A are 
closed, thereby closing off the lower or inlet end of the first column A. 
At the top, or outlet end, of column A, valves 4A and 5A are closed and 
valve 3A is open. With respect to the second column B, valves 9B and 10B 
are closed; thus gas from the outlet of column B is being introduced into 
the outlet of column A through valve 3A and the flow is controlled by 
valve 8B. At the same time in Step 1, at the inlet end of column B valve 
6B is closed but valve 7B is open; thus gas is being withdrawn from the 
inlet end of column B by means of vacuum pump 16. 
During this step, the pressure in column B, which is initially higher than 
the pressure in column A, is used to substantially equalize the pressures 
in both columns. That is, column B may, at the beginning of step 1, be at 
a positive pressure of about 1010 torr (4.84 psig) and is reduced to about 
500 torr (-5.03 psig) by the end of step 1, while column A commences step 
1 at a pressure of about 200 torr (-10.83 psig) and the pressure is raised 
to 470 torr (-5.61 psig). At the end of step 1, therefore, the column 
pressures are essentially equalized. Step 1 may take place extremely 
rapidly, preferably in about 2 seconds to 6 seconds and more preferably in 
about 4 seconds. 
In Step 2, valve 3A is closed and valve 5A and valve 24 opened and oxygen 
enriched product gas from the reservoir 18 is introduced into the outlet 
of column A and is controlled by metering valve 26 to backfill column A 
and to raise the pressure further in column A. Typically, since the 
pressure in product reservoir is about 800 torr, the pressure within 
column A continues to increase from 470 torr (-5.61 psig) to about 660 
torr (-1.93 psig). At the same time, gas is still being withdrawn from the 
inlet of column B through open valve 7B by vacuum pump 16 and the pressure 
within column B continues to decrease. That pressure may decrease, in step 
2, from 500 torr (-5.03 psig) to about 450 torr (-6.00 psig). Again, the 
timing of step 2 is extremely rapid, preferably being completed in about 1 
to 5 seconds, and more preferably in about 3 seconds. 
In step 3, valve 1A is open, and air or other feed gas containing 
principally oxygen and nitrogen under a predetermined feed pressure is 
introduced to the inlet of column A through line 14. Inlet pressures may 
vary but the inlet pressure ideally has a minimum predetermined pressure 
of between 3 and 7 psig, and more preferably has a minimum value of about 
5 psig. At the outlet of column A, valve 5A is closed and valve 4A is 
opened. Thus the feed air passes through column A where nitrogen is 
adsorbed and an oxygen enriched product stream passes from the outlet end 
of column A, through valve 4A, check valve 11 and through line 20 to the 
product reservoir 18. During this step, the pressure in column A may 
increase from 660 torr (-1.93 psig) to about 1010 torr (4.84 psig) in 
producing oxygen enriched product. At the same time, in step 3, gas 
continues to be withdrawn from the inlet end of column B to desorb or 
evacuate nitrogen enriched gas from column B by means of vacuum pump 16. 
Simultaneously with the desorption of column B via its inlet, valves 10B 
and 24 are open and oxygen enriched product stream is introduced into the 
outlet of column B to purge column B. The flow of the oxygen enriched 
product stream is controlled by metering valve 26. Thus, column B is both 
purged by an oxygen enriched stream of gas introduced into its outlet and 
desorbed by withdrawing nitrogen rich gas from its inlet. The pressure in 
column B thus continues to decrease, typically from about 450 torr (-6.10 
psig) to about 200 torr (-10.83 psig) as the withdrawal by means of vacuum 
pump 16 continues uninterrupted. Step 3 is also carried out quite rapidly, 
in a range of cycle time preferably of about 10 seconds to 25 seconds and 
more preferably about 18 seconds. 
Continuing on to step 4, equalization again takes place, this time by 
introducing the now higher pressure gas of column A into column B. This is 
carried out by closing valve 4A at the outlet of column A and opening 
valve 3A. At the outlet of column B, valve 10B is closed and thus, gas 
passes from column A to column B for equalization of pressures controlled 
by metering valve 8B. At the same time, of course, the feed stream is cut 
off by closing valve 1A at the inlet to column A and valve 2A is opened so 
that gas can be withdrawn from the inlet end of column A through vacuum 
pump 16. The inlet of column B is closed completely by closing valve 7B. 
In step 4, therefore, the pressures within column A and B are approximately 
equalized, the pressure in column A is reduced from about 1010 torr (4.84 
psig) to about 500 torr (-5.03 psig) while the pressure in column B is 
increased from about 200 torr (-10.83 psig) to about 470 torr (-5.61 
psig). Step 4 is carried out preferably in a time of from about 2 to about 
6 seconds, and more preferably in about 4 seconds. 
In step 5, valve 3A is closed, thus closing entirely the outlet end of 
column A while gas continues to be withdrawn from the inlet end of column 
A drawing the pressure down, typically, from 500 torr (-5.03 psig) to 450 
torr (-6.00 psig). Valves 10B and 28 are opened and oxygen enriched 
product from product reservoir 18 enters column B to backfill that column 
controlled by metering valve 30 such that the pressure in column B is 
increased from, typically, about 470 torr (-5.61 psig) to about 660 torr 
(-1.93 psig). Again, as in step 2, the backfilling step takes place in 
about 1 to 5 seconds, and preferably in about 3 seconds. 
Finally, in step 6, valve 6B is opened, thus introducing the pressurized 
feed stream into the inlet of column B. Valve 9B is opened so that the 
oxygen enriched product stream from column B passes through check valve 12 
and continues via line 20 to product reservoir 18. 
During step 6, valves 24 and 5A are open thereby allowing oxygen enriched 
gas to enter the outlet of column A to purge column A, controlled by 
metering valve 26. Simultaneously with the purging of column A, gas 
continues to be withdrawn from the inlet of column A by vacuum pump 16 to 
desorb or evacuate nitrogen rich gas. Typically, again, the pressure 
within column A decreases from about 450 torr (-6.00 psig) to about 200 
torr (-10.83 psig) while the pressure in column B increases from about 660 
torr (-1.93 psig) to about 1010 torr (4.84 psig). The timing of step 6 can 
be from about 10 to about 25 seconds and is preferably about 18 seconds. 
At the completion of step 6, the entire sequence is repeated on a continual 
cyclic basis so that product is continuously taken from product reservoir 
18 through valve 32 during each of the steps. 
As can be seen, in this embodiment the vacuum pump 16 is continuously 
utilized to withdraw gas alternately from one or the other of the two 
columns, thus it is efficiently utilized to minimize power use throughout 
the cycle. 
Turning now to FIG. 3, represented therein is a modification of the basic 
cycle illustrated in FIG. 2. Steps 1, 2, 5 and 6 of the cycle of FIG. 3 
are identical to steps 1, 2, 4 and 5, respectively, of the cycle of FIG. 
2. Step 3 of the cycle of FIG. 3 is similar to step 3 of the FIG. 2 cycle 
except that column B is not purged with product gas during step 3 of FIG. 
3. Similarly, step 7 of the FIG. 3 cycle differs from step 6 of the FIG. 2 
cycle in that column A is not purged during step 7 of the FIG. 3 cycle. 
This result is accomplished by keeping valves 10B and 24 closed during 
step 3 and valves 5A and 24 closed during step 7 of the FIG. 3 cycle. 
Thus, in step 3 of the cycle of FIG. 3 valve 1A is open, and air or other 
feed gas containing principally oxygen and nitrogen under a predetermined 
feed pressure is introduced to the inlet of column A. The inlet pressure 
may vary but ideally has a minimum predetermined value of between 3 and 7 
psig, and preferably has a minimum value of about 5 psig. At the outlet of 
column A, valve 5A is closed and valve 4A is open. The feed air passes 
through column A, where nitrogen is adsorbed, and an oxygen-enriched 
product stream passes from the outlet end of column A and through valve 
4A, check valve 11 and line 20 to product reservoir 18. During this step, 
the pressure in column A may increase from about 660 torr (-1.93 psig) to 
about 900 torr (2.71 psig) in producing oxygen enriched product. During 
step 3, gas continues to be withdrawn from the inlet end of column B to 
desorb or evacuate nitrogen enriched gas from column B by means of vacuum 
pump 16. The pressure in column B thus continues to decrease, typically 
from about 450 torr (-6.00 psig) to about 210 torr (-10.64 psig) as the 
withdrawal by means of vacuum pump 16 continues uninterrupted. Step 3 is 
carried out very rapidly, in a range of cycle time preferably of about 8 
seconds to 20 seconds and more preferably about 13 seconds. 
Similarly, in step 7 of the cycle of FIG. 3 valve 6B is open, thus 
introducing feed gas into column A through its inlet. At the outlet of 
column B, valve 9B is open, thereby permitting oxygen-enriched product 
stream from column B to pass through check valve 12, line 20 and into 
product reservoir 18. During step 7 the pressure within column A decreases 
from about 450 torr (-6.00 psig) to about 210 torr (-10.64 psig) while the 
pressure in column B increases from about 660 torr (-1.93 psig) to about 
900 torr (2.71 psig). The timing of step 7 can be from about 8 to about 20 
seconds and is preferably about 13 seconds. 
Steps 4 and 8 of the FIG. 3 cycle are identical to steps 3 and 6 of the 
FIG. 2 cycle, except that the duration of steps 4 and 8 of the cycle of 
FIG. 3 is shorter than that of steps 3 and 6 of the cycle of FIG. 2. Also, 
the initial pressure of the column being evacuated in steps 4 and 8 of the 
FIG. 3 cycle is lower than the initial pressure of the column being 
evacuated in steps 3 and 6 of the FIG. 2 cycle, due to the continuation of 
evacuation of the adsorbers in steps 3 and 7 of the cycle in FIG. 3. 
Thus, in step 4 of the cycle of FIG. 3, valves 1A and 4A are open, thereby 
permitting oxygen enriched product produced in column A to pass through 
check valve 11 and line 20 and to enter product reservoir 18, and in step 
8, valves 6B and 9B are open, thereby permitting oxygen enriched product 
produced in column B to pass through check valve 12 and line 20 to product 
reservoir 18. Also during step 4, valves 7B, 10B and 24 are open, thereby 
allowing oxygen enriched gas to purge column B and permitting vacuum pump 
16 to continue to evacuate column B. During step 8, valves 2A, 5A and 24 
are also open, thereby allowing oxygen-enriched gas to purge column A and 
permitting vacuum pump 16 to continue to evacuate column A. 
During step 4 the pressure within column B decreases from about 210 torr 
(-10.64 psig) to about 200 torr (-10.83 psig) while the pressure in column 
A increases from about 900 torr (2.71 psig) to about 1010 torr (4.84 
psig). Similarly, during step 8, the pressure within column A decreases 
from about 210 torr (-10.64 psig) to about 200 torr (-10.83 psig) while 
the pressure in column B increases from about 900 torr (2.71 psig) to 
about 1010 torr (4.84 psig). The timing of steps 4 and 8 can be from about 
5 to about 15 seconds and is preferably about 10 seconds. 
From the above it can be seen that the total cycle time for this embodiment 
is usually in the range of about 16 to about 46 seconds. In a preferred 
embodiment the total time for the eight step cycle is less than about 40 
seconds and is most preferably about 30 seconds. 
In this embodiment also, the vacuum pump 16 is continuously utilized to 
withdraw gas alternately from one or the other of the two columns, thus it 
is efficiently utilized to minimize power use throughout the cycle. 
Turning now to FIG. 4, represented therein is a modification of the basic 
cycle illustrated in FIG. 3. Steps 3, 4, 5, 8, 9 and 10 of the cycle of 
FIG. 4 are identical to steps 2, 3, 4, 6, 7 and 8 respectively, of the 
cycle of FIG. 3. Step 1 of the cycle of FIG. 4 differs from step 1 of the 
FIG. 3 cycle in that column B is not evacuated during step 1 of the cycle 
of FIG. 4. Similarly, step 6 of the FIG. 4 cycle differs from step 5 of 
the FIG. 3 cycle in that column A is not evacuated during step 6 of the 
FIG. 4 cycle. This result is accomplished by keeping valve 7B closed 
during step 1 of the FIG. 4 cycle and valve 2A closed during step 6 of the 
FIG. 4 cycle. Steps 2 and 7 of the FIG. 4 cycle differ from steps 1 and 5 
of the FIG. 3 cycle only in that duration of these steps and the pressures 
at the beginning of these steps are not the same. 
In step 1 of the cycle of FIG. 4 valve 3A is open and all other valves 
(except valve 32) are closed. During this step gas will pass from column B 
to column A. Also during this step, the pressure in column A typically 
increases from about 200 torr (-10.83 psig) to about 400 torr (-6.96 psig) 
while the pressure in column B decreases from about 1010 torr (4.84 psig) 
to about 750 torr -0.19 psig). Step 1 is carried out very rapidly, 
preferably in a cycle time range of about 2 to 6 seconds and more 
preferably in a cycle time of about 4 seconds. 
Similarly, in step 6 of the cycle of FIG. 4 valve 3A is open and all other 
valves (except valve 32) are closed. During this step gas will pass from 
column A to column B and the pressure in column B typically increases from 
about 200 torr (-10.83) psig) to about 400 torr (-6.96 psig) while the 
pressure in column A decreases from about 1010 torr (4.84 psig) to about 
750 torr (-0.19 psig). Step 6 is likewise preferably carried out in a 
cycle time range of about 2 to 6 seconds and more preferably in a cycle 
time of about 4 seconds. 
Steps 2 and 7 of the FIG. 4 cycle are identical to steps 1 and 5 of the 
FIG. 3 cycle, except that the preferred duration of steps 2 and 7 of the 
cycle of FIG. 3 is shorter than the preferred duration of steps 1 and 5 of 
the cycle of FIG. 3 and the initial pressure of the column being evacuated 
in steps 2 and 7 of the FIG. 4 cycle is lower than the initial pressure of 
the column being evacuated in steps 1 and 5 of the FIG. 3 cycle, due to 
the transfer of gas during steps 1 and 6 from the column that has just 
completed production to the column that has just completed regeneration. 
During step 1 of the cycle of FIG. 4, the pressure in column B decreases 
from about 1010 torr (4.84 psig) to about 750 torr (-0.19 psig) while the 
pressure in column A increases from about 200 torr (-10.83 psig) to about 
400 torr (-6.96 psig). Similarly, during step 6, the pressure within 
column A decreases from about 1010 torr (4.84 psig) to about 750 torr 
(-0.19 psig) while the pressure in column B increases from about 200 torr 
(-10.83 psig) to about 400 torr (-6.96 psig). The timing of steps 1 and 6 
can be from about 2 to about 6 seconds and is preferably about 4 seconds. 
During step 2 of the cycle of FIG. 4, the pressure within column B 
decreases from about 750 torr (-0.19 psig) to about 500 torr (-5.03 psig) 
while the pressure in column A increases from about 400 torr (-6.96 psig) 
to about 470 torr (-5.61 psig). Similarly, during step 7, the pressure 
within column A decreases from about 750 torr (-0.19 psig) to about 500 
torr (-5.03 psig) while the pressure in column B increases from about 400 
torr (-6.96 psig) to about 470 torr (-5.61 psig). The timing of steps 2 
and 7 can be from about 1 to about 5 seconds and is preferably about 3 
seconds. 
In this embodiment, the vacuum pump 16 is continuously utilized to withdraw 
gas alternately from one or the other of the two columns during eight out 
of the ten steps of this cycle. Thus it is efficiently utilized to 
minimize power use throughout most of the cycle. During the steps when the 
vacuum pump is not utilized to evacuate the columns it can continue to be 
operated, if desired, by supplying air to the pump. 
From the above it can be seen that the total cycle time for this embodiment 
is usually in the range of about 17 to about 51 seconds. In a preferred 
embodiment the total time for the ten step cycle is less than about 40 
seconds and is ideally about 30 seconds. 
The invention is further illustrated in the following examples in which, 
unless otherwise indicated, parts percentages and ratios are on a volume 
basis. 
EXAMPLE 1 
Using the apparatus illustrated in FIG. 1 and the sequence of steps 
illustrated in FIG. 2, the process of the invention was conducted to 
obtain an oxygen-enriched product stream. Two adsorption columns, A and B, 
each 2 inches in diameter and 15 inches in height were packed with Calcium 
X zeolite molecular sieve material in the form of 0.4-0.8 mm beads 
commercially available from Laporte Co. for runs 1-3 (TABLE 1) and zeolite 
material in the form of 1.5 mm pellets from Tosoh Company (Tosoh Zeolum 
SA) for run 4. The pressure swing range during the cycle was 3.5 psig to 
200 torr. 
The cycle times, production rates and yields obtained are tabulated in 
TABLE 1. 
TABLE 1 
______________________________________ 
Run 1 2 3 4 
______________________________________ 
Cycle times (second) 
25 20 17 25 
Oxygen purity (%) 93 93 93 93 
Bulk density (kg/cm3) 
681 681 681 620 
Oxygen yield (%) 59 58 56 55 
specific product (standard liter/hr 
40 51 59 40 
of produced oxygen/liter of bed) 
Bed size factor (kg zeolite per 
535 420 375 487 
metric tons of oxygen per day) 
______________________________________ 
From the above test, it can be seen that a high yield and a high production 
rate at a high purity can be achieved by a two column system wherein 
vacuum is continuously applied to one or the other of the columns during 
each of the steps. Thus, the vacuum pump is efficiently used and power 
conserved. The cycles are extremely rapid to achieve good utilization of 
the sieve material, yet the construction and operation of the two bed 
system is obviously more advantageous than the more complex, more 
expensive three bed systems. 
EXAMPLE 2 
Using the apparatus illustrated in FIG. 1 and the sequence of steps 
illustrated in FIG. 3, the process of the invention was conducted to 
obtain an oxygen-enriched product stream. Adsorption columns A and B had 
diameters of 24 inches and were 4 feet long. The columns were packed with 
25 inches of Tosoh SA500 sieve and 6 inches of alumina, with the alumina 
placed at the inlet end of the columns to adsorb moisture. The duration of 
the run was sufficient to establish steady state. 
The cycle times, production rates and yields obtained are tabulated in 
TABLE 2. 
TABLE 2 
______________________________________ 
Steps Duration, secs. 
______________________________________ 
1 and 5 4 
2 and 6 3 
3 and 7 13 
4 and 8 10 
Total cycle time 30 
Product purity (% oxygen) 
93.1 
Yield (%) 44.7 
Specific Product (Nm.sup.3 /hr product/ 
40.1 
m.sup.3 of sieve) 
______________________________________ 
As shown in TABLE 2 a high product purity and good yield are obtained when 
using the cycle of this embodiment of the invention. 
EXAMPLE 3 
Using the apparatus illustrated in FIG. 1 and the sequence of steps 
illustrated in FIG. 4, the process of the invention was conducted to 
obtain an oxygen-enriched product stream. Adsorption columns A and B had 
inside diameters of 4.3 cm. and were 1.8 meters long. The columns were 
packed to a height of about 1.7 meters with Tosoh SA500 sieve. In this 
example a preliminary guard bed packed with about 30 cm. of alumina was 
used with each column to adsorb moisture. To determine if the bed 
experiences disturbance during the cycle the top surface of the adsorbent 
bed was sprayed with paint prior to the experiment. The surface of the bed 
was examined after completion of the experiment to see if the paint layer 
was intact. A disrupted surface indicates disturbance of the bed. 
The cycle times, production rates and yields obtained are tabulated in 
TABLE 3. 
TABLE 3 
______________________________________ 
Steps Duration, secs. 
______________________________________ 
1 and 6 4 
2 and 7 3 
3 and 8 3 
4 and 9 10 
5 and 10 10 
Total cycle time 30 
Product purity (% oxygen) 
93 
Yield (%) 49.2 
Specific Product (Nm.sup.3 /hr product/ 
41 
m.sup.3 of sieve) 
______________________________________ 
As can be seen, good performance results were obtained. The surface of the 
bed was examined and found to be undisturbed, indicating that no movement 
of the adsorbent bed occurred. When the same test was performed without 
using steps 1 and 6 some disturbance of the bed was detected. Thus, the 
ten step cycle of the invention presents an additional advantage. 
While particular embodiments of the invention have been shown, it should be 
understood that the invention is not limited thereto, since modifications 
may be made, and it is contemplated to cover such modifications as fall 
within the spirit and scope of the appended claims.