U.S. patent number 3,594,984 [Application Number 04/886,803] was granted by the patent office on 1971-07-27 for refining separation procedure of oxygen from air.
This patent grant is currently assigned to Kobe Steel, Ltd.. Invention is credited to Hiroetu Miki, Yukio Nakako, Sakayuki Nakanishi, Akira Toyama.
United States Patent |
3,594,984 |
Toyama , et al. |
July 27, 1971 |
REFINING SEPARATION PROCEDURE OF OXYGEN FROM AIR
Abstract
The air refining separation procedure, comprising, by using both
the moisture-carbon dioxide absorbing apparatus consisting of the
multiple fixed beds, which have two layers of a moisture absorbing
layer and a carbon dioxide absorbing layer, where four processes of
absorbing, heating regenerating, and cooling are repeated in turn,
and the nitrogen absorbing apparatus consisting of the multiple
fixed beds, where two processes of absorbing and regenerating are
repeated in turn: (a) supplying the raw air, to obtain the refined
air, into the fixed beds, which is in process of adsorption, of the
said moisture-carbon dioxide absorbing apparatus; (b) subsequently
supplying the refined air, to obtain the oxygen of low purity, into
the fixed bed, which is in process of adsorption, of the said
nitrogen absorbing apparatus; (c) supplying a part of the product
oxygen of low purity into the fixed bed, which is in process of
regeneration, of the said moisture-carbon dioxide absorbing
apparatus, and subsequently recovering it as the product oxygen of
low purity from the air refining separation apparatus; (d)
supplying the rest of the oxygen of low purity into the fixed bed,
which is in process of cooling, of the said moisture-carbon dioxide
absorbing apparatus, where it is cooled and dehydrated, and then
joining it with the low purity oxygen flow issued from the nitrogen
adsorbing apparatus; and (e) supplying the nitrogen which desorbs
from the fixed bed, which is in process of regeneration, of the
said nitrogen adsorbing apparatus, after heating, into the fixed
bed, which is in process of heating, of the said moisture-carbon
dioxide absorbing apparatus, and subsequently discharging it out
from the air refining separation apparatus.
Inventors: |
Toyama; Akira (Kobe-shi,
JA), Nakako; Yukio (Nishinomiya-shi, JA),
Nakanishi; Sakayuki (Kobe-shi, JA), Miki; Hiroetu
(Akashi-shi, JA) |
Assignee: |
Kobe Steel, Ltd. (Kobe-shi,
JA)
|
Family
ID: |
26409001 |
Appl.
No.: |
04/886,803 |
Filed: |
December 19, 1969 |
Foreign Application Priority Data
|
|
|
|
|
Dec 20, 1968 [JA] |
|
|
43/94090/68 |
|
Current U.S.
Class: |
95/126; 95/130;
95/139 |
Current CPC
Class: |
B01D
53/0407 (20130101); B01D 53/04 (20130101); B01D
2259/4009 (20130101); B01D 2257/80 (20130101); Y02C
10/08 (20130101); B01D 2259/404 (20130101); B01D
2259/4146 (20130101); Y02C 20/40 (20200801); B01D
2256/12 (20130101); B01D 2257/504 (20130101) |
Current International
Class: |
B01D
53/04 (20060101); B01d 053/03 () |
Field of
Search: |
;55/28,29,33,68,74,76,179,180 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Friedman; Reuben
Assistant Examiner: Burks; R. W.
Claims
What we claim is:
1. The air refining separation procedure, comprising, the use of
both a moisture-carbon dioxide adsorbing apparatus consisting of
the multiple fixed beds, which have two layers of a moisture
adsorbing layer and a carbon dioxide adsorbing layer, where four
processes of adsorbing, heating regenerating, and cooling are
repeated in turn, and a nitrogen adsorbing apparatus consisting of
the multiple fixed beds, where two processes of adsorbing and
regenerating are repeated in turn,
a. supplying raw air, to obtain the refined air, into the fixed
bed, which is in process of adsorption, of the said moisture-carbon
dioxide adsorbing apparatus,
b. subsequently supplying the refined air, to obtain the oxygen of
low purity, into the fixed bed, which is in process of adsorption,
of the said nitrogen adsorbing apparatus,
c. supplying a part of the separate oxygen of low purity into the
fixed bed, which is in process of regeneration, of the said
moisture-carbon dioxide adsorbing apparatus, and subsequently
recovering it as the product oxygen of low purity from the air
refining separation apparatus,
d. supplying the rest of the oxygen of low purity into the fixed
bed, which is in process of cooling, of the said moisture-carbon
dioxide adsorbing apparatus, where it is dehydrated and cooled, and
then joining it with the low purity oxygen flow issued from the
nitrogen adsorbing apparatus, and
e. supplying the nitrogen which desorbs from the fixed bed, which
is in process of regeneration, of the said nitrogen adsorbing
apparatus, after heating, into the fixed bed, which is in process
of heating, of the said moisture-carbon dioxide adsorbing
apparatus, and subsequently discharging it out from the air
refining separation apparatus.
Description
This invention relates to a refining separation procedure of oxygen
from air. Particularly saying, this invention relates to a
procedure for refining separation of oxygen from air by the
so-called adsorption method using an adsorbent for removing
moisture, carbon dioxide and nitrogen, which are included in air.
In details further, this invention relates to a procedure for
refining separation of air to obtain continuously oxygen in low
purity by adsorbing moisture and carbon dioxide in air with an
adsorbing apparatus which includes double layers of adsorbents and
then nitrogen with natural or synthetic zeolite.
Hitherto, oxygen has been produced from air by the cryogenically
liquefying rectification method or the adsorption method. Since
moisture and carbon dioxide in air bring, in the former method,
obstructive occlusion into the apparatus owing to their high
melting points and reduce, in the latter method, the adsorbability
of an adsorbent for nitrogen, they have usually been removed
previously in the foretreatment process by the cryogenically
solidifying method, the washing method and the adsorption method.
Among them, the adsorption method is effected using the adsorption
apparatus with either the fixed bed or the moving bed of the
adsorbent. In the fixed bed adsorption apparatus, the size of the
adsorber increases proportional to the interval of the
adsorption-regeneration cycle. When the heating regeneration method
is employed, it takes a relatively long time to heat up or cool
down the adsorbent, the cycle period gets longer and the size of
the apparatus is naturally enlarged, yielding troubles in
construction of the apparatus having a large capacity and an
unavoidable expensive cost. The moving bed adsorption apparatus,
where adsorption and regeneration can continuously proceed, is
suitable for treating a large amount of gas with a relatively small
amount of the adsorbent, compared with the fixed bed adsorption
apparatus. However, it has disadvantages in requiring a high degree
of technique to design the stable apparatus and consuming a large
amount of the adsorbent due to pulverization during movement in the
apparatus.
The first object of this invention is, in the refining separation
procedure of air by the adsorption method, to shorten remarkably
the cycle in the apparatus consisting of adsorbing, heating,
regenerating and cooling by using a usual fixed bed adsorber in a
specific arrangement as the adsorption apparatus for adsorbing
moisture, carbon dioxide, and nitrogen, whereby the adsorbent
amount to be used can be reduced and the size of the adsorption
apparatus is minimized.
The second object of this invention is to make enable the
adsorption apparatus to operate continuously for a long time by
using a usual fixed bed adsorber in a specific arrangement as the
adsorption apparatus, whereby the highly efficient procedure can be
offered to refining separation of air.
The third object of this invention is to simplify the system of the
air refining separation apparatus by using a usual fixed bed
adsorber in a specific arrangement as the adsorption apparatus,
whereby the maintenance and operation of the apparatus can be
easily done.
The fourth object of this invention is to avail of the whole
adsorption heat, which is generated during the adsorbing operation,
as the desorption heat, by using a usual fixed bed adsorber in a
specific arrangement as the adsorption apparatus, whereby the heat
to be supplied from the outside for heating regeneration can be
greatly reduced.
The air refining separation procedure of this invention is
characterized by using both the moisture-carbon dioxide adsorbing
apparatus comprising multiple fixed beds, which have two layers of
a moisture adsorbing layer and a carbon dioxide adsorbing layer,
where four processes of adsorbing, heating, regenerating and
cooling are repeated in turn, and the nitrogen adsorbing apparatus
comprising multiple fixed beds, where two processes of adsorbing
and regenerating are repeated in turn, and comprises:
a. supplying the raw air into the fixed bed, which is in the
adsorption step of the said moisture-carbon dioxide adsorbing
apparatus, to obtain the refined air;
b. supplying the refined air into the fixed bed, which is in the
adsorption step of the said nitrogen adsorbing apparatus, to obtain
the oxygen of low purity;
c. supplying a part of the product oxygen of low purity into the
fixed bed, which is in the regeneration step of the said
moisture-carbon dioxide adsorbing apparatus, and subsequently
recovering it as the product oxygen of low purity from the air
refining separation apparatus;
d. supplying the rest of the oxygen of low purity into the fixed
bed, which is in the cooling step of the said moisture-carbon
dioxide adsorbing apparatus, to cool and dehydrate and then joining
it with the low purity oxygen flow from the nitrogen adsorbing
apparatus; and
e. supplying the nitrogen which desorbs from the fixed bed, which
is in the regeneration step of the said nitrogen adsorbing
apparatus, after heating into the fixed bed, which is in the
heating step of the said moisture-carbon dioxide adsorbing
apparatus, and subsequently discharging out the same from the air
refining separation apparatus.
Although the adsorbing apparatus to be used in this invention is a
conventional fixed bed adsorber, its arrangement and usage are
substantially different from those of the conventional one so that
the remarkable effect is obtained as hereinafter described in
details.
In the air refining separation procedure of this invention, the
moisture-carbon dioxide adsorbing apparatus and the nitrogen
adsorbing apparatus, consisting of conventional multiple adsorbers
as shown in FIG. 1, comprise a construction so as to repeat each
process in turn by the valve operation according to the usage form.
In addition, in this invention, the adsorber so constructed in a
body with the multiple fixed beds shown in FIG. 4 as to repeat each
process in turn by rotating operation can be used.
FIG. 1 is a flow sheet showing an embodiment of this invention;
FIG. 2 is a chart showing the interrelation between the process of
the moisture-carbon dioxide adsorbing apparatus and the
valve-switching operation in the embodiment shown in FIG. 1;
FIG. 3 is a flow sheet showing another embodiment of this
invention;
FIG. 4 is a plane figure and a side view illustrating the adsorbing
apparatus to be used in the embodiment shown in FIG. 3;
FIG. 5 is a profile showing the temperature distribution and the
concentration distribution of the adsorbate in the adsorbing bed of
the moisture-carbon dioxide adsorbing apparatus in the embodiments
shown in FIGS. 1 and 3; and
FIG. 6 is a graph showing the influence of the moisture on the
nitrogen adsorbent.
As described above, the characteristics of the air refining
separation procedure of this invention lie principally in
peculiarity of the usage of the adsorber, which will be clarified
by the following illustration with the accompanying drawings.
The moisture-carbon dioxide adsorbing apparatus of the embodiments
shown in FIG. 1 consists of the combination of four groups of the
conventional fixed bed adsorbers A, B, C, D of the same kind, each
adsorber being fitted with the supplying duct 110 for the feed air,
the supplying duct 111 for the heated gas, the discharging duct 112
for the refined air, the discharging duct 113 for the product gas,
the supplying duct 114 for the product gas and the circulating
cooled gas, the discharging duct 116 for the circulating gas for
cooling and the discharging duct 115 for the heated gas. Between
each adsorber and the ducts there are set up seven electromagnetic
valves, which are so contrived together with the timer that each
adsorber can continuously remove moisture and carbon dioxide by
repeating the cycle of four processes, i.e. adsorbing, heating,
regenerating and cooling. Illustrating the example of the valve
switching shown in FIG. 2 (wherein the square indicates the opening
of the electromagnetic valve) for the process where an adsorber is
used for each of the four groups of the moisture-carbon dioxide
adsorbing apparatus as shown in FIG. 1, the adsorber A plays, on
the opening of the electromagnetic valves VA-1 and VA-1', the
adsorbing operation of the feed air flowing in through the duct 110
and the valve VA-l, and the refined air is sent through the valve
VA-1' to the duct 112. In the adsorber B, on the opening of the
valves VB-3' an VB-4, the cooling operation proceeds by means of
the cooling gas flowing in through the duct 114 and the valve
VB-3', and the said cooling gas then flows through the valve VB-4
into the discharging duct 116 for the circulating gas for cooling.
In the adsorber C, on the opening of the valves VC-3 and VC-3', the
regenerating operation proceeds by means of the regenerating gas
flowing in through the duct 114 and the valve VC-3', and the said
regenerating gas is discharged as the product gas through the valve
VC-3 and the duct 113. In the adsorber D, on the opening of the
valves VD-2' and VD-2, the heating operation proceeds by means of
the heating gas flowing in through the duct 111 and the valve
VD-2', and the said heating gas is discharged through the valve
VD-2 and the duct 115. After a given period of time elapses, the
respective electromagnetic valves are switched, and each adsorber
continuously repeats in turn the processes of adsorbing, heating,
regenerating and cooling by means of the on-off operation of the
electromagnetic valves with the timer operation, like that way as
the adsorber A from adsorbing to heating, the adsorber B from
cooling to adsorbing, and so on. In these operations, the gas
flowing in from the one side of the piping issues to the other side
of the piping at the corresponding location through the adsorber.
During this process, the adsorbing of the adsorbate on the
adsorbing bed with the gas to be treated, the heating and partially
regenerating of the adsorbing bed with the heating gas, the
desorbing of the adsorbate and the regenerating of the adsorbent
with the regenerating gas, and the cooling of the adsorbing bed
with the cooling gas proceed.
The nitrogen adsorber 105 employs a conventional fixed bed adsorber
as shown in the flow sheet of FIG. 1 and it so contrived that
adsorbing and regenerating in vacuum continuously proceed by means
of the combination of the electromagnetic valves and the timer.
Illustrating the operation, the refined air flows into the adsorber
E and the adsorption of nitrogen proceeds when the electromagnetic
valves VE-1 and VE-1' are opened and the valves VE-2 and VE-2' are
shut. On the other hand, in the adsorber F, on the opening of the
valves VF-2 and VF-2' and the shutting of the valves VF-1 and
VF-1', the desorption of the adsorbed nitrogen as well as the
regeneration of the adsorbent proceed by means of the vacuum pump
reducing the inside pressure. The electromagnetic valves
continuously change these operations with each other by the timer
operation, whereby the adsorbers E and F repeat alternately the
adsorbing and regenerating.
In the embodiment of FIG. 3, there is shown the continuous fixed
bed adsorber served as the moisture-carbon dioxide adsorber and the
nitrogen adsorber and consisting of the multiple continuous
fixed-bed adsorbent-packed layers, which are adjacent to each other
by means of partition walls, and the gas distributing sections,
which distribute the gases to be supplied to and discharged from
the said adsorbent-packed layers. It is so constructed that either
of the said adsorbent-packed layers and the gas distributing
sections can rotate.
The moisture-carbon dioxide adsorber 104, shown in FIG. 3, consists
of, as shown in FIG. 4-1 and FIG. 4-2, three portions, i.e. the
adsorbing bed A, which is fixed on the freely rotatable central
axis 15 settled on the bearings 20 fixed at the centers of the
upper and lower surfaces of the apparatus body, and the
distributing sections B and B', which are so fixed to the frame 19
as to contact on the upper and lower surfaces of this adsorbing
bed. The adsorbing bed A is divided with the partition walls 2
welded to the central axis 15 and the outer cylinder 5 into the
radially ordered small chambers, on the upper and lower surfaces of
which are settled either the metal gauzes or the perforated plates
6 and 7 having the adequate opening area required for the
adsorbents 1 not to leak and for the gas to flow freely, and in the
space of which are the adsorbents packed. On the outer cylinder 5
of this adsorbing bed A, the driving devices 8 and 9 are settled,
and the adsorbing bed A is rotated by this driving device toward
the definite direction at the constant speed. The distributing
sections B and B' settled at the upper and lower positions of this
adsorbing bed A are divided respectively with the parting strips 10
into four divisions for adsorbing, heating, regenerating, and
precooling at the corresponding positions of B and B',
respectively. When the same gas is used for both regenerating and
precooling, either one of the distributing sections is divided into
three portions. In the embodiment of FIG. 3 and also in FIG. 4-1
and FIG. 4-2, the distributing section B is divided into three
portions and the distributing section B' is divided into four
portions.
The said parting strip 10 is fixed to the outer cylinder 21, the
upper and lower plates 17 and the central tube 4, respectively, by
means of such as to keep airtight. Each contact portion of the
parting strip 10 to the adsorbing bed A is fitted with the sealing
plate 11 which has the size greater than at least one of the
adsorbing chambers radially ordered, and it is so constructed to
seal the contact portion between the sealing plate 11 and the end
surface of the partition wall 2. Also, the contact portion between
the outer cylinder 5 of the adsorbing bed and the outer cylinder 21
of the distributing section has an airtight construction. Thus, the
distributing chambers are kept to be perfectly airtight to each
other and to atmosphere. Each of the distributing sections B and B'
is provided with the raw material air supplying duct 110, the
heating gas supplying duct 111, the refined air discharging duct
112, the product gas discharging duct 113, the supplying duct 114
for the product gas and the circulating gas for cooling, the
discharging duct 116 for the circulating gas for cooling and the
heating gas discharging duct 115. The gas flowing in from the one
side of these ducts, goes through the adsorbing bed A into the
other side of the ducts at the corresponding position. During this
process, the adsorbing of the adsorbate on the adsorbing bed with
the gas to be treated, the heating and partially regenerating of
the adsorbing bed with the heating gas, the desorbing of the
adsorbate and the regenerating of the adsorbent with the
regenerating gas, and the cooling of the adsorbing bed with the
precooling gas take place.
In the nitrogen adsorber 105 shown in FIG. 3, each adsorbing
chamber carries the adsorbing-regenerating cycle out at a definite
period, by means of rotation of the distributing sections, which
are settled on the upper and lower surfaces of the multiple
adsorbing chambers adjacent to each other by means of the partition
walls, as shown in FIG. 4-3 and FIG. 4-4. To illustrate the
construction, the outside of the apparatus consists of the cylinder
5 and the upper and lower covers 17, and, at the middle of the
inside, the adsorbing section A consisting of a series of the fixed
bed adsorbing chambers 3 packed with the adsorbent 1. These
chambers 3 are divided by means of the outer cylinder 5 of the
apparatus, the inner cylinder 4 having the concentric axis
therewith, the partition walls 2 to prevent the mingling of gases,
which are welded firmly to both of the said cylinders, and the
upper surface 7 and the lower surface 6 formed with the perforated
plate or the metal gauze having the adequate opening area required
for the gas to flow freely and for the adsorbent not to leak. At
the central portion of the apparatus, the central tube 15, which is
rotatable and internally touched to the inner cylinder 4, is
settled, being connected with the duct 118, which is fixed to the
upper and lower covers 17 by means of the airtight joint 16. To
this central tube 15, the duct 12 leading to the adsorbing chamber
3 is fitted at the upper and lower sides, whereby the desorbed gas
from the adsorbing chamber can be discharged to the outside of the
apparatus through the tube 15 and the duct 118. At the front and
rear of the duct 12, the sealing plates 11 are fitted, and the
respective contact portions between these sealing plates 11 and the
upper and lower end surfaces of the parting walls 2 are furnished
with the sealing devices, to prevent the gas leakage at the
adsorbing and regenerating sections. It is so contrived that the
central tube 15, which is fitted with the duct 12 and the sealing
plates 11, is made revolved by revolving the revolving body 9 at a
constant speed by means of the driving devices 8. In FIG. 4-3, a
single duct 12 is settled, respectively, at the corresponding
positions to the upper and lower sides, but it is possible to set
up the duct in two portions at the symmetrical positions for good
balance. For such a case, the sealing plates 11 must be settled at
the front and rear of the respective ducts 12. The outer cylinder 5
is fitted with the ducts 112 and 121, respectively, at the upper
and lower sides and the gas flows in and out through these two
ducts. Namely, the raw gas supplied at the duct 112 flows in the
adsorbing chamber 3 of the adsorbing operation section, where the
adsorbate is removed by adsorption, and goes out from the duct 121
to the outside as the product gas. On the other hand, in the
adsorbing chamber, which contacts at the upper and lower surfaces 6
and 7 to the duct 12, the regenerating operation is carried out at
a lower inside pressure by employing a vacuum pump (not indicated
in FIGURES) connected with the duct 118. As the ducts 15 and 12
rotate by means of the revolving device 8, the process in the
adsorbing chamber changes from adsorbing to regenerating in vacuum,
in turn. During this operation, the adsorbing chamber is sealed for
a moment with the sealing plate 11, the raw gas is interrupted to
flow in. The said adsorbing chamber gets to connect with the duct
12 by rotation of the ducts 15 and 12, and to carry the
regenerating process out. The sealing plates 11 should be those
having such width as to cover at least one of the adsorbing
chambers for carrying the adsorbing and regenerating processes out
smoothly.
As understood from the above descriptions, the adsorbent in the
adsorbing chamber is fixed as in the fixed bed adsorber. On the
other hand, the movement of the ducts relative to the adsorbing
chamber makes it possible to subject the adsorbent to adsorption
and regeneration in continuation. Therefore, the adsorbing
apparatus in this invention can treat a great amount of gas with
only a small amount of the adsorbent, not consuming the adsorbent
caused by pulverization as seen in the moving bed adsorbing
apparatus.
According to this invention, the air refining separation is done by
the following new process, based on the specific usage form of the
adsorbing apparatus as described above.
To illustrate the air refining separation procedure of this
invention with the representative example in FIG. 1, the natural
air including moisture and carbon dioxide, after solid components
such as dust are removed by a simple filter 100, flows through the
duct 109 into the blower 101 for raising pressure up to the
necessary pressure for the apparatus, and is further introduced
into the moisture-carbon dioxide adsorbing apparatus through the
duct 110. The raw air flows then into the adsorbing bed consisting
of two layers, i.e. a moisture adsorbing layer a and a carbon
dioxide adsorbing layer b. The majority of moisture is removed
during passing through the adsorbing layer a, and the remaining
moisture in trace and carbon dioxide are removed on passing through
the adsorbing layer b. When the adsorbing bed gets to adsorb
moisture to 40--60 percent of the saturated adsorption capacity, it
is transferred by the valve switching operation to the heating as
the next process. The adsorption heat evolved at the adsorbing
layers accumulates in the adsorbent in the adsorbing bed, and the
refined air goes out at a temperature nearly close to the inlet
temperature. Accordingly, at the end of the adsorbing operation,
the adsorption profile in the adsorbing bed gets to the pattern of
A-1 in FIG. 5-2, showing the concentration distribution of the
adsorbate in the adsorbing layer, where the parts indicated by X
and X' show the saturated state or nearly for moisture and carbon
dioxide, respectively. The temperature distribution at this state
affords as shown by A-1 of FIG. 5-1, the mountain-shaped curve
having the nearly same temperatures at the air inlet and outlet
portions and the highest at the adsorption zone. This means that
the adsorption heat evolved by adsorption is all retained in the
adsorbing layers. In the adsorbing layer a, the adsorbent (e.g.
silica gel, alumina gel) having a large adsorption capacity in the
high relative humidity region is used. In the adsorbing layer b,
the adsorbent (e.g. natural zeolite, synthetic zeolite) having a
strong adsorption ability in the low relative humidity region and
an adsorption ability of carbon dioxide at normal temperatures.
The desorbing nitrogen, which is heated at the heater 108, flows
through the duct 111 into the adsorbing bed, which has been
transfered to the heating section A-2. After heating a part of the
inlet side of the adsorbing layers b and a, removing the adsorption
heat accumulated in the adsorbing bed to the moisture adsorbing
section formed in the air inlet side of the adsorbing layer a,
desorbing a part of the adsorbed moisture and getting to the nearly
same low temperature as of the raw air simultaneously with
retention of moisture and carbon dioxide, the nitrogen flows out.
The majority of the adsorbed carbon dioxide in the adsorbing layer
b is desorbed off during the said process. Accordingly, as shown in
FIG. 5-1, by means that the adsorbing layer b is heated with the
heated desorbing nitrogen, the temperature of the said adsorbing
layer increases, and the majority of carbon dioxide are desorbed as
shown in FIG. 5-2, while in the adsorbing layer a, by means of the
flowing of the heated desorbing nitrogen, the high temperature zone
moves upward, and thereby, a part of the adsorbed moisture is
desorbed, and the height of the saturated adsorption section X
becomes low. By further switching the valves, the adsorbing bed is
transferred to the regenerating section A-3. In the regenerating
operation, the product oxygen coming through the duct 114 flows
through the adsorbing bed, moving further the high temperature
zone, which has been formed in the adsorbing layer by the
adsorption heat in the previous adsorbing operation A-1, and by the
flowing of the hot desorbing nitrogen in the heating operation, to
the moisture adsorbing section of the adsorbing bed at the air
inlet side, and regenerating the adsorbent. The product oxygen flow
issues out of the apparatus at the nearly same temperature as of
the inlet air, containing the desorbed moisture and carbon dioxide.
On the other hand, the adsorbing bed is made almost free from the
adsorbed moisture and carbon dioxide in the regenerating section
A-3. The high temperature zone caused by adsorption heat in the
adsorbing section A-1 of the adsorbing bed is removed by desorption
heat nearly equal thereto in the absolute value of calory to remain
in the adsorbing layer a the high temperature zone formed in the
heating section A-2. Therefore, in the adsorbing bed, the
temperature distribution as shown in FIG. 5-1 is established, and
moisture in the adsorbent is mostly desorbed, as shown in FIG. 5-2.
The adsorbing bed of this state is transfered to the cooling
operation. In the cooling section A-4, a part of the product gas to
be circulated as the cooling gas, flows through the adsorbing bed
as in the regenerating section A-3, removing completely the said
high temperature zone, which has been retained in the adsorbing
layer, to the outside of the adsorbing bed, and accordingly, the
high temperature zone is completely eliminated as the result of the
changing of the temperature distribution along the course of 1, 2
and 3 in turn, as shown in FIG. 5-1. During this process, the
remaining moisture is completely desorbed, and the regenerating and
cooling operations of the adsorbing bed are completed. This
regenerating of the adsorbent can be carried out more completely,
due to the passing of the high temperature zone, which has been
formed in the heating section A-3, through the adsorbing bed during
the regenerating and cooling operations. On the other hand, the
cooling gas issues out at the relatively high temperature,
accompanied by a very small amount of moisture, being cooled at the
cooler 107 after passing through the duct 116, being dried
sufficiently at the desiccator 106 after passing through the duct
117, and being furnished through the duct 114 for the cooling
operation. Because of extremely low relative humidity of this
cooling gas, natural zeolite or synthetic zeolite is suitable for
the desiccant of the desiccator. The air refined in the
moisture-carbon dioxide adsorbing apparatus 104 is introduced into
the nitrogen adsorbing apparatus 105 through the duct 112. The
refined gas introduced flows into the one of the fixed bed
adsorbers, which have the similar construction to the
moisture-carbon dioxide adsorbing apparatus. Each adsorber is
packed with natural zeolite or synthetic zeolite as the adsorbent,
which can adsorb larger amounts of nitrogen than oxygen at the
temperature close to the normal temperature. During the passing of
the refined air, which has flowed in, through this adsorbing bed,
nitrogen in the air is adsorbed, and oxygen in the rest air is
enriched, issuing out as the product oxygen through the duct 114,
being supplied to the regenerating operation of the said
moisture-carbon dioxide adsorbing apparatus 104, and finally,
flowing out as the product oxygen through the duct 113 to the
outside of the apparatus. On the other hand, the nitrogen, which
has been adsorbed in the adsorbing layer of the nitrogen adsorber,
is desorbed adiabatically under the reduced pressure by the vacuum
pump 103, and discharged through the duct 118, being supplied to
the heating operation of the moisture-carbon dioxide adsorbing
apparatus 104 through the duct 119, the heater 108, and the duct
111, and finally, being exhausted as the waste nitrogen through the
duct 115 to the atmosphere.
In addition, in the procedure of this invention, if it is required
to obtain the clean low purity oxygen having no moisture and carbon
dioxide, a part of it can be taken out from the duct 120. According
to the procedure of this invention, the processes were carried out
under the conditions as indicated in Table 1, by employing the
moisture-carbon dioxide adsorbing apparatus 104, which consists of
the eight adsorbers, where the moisture adsorbing layer a is packed
with alumina gel, the carbon dioxide adsorbing layer b is packed
with natural zeolite, and the adsorbing layer of the nitrogen
adsorbing apparatus 105 is packed with natural zeolite, and
thereby, about 27 Nm.sup.3 /hr of the low purity product oxygen,
which contains about 35 percent oxygen, were obtained from 50
Nm.sup.3 /hr of the raw air. In the moisture-carbon dioxide
adsorbing apparatus of this case, the numbers of the adsorber were
so assigned to the respective processes as follows; three to
adsorbing, one to heating, two to regenerating, and two to cooling.
##SPC1##
The resulting amounts of the removed moisture and the removed
carbon dioxide are those shown in Table 2. ##SPC2##
Although it is possible as described before to use synthetic
zeolite as the adsorbent, nitrogen adsorbing ability of the both
being listed in Table 3, cheaper natural zeolite is excellent in
adsorbing ability and was the preferably adequate adsorbent for
that use. ##SPC3##
N.z. ... natural zeolite
M.s. synthetic zeolite (means Molecular Sieves)
The nitrogen adsorbability of the said adsorbent for nitrogen is
influenced by moisture and carbon dioxide in the gas. The influence
by moisture is especially remarkable as shown in FIG. 4, and it
must be completely removed in the moisture-carbon dioxide adsorbing
apparatus. Thus, it was necessary to dry the cooling gas up to the
value (a dew-point below -55.degree. C) as shown in Table 3, by
means of such adsorbents suitable for drying the gas of low
relative humidity as natural zeolite or synthetic zeolite.
As specified above, according to the procedure of this invention
for producing the low purity oxygen, the following effects can be
obtained:
1. Conventional fixed bed adsorbers are employed as the
moisture-carbon dioxide adsorbing apparatus and the nitrogen
adsorbing apparatus. Because of the feature particularly in the
adsorbing and regenerating procedures of the moisture-carbon
dioxide adsorbing apparatus, however, the cycle of adsorbing,
heating, regenerating and cooling can be markedly shortened whereby
the amount of the adsorbent as well as the size of the apparatus
can be minimized to more or less 1/10 of the conventional one and
further the operation of the process can be made continuous;
2. Due to employing the continuous fixed bed adsorbing apparatus,
the flow-system is very simple, and the operation and maintenance
are quite easy;
3. Since the adsorption heat evolved in adsorbing moisture is
effectively utilizable as desorption heat, only a little amount of
heat to be supplied from the outside is needed for heating and
regenerating;
4. Since the product oxygen and the desorbing nitrogen, both of
which have no moisture and carbon dioxide, are employed as the
regenerating gas for the adsorbent of the moisture-carbon dioxide
adsorbing apparatus, the cost for power consumption can be markedly
saved; and
5. Since the high temperature zone, which is formed by the
desorbing nitrogen heated in the process of heating operation of
the moisture-carbon dioxide adsorbing apparatus, moves through the
adsorbing layer during the regenerating and cooling operations, the
adsorption of moisture and carbon dioxide can be accomplished
completely.
* * * * *