[0001] The present invention relates to a high-purity oxygen production method and an air
separation apparatus for producing high-purity oxygen.
[0002] As high-purity oxygen production methods in which components having a higher boiling
point or a lower boiling point than oxygen are controlled to the order of ppm or less,
there are known methods that employ cryogenic air separation. One such production
method that can be cited is a method in which an oxygen-containing liquid or gas is
discharged from a cryogenic air separation apparatus, and high-purity oxygen is rectified
(see, for example,
WO2018/219685 A1).
[0003] In order to rectify high-purity oxygen, a step is required in which feedstock liquefied
oxygen is heated to vaporise low boiling point components such as nitrogen and argon,
and as a heat medium for this process, it is known to use an oxygen-enriched liquid
(
WO2018/219685 A1), feed air (
WO2014/173496 A2), recycled air (
JP 2020-173041), and nitrogen gas (
US11549747).
[0004] If a process liquid such as an oxygen-enriched liquid is used as the heat medium,
as in
WO2018/219685, since the sensible heat of the process liquid is used to provide the latent heat
of vaporisation of the liquefied oxygen, a large molar flow rate is required, while
at the same time the amount of heat supplied is limited by process balance constraints,
and as a result there is a problem in that the amount of high-purity oxygen that can
be recovered remains small.
[0005] In the methods of
WO2014/173496 A2,
JP 2020-173041 and
US11549747, the flow rate of the feed air, recycled air, or nitrogen gas used to vaporise the
liquefied oxygen can be increased, so there are no constraints on the high-purity
oxygen production capacity, but there is another problem in that the methods involve
a gas compression process, and thus energy consumption is high.
[0006] The present disclosure provides a high-purity oxygen production method and an air
separation apparatus for producing high-purity oxygen, with which energy consumption
is reduced even while a process gas is used as a heat medium for liquefied oxygen,
so as to avoid high-purity oxygen production capacity constraints.
US 2023/0038170 relates to a process for oxygen production at 99.8% content whereas the present invention
allows oxygen to be produced with ppm order impurities. The liquid fed to the oxygen
column comes from the liquid sump at the bottom of the column fed by the feed air,
where hydrocarbons from feed air are accumulated.
[0007] According to the invention the feed (oxygen containing stream) to the pure oxygen
column is comes from a section where hydrocarbons (eg. methane) have been removed.
[0008] When condensable gas is introduced as a heat source for oxygen reboil, the difference
between the boiling point of oxygen and the ΔT of the heat exchanger determine the
saturation temperature and pressure of the condensable gas. Principally, the lower
the saturation pressure, the less energy is needed for reboil. The present invention
uses oxygen-enriched gas for oxygen reboil, where the saturation pressure can be lower
than pure nitrogen.
[0009] According to the invention, there is provided a method for producing high purity
oxygen, comprising the following steps:
- a nitrogen and oxygen separation step of introducing a feed air cooled by a main heat
exchanger to a lower section of a first nitrogen rectification column, and introducing
oxygen-enriched liquid removed from the bottom of the first nitrogen rectification
column into a rectification section of a second nitrogen rectification column and
separating the feed air into a nitrogen-enriched component and an oxygen-enriched
component in the first nitrogen rectification column and the second nitrogen rectification
column;
- a first nitrogen condensation step of condensing vapor stream from the first nitrogen
rectification column in a first nitrogen condenser;
- a second nitrogen condensation step of condensing vapor stream from the second nitrogen
rectification column in a second nitrogen condenser;
- a high-purity oxygen production step of introducing an oxygen-containing fluid removed
from the rectification section of the second nitrogen rectification column into a
high-purity oxygen rectification column and producing high-purity product oxygen by
using an oxygen evaporator; and
- a heating medium utilization step of using gas removed from the bottom of the second
nitrogen rectification column as a heat medium for the oxygen evaporator which evaporates
liquefied oxygen, and returning the gas to the second nitrogen condenser.
[0010] According to optional features, the method comprises:
- a partial feed air introduction step of compressing part of the feed air by a compressor,
cooling the compressed part of the feed air in a main heat exchanger and expanding
the feed air by an expansion turbine, and introducing the feed air into the second
nitrogen rectification column;
- expanding in a turbine a vapor formed by vaporising liquid in the second condenser;
- pressuring nitrogen condensed in the second condenser in a pump and sending the pressurised
condensed nitrogen to the top of the first nitrogen rectification column;
- the oxygen-containing fluid removed from the rectification section of the second nitrogen
rectification column is introduced into the high-purity oxygen rectification column
as the sole feed for the high-purity oxygen rectification column;
- oxygen-enriched liquid removed from the bottom of the first nitrogen rectification
column is introduced into a rectification section of a second nitrogen rectification
column at a point below the point from which the oxygen-containing fluid removed from
the rectification section of the second nitrogen rectification column;
In the present disclosure, a fluid that is discharged from a rectification stage of
the rectification column above an introduction point of the feed air, recycled air,
or oxygen-enriched liquid and that is introduced into the high-purity oxygen rectification
column is referred to as oxygen-containing fluid, and a liquid discharged below the
feed air introduction stage (for example, the bottom portion of the nitrogen rectification
column) is referred to as oxygen-enriched liquid.
[0011] The oxygen-containing fluid may be a liquid or a gas-liquid mixture.
[0012] With this configuration, the nitrogen gas in the vapour stream is caused to exchange
heat with the oxygen-enriched liquid in the nitrogen condenser, thereby vaporising
the oxygen-enriched liquid to generate oxygen-enriched gas. The oxygen-enriched gas,
which is utilised as a heat medium for the oxygen evaporator, has a pressure and composition
sufficient to vaporise the rectified liquefied oxygen in the bottom portion of the
high-purity oxygen rectification column using latent heat. In particular, since oxygen-enriched
gas containing a large amount of oxygen can vaporise liquefied oxygen at a lower pressure
than air or nitrogen, liquefied oxygen can be vaporised at the supply pressure from
the nitrogen evaporator without the use of a com pressor.
[0013] The oxygen-containing gas condensed (re-liquefied) in the oxygen evaporator may be
re-supplied to the nitrogen condenser.
[0014] With this configuration, recondensed oxygen enriched liquid obtained by condensing
the oxygen enriched gas in the oxygen evaporator is re-supplied to a refrigerant side
of the nitrogen condenser and vaporised through heat exchange with the vapour stream
(nitrogen gas). The recondensed oxygen enriched liquid may be delivered to the nitrogen
condenser by means of a head pressure utilizing a height difference between the oxygen
evaporator and the nitrogen condenser.
[0015] If the oxygen evaporator is disposed at a lower position than the nitrogen condenser,
delivery may be effected using a pump.
[0016] The nitrogen rectification column may include a rectification portion for separating
high boiling-point components (for example, methane) from the oxygen contained in
the supplied feed air, and for discharging an oxygen-containing liquid from an upper
stage thereof.
[0017] With this configuration, the high boiling-point components contained in the feed
air are concentrated in the liquefied oxygen. The oxygen-containing liquid serving
as the feedstock for the high-purity oxygen is obtained by discharging some reflux
liquid from above the feed air introduction portion of the nitrogen rectification
column as the oxygen-containing liquid, the reflux liquid containing sufficient oxygen
to serve as a feedstock for the high-purity oxygen while having high boiling-point
components removed sufficiently. A rectification portion is disposed midway between
the feed air introduction portion and the oxygen-containing liquid discharge portion,
and is configured such that high boiling-point components removed from the feed air
are transferred into the liquefied oxygen by gas-liquid contact and are concentrated
in the lower portion of the rectification column.
[0018] The rectification portion may consist of rectification plates, structured packing,
or random packing.
[0019] A high-purity oxygen production method includes:
- a nitrogen-oxygen separation step in which feed air cooled in (partially cooled by
being discharged from an intermediate part of) a main heat exchanger (1) is introduced
into an introduction portion in a lower part of a nitrogen rectification column, and
the feed air is separated in first and second nitrogen rectification columns into
a nitrogen-enriched component (nitrogen-enriched fluid) and an oxygen-enriched component
(oxygen-enriched fluid);
- a first nitrogen condensation step in which a vapour stream (nitrogen-enriched gas)
from the first nitrogen rectification column is condensed in a first nitrogen condenser;
- an oxygen-enriched liquid circulation step in which oxygen-enriched liquid discharged
from a bottom portion of the nitrogen rectification column is passed through the main
heat exchanger and is then sent to a rectification portion of the second nitrogen
rectification column;
- a second nitrogen condensation step in which a vapour stream (nitrogen-enriched gas)
from the second nitrogen rectification column is condensed in a second nitrogen condenser;
- a product nitrogen gas extraction step in which gas (nitrogen gas) discharged from
a top portion of the first nitrogen rectification column is passed through the main
heat exchanger and is extracted as product nitrogen gas;
- a waste gas extraction step in which gas (nitrogen gas) discharged from a top portion
of the second nitrogen condenser is passed through a portion of the main heat exchanger,
is then expanded and cooled in an expansion turbine, and is then passed through the
main heat exchanger again and is extracted as waste gas;
- a high-purity oxygen production step in which an oxygen-containing fluid discharged
from a rectification portion of the second nitrogen rectification column is introduced
into a top portion of a high-purity oxygen rectification column, and an oxygen evaporator
provided in a bottom portion is utilised to produce high-purity oxygen;
- a heat medium utilisation step in which gas (oxygen-enriched gas) discharged from
a bottom portion of the second nitrogen rectification column or a top portion of the
first nitrogen condenser is utilised as a heat medium for the oxygen evaporator which
vaporises liquefied oxygen, and is returned to the top portion of the nitrogen condenser;
and
- a recycled gas introduction step in which gas discharged from the rectification portion
of the second nitrogen rectification column is compressed by a compressor, is passed
through the main heat exchanger, and is then introduced as recycled gas into a lower
part of the first nitrogen rectification column.
[0020] A fourth high-purity oxygen production method includes:
- a partial feed air introduction step in which feed air compressed by a compressor
is passed through (partially cooled by being discharged from an intermediate part
of) a main heat exchanger, is expanded in an expansion turbine, and is introduced
into a second nitrogen rectification column;
- a nitrogen-oxygen separation step in which feed air cooled in (partially cooled by
being discharged from an intermediate part of) a main heat exchanger is introduced
into an introduction portion in a lower part of a nitrogen rectification column, and
the feed air is separated in first and second nitrogen rectification columns into
a nitrogen-enriched component (nitrogen-enriched fluid) and an oxygen-enriched component
(oxygen-enriched fluid);
- a first nitrogen condensation step in which a vapour stream (nitrogen-enriched gas)
from the first nitrogen rectification column is condensed in a first nitrogen condenser;
- an oxygen-enriched liquid circulation step in which oxygen-enriched liquid discharged
from a bottom portion of the first nitrogen rectification column is passed through
the main heat exchanger and is then sent to a rectification portion of the second
nitrogen rectification column;
- a second nitrogen condensation step in which a vapour stream (nitrogen-enriched gas)
from the second nitrogen rectification column is condensed in a second nitrogen condenser;
- a product nitrogen gas extraction step in which gas (nitrogen gas) discharged from
a top portion of the first nitrogen rectification column is passed through the main
heat exchanger and is extracted as product nitrogen gas;
- a low-pressure nitrogen gas extraction step in which gas (nitrogen gas) discharged
from a top portion of the second nitrogen rectification column is passed through the
main heat exchanger and is extracted as low-pressure nitrogen gas;
- a waste gas extraction step in which gas (nitrogen gas) discharged from a top portion
of the second nitrogen condenser is passed through the main heat exchanger and is
extracted as waste gas;
- a high-purity oxygen production step in which an oxygen-containing fluid discharged
from the rectification portion of the second nitrogen rectification column is introduced
into a top portion of the high-purity oxygen rectification column, and an oxygen evaporator
provided in a bottom portion is utilised to produce high-purity oxygen; and
- a heat medium utilisation step in which gas (oxygen-enriched gas) discharged from
a bottom portion of the second nitrogen rectification column or a top portion of the
first nitrogen condenser is utilised as a heat medium for the oxygen evaporator which
vaporises liquefied oxygen, and is returned to the top portion of the second nitrogen
condenser.
[0021] The first, second, third and fourth high-purity oxygen production methods may include
a waste gas extraction step in which gas discharged from the top portion of the high-purity
oxygen rectification column is passed through the main heat exchanger and is extracted
as waste gas.
[0022] "High-purity oxygen" is oxygen having a concentration of at least 99.99% mol. According
to the present invention, there is provided an air separation apparatus for producing
high purity oxygen, comprising:
- a main heat exchanger;
- a first nitrogen rectification column;
- a second nitrogen rectification column;
- a first nitrogen condenser at the top of the first nitrogen rectification column;
- a second nitrogen condenser at the top of the second nitrogen rectification column;
- a high purity oxygen rectification column;
- an oxygen evaporator at the bottom of the rectification column;
- a conduit for introducing feed air cooled by a main heat exchanger to a lower section
of a first nitrogen rectification column in order to separate the feed air into a
nitrogen-enriched component and an oxygen-enriched component in the first nitrogen
rectification column;
- a conduit for introducing oxygen-enriched liquid removed from the bottom of the first
nitrogen rectification column into a rectification section of a second nitrogen rectification
column in order to separate the oxygen enriched liquid into a nitrogen-enriched component
and an oxygen-enriched component in the second nitrogen rectification column;
- a conduit for sending a nitrogen enriched vapor stream from the first nitrogen rectification
column in the first nitrogen condenser;
- a conduit for sending a nitrogen enriched vapor stream from the second nitrogen rectification
column in the second nitrogen condenser;
- a conduit for sending an oxygen-containing fluid removed from the rectification section
of the second nitrogen rectification column into the high-purity oxygen rectification
column and producing high-purity product oxygen at the bottom of the high purity oxygen
rectification column and
- a conduit for sending gas removed from the bottom of the second nitrogen rectification
column as a heat medium for the oxygen evaporator which evaporates liquefied oxygen,
and returning the gas condensed in the oxygen evaporator to the second nitrogen condenser.
[0023] The air separation apparatus may comprise:
- an oxygen-enriched liquid pipeline through which oxygen-enriched liquid discharged
from a bottom portion of the first nitrogen rectification column is passed partially
through the main heat exchanger and is then sent to a rectification portion of the
second nitrogen rectification column;
- an oxygen-containing fluid pipeline through which oxygen-containing fluid discharged
from a middle-stage rectification portion of the second nitrogen rectification column
is introduced into a top portion of the high-purity oxygen rectification column;
- a heat medium pipeline through which gas discharged from a lower-stage rectification
portion of the second nitrogen rectification column is sent as a heat medium of the
oxygen evaporator and is introduced as liquefied gas into the second nitrogen condenser;
- a recycled gas pipeline through which gas discharged from the middle-stage rectification
portion of the second nitrogen rectification column is compressed by the compressor,
is passed through the main heat exchanger, and is then introduced as recycled gas
into the rectification portion of the first nitrogen rectification column;
- a waste gas extraction pipeline through which gas discharged from the top portion
of the second nitrogen condenser is passed partially through the main heat exchanger,
is then sent to the expansion turbine, is again passed through the main heat exchanger,
and is extracted as waste gas;
- a turbine, a conduit for sending air to the turbine and a conduit for sending expanded
air from the turbine to the second nitrogen rectification column;
- a turbine, a conduit for sending gas from the second nitrogen condenser to the turbine
and a conduit for sending expanded gas from the turbine to the atmosphere;
- a compressor, a conduit for sending gas from between intermediate stages of the second
nitrogen rectification column to the compressor and a conduit for sending compressed
gas from the compressor to the bottom of the first nitrogen rectification column;
- an arrival point for the gaseous air in the first nitrogen rectification column is
above an arrival point for the gas compressed in the compressor;
- the compressor is coupled to the turbine;
- means for sending condensed nitrogen from the second condenser to the top of the first
nitrogen rectification column;
- means for sending a top gas from the oxygen rectification column to the main heat
exchanger.
[0024] Further, a fourth air separation apparatus may comprise:
- a compressor for compressing a portion of the feed air, and
- an expansion turbine for expanding compressed air that has been compressed by the
compressor, introduced into the main heat exchanger, and discharged from an intermediate
part thereof.
[0025] The air separation apparatus may comprise:
- a feed air branch pipeline which sends a portion of the feed air to the compressor
that compresses the feed air, sends the feed air compressed by the compressor to the
main heat exchanger and discharges the same from an intermediate part thereof to the
expansion turbine to expand the feed air, and then sends the feed air to the rectification
portion of the second nitrogen rectification column;
- a low-pressure nitrogen gas extraction pipeline through which gas discharged from
a top portion of the second nitrogen rectification column is extracted as low-pressure
nitrogen gas; and
- a waste gas extraction pipeline through which gas discharged from the top portion
of the second nitrogen condenser is extracted as waste gas.
[0026] The air separation apparatus may include:
- various measuring instruments such as flow rate measuring instruments, pressure measuring
instruments, temperature measuring instruments, and liquid level measuring instruments;
- various valves such as control valves and gate valves; and
- piping that connects each element.
[0027] Energy consumption can be reduced even while using a process gas as a heat medium
for liquefied oxygen, so as to avoid high-purity oxygen production capacity constraints.
[Figure 1] is a drawing illustrating an air separation apparatus according to a comparative
example.
[Figure 2] is a drawing illustrating an air separation apparatus according to a comparative
example.
[Figure 3] is a drawing illustrating an air separation apparatus according to the
invention.
[Figure 4] is a drawing illustrating an air separation apparatus according to the
invention.
[0028] The first air separation apparatus A1 according to a comparative example will be
described with reference to Figure 1.
[0029] The first air separation apparatus A1 comprises a main heat exchanger 1, a nitrogen
rectification column 2, a nitrogen condenser 3, an expansion turbine 92, a high-purity
oxygen rectification column 5, and an oxygen evaporator 6.
[0030] The main heat exchanger 1 cools feed air introduced from a hot end and discharges
the same from a cold end. The cooled feed air is introduced into the nitrogen rectification
column 2 via a feed air pipeline L1.
[0031] The nitrogen rectification column 2 comprises a bottom portion 21, a rectification
portion 22, and a top portion 23. The feed air pipeline L1 is connected to the bottom
portion 21.
[0032] Oxygen-enriched liquid that collects in the bottom portion 21 is sent to a refrigerant
phase 31 of the nitrogen condenser 3 via an oxygen-enriched liquid pipeline L21.
[0033] The nitrogen condenser 3 is provided above the top portion 23. A portion of nitrogen
gas (vapour stream) discharged from the top 23 of the nitrogen rectification column
2 is introduced into the nitrogen condenser 3 via a reflux pipeline L231, and is cooled
(condensed) through heat exchange with the oxygen-enriched liquid to form liquefied
nitrogen. The liquefied nitrogen is returned to the top portion 23 of the nitrogen
rectification column 2 as reflux liquid.
[0034] An oxygen-containing fluid is discharged from between intermediate portions 221,
222 of the rectification portion 22 of the nitrogen rectification column 2 via the
oxygen-containing fluid pipeline L221 and is introduced into a top portion 53 of the
high-purity oxygen rectification column 5.
[0035] Nitrogen gas discharged from the top portion 23 of the nitrogen rectification column
2 is sent via a product nitrogen gas extraction pipeline L23 to the main heat exchanger
1 and is extracted as product nitrogen gas.
[0036] Oxygen-enriched gas (oxygen-enriched liquid vapour) discharged from a top portion
31 of the nitrogen condenser 3 is introduced via a waste gas extraction pipeline L31
into the cold end of the main heat exchanger 1, is discharged from an intermediate
part thereof, is then expanded and cooled in the expansion turbine 92, and is again
sent to the main heat exchanger 1 and is extracted as waste gas.
[0037] A portion of the oxygen-enriched gas (oxygen-enriched liquid vapour) discharged from
the top portion (refrigerant phase) 31 of the nitrogen condenser 3 is sent as a heat
medium via a heat medium pipeline L311 to the oxygen evaporator 6, is re-liquefied,
and is returned again to the top portion (refrigerant phase) 31 of the nitrogen condenser
3. The re-liquefied oxygen-enriched gas is supplied as a recycled oxygen-enriched
liquid to the nitrogen condenser 3, as a refrigerant.
[0038] The high-purity oxygen rectification column 5 includes a bottom portion 51, a rectification
portion 52, and a top portion 53.
[0039] Oxygen-containing liquid is introduced into the top portion 53 of the high-purity
oxygen rectification column 5 and is rectified in the rectification portion 52, and
liquefied oxygen collects in the bottom portion 51.
[0040] The oxygen evaporator 6 is provided in the bottom portion 51 of the high-purity oxygen
rectification column 5. Liquid oxygen is converted into a vapour stream (oxygen gas)
by the heat medium nitrogen gas in the oxygen evaporator 6, heat and material are
exchanged in the rectification portion 52, and high-purity oxygen accumulates in the
bottom portion 51. Gas discharged from the top portion 53 of the high-purity oxygen
rectification column 5 passes through a pipeline L53 to merge with the waste gas extraction
pipeline L31, is sent to the main heat exchanger 1, and is extracted as waste gas.
[0041] According to the air separation apparatus A1, coldness necessary to maintain the
heat balance of the air separation apparatus can be supplied.
[0042] The second air separation apparatus A2 according to the comparative example will
be described with reference to Figure 2. The same reference numerals as those in Figure
1 have the same functions, and therefore descriptions thereof may be omitted.
[0043] The second air separation apparatus A2 comprises the main heat exchanger 1, the nitrogen
rectification column 2, a first nitrogen condenser 3, a second nitrogen condenser
4, a compressor 91, the expansion turbine 92, the high-purity oxygen rectification
column 5, and the oxygen evaporator 6. Aspects of the configuration that differ from
embodiment 1 will mainly be described.
[0044] The first nitrogen condenser 3 is disposed above the nitrogen rectification column
2, and the second nitrogen condenser 4 is disposed above the first nitrogen condenser
3. Some nitrogen gas (vapour stream) discharged from the top portion 23 of the nitrogen
rectification column 2 is introduced into the first nitrogen condenser 3 via a first
reflux pipeline L231, and is cooled (condensed) through heat exchange with the oxygen-enriched
liquid to form liquefied nitrogen. The liquefied nitrogen is returned to the top portion
23 of the nitrogen rectification column 2 as reflux liquid. Some nitrogen gas (vapour
stream) discharged from the top portion 23 of the nitrogen rectification column 2
is introduced into the second nitrogen condenser 4 via a second reflux pipeline L232,
and is cooled (condensed) through heat exchange with the oxygen-enriched liquid to
form liquefied nitrogen. The liquefied nitrogen is returned to the top portion 23
of the nitrogen rectification column 2 as reflux liquid.
[0045] An oxygen-enriched liquid pipeline L211 is a pipeline through which oxygen-enriched
liquid discharged from the bottom portion 21 of the nitrogen rectification column
2 is passed partially through the main heat exchanger 1 and is then introduced into
the second nitrogen condenser 4. The oxygen-enriched liquid from the second nitrogen
condenser 4 is sent as a refrigerant to the first nitrogen condenser 3.
[0046] The compressor 91 compresses gas discharged from a top portion 41 of the second nitrogen
condenser 4. A recycled gas pipeline L41 is a pipeline through which gas is discharged
from the top portion 41 of the second nitrogen condenser 4, is compressed by the compressor
91, is passed through the main heat exchanger 1, and is then introduced as recycled
gas into the rectification portion 22 of the nitrogen rectification column 2.
[0047] The third air separation apparatus A3 according to the invention will be described
with reference to Figure 3. The same reference numerals as those in Figures 1 and
2 have the same functions, and therefore descriptions thereof may be omitted.
[0048] The third air separation apparatus A3 comprises the main heat exchanger 1, a first
nitrogen rectification column 2, a second nitrogen rectification column 7, the first
nitrogen condenser 3, the second nitrogen condenser 4, the compressor 91, the expansion
turbine 92, the high-purity oxygen rectification column 5, and the oxygen evaporator
6. Aspects of the configuration that differ from Figure 2 will mainly be described.
[0049] Oxygen-enriched gas (vapour) generated in the first nitrogen condenser 3 and oxygen-enriched
liquid discharged from the bottom portion 21 of the first nitrogen rectification column
2 are introduced into the second nitrogen rectification column 7. An oxygen-enriched
liquid pipeline L212 is a pipeline through which oxygen-enriched liquid discharged
from the bottom portion 21 of the first nitrogen rectification column 2 is introduced
into the main heat exchanger 1, is discharged from an intermediate stage thereof,
and is then introduced between intermediate stages 721 and 722 of the rectification
portion of the second nitrogen rectification column 7.
[0050] An oxygen-containing liquid pipeline L723 is a pipeline that introduces oxygen-containing
fluid discharged from between intermediate stages 722, 723 of the rectification portion
of the second nitrogen rectification column 7 into the top portion 53 of the high-purity
oxygen rectification column 5.
[0051] The position at which the oxygen-containing fluid is discharged into the oxygen-containing
fluid pipeline L723 is above the position at which the oxygen-enriched liquid from
the oxygen-enriched liquid pipeline L212 is introduced.
[0052] A heat medium pipeline L711 is a pipeline through which gas (oxygen-enriched gas)
discharged from below the lower-stage rectification portion 721 of the second nitrogen
rectification column 7 is sent as a heat medium to the oxygen evaporator 6, is re-liquefied,
and is sent as a refrigerant phase 41 to the second nitrogen condenser 4 via pipeline
L61.
[0053] A recycled gas pipeline L722 is a pipeline through which gas is discharged from between
the intermediate stages 721 and 722 of the rectification portion of the second nitrogen
rectification column 7, is compressed by the compressor 91, is passed through a portion
of the main heat exchanger 1, and is then introduced as recycled gas into the rectification
portion 22 of the first nitrogen rectification column 2.
[0054] A waste gas extraction pipeline L411 is a pipeline through which gas discharged from
the top portion 41 of the second nitrogen condenser 4 is passed partially through
the main heat exchanger 1, is then sent to the expansion turbine 92 to be expanded
and cooled, is again passed through the main heat exchanger 1, and is extracted as
waste gas, after mixing with top gas from the oxygen rectification column.
[0055] A vapour stream pipeline L731 is a pipeline through which a vapour stream that is
discharged from a top portion 73 of the second nitrogen rectification column 7 and
is sent to the second nitrogen condenser 4 and is returned in liquid form in part
to the top portion 73 of the second nitrogen rectification column 7.
[0056] A pipeline L732 branches off from the liquid stream pipeline L731 downstream of the
second nitrogen condenser 4 and feeds into the top portion 23 of the first nitrogen
rectification column 2. A liquid transfer pump P1 is provided in the pipeline L732.
[0057] The fourth air separation apparatus A4 will be described with reference to Figure
4. The same reference numerals as those in figures 2 and 3 have the same functions,
and therefore descriptions thereof may be omitted.
[0058] The fourth air separation apparatus A4 comprises the main heat exchanger 1, the first
nitrogen rectification column 2, the second nitrogen rectification column 7, the first
nitrogen condenser 3, the second nitrogen condenser 4, the compressor 911, the expansion
turbine 921, the high-purity oxygen rectification column 5, and the oxygen evaporator
6. Aspects of the configuration that differ from figure 3 will mainly be described.
[0059] The compressor 911 compresses a portion of the feed air.
[0060] The expansion turbine 921 expands compressed air that has been compressed by the
compressor 911, introduced into the main heat exchanger 1, and discharged from an
intermediate part thereof.
[0061] A feed air branch pipeline L11 is a pipeline that branches off from the feed air
pipeline L1 upstream of the main heat exchanger 1, sends a portion of the feed air
to the compressor 911 that compresses the feed air, sends the feed air compressed
by the compressor 911 to the main heat exchanger 1 and discharges the same from an
intermediate part thereof to the expansion turbine 921 that expands the feed air,
and then sends the feed air to the rectification portion of the second nitrogen rectification
column 7.
[0062] A low-pressure nitrogen gas extraction pipeline L732 is a pipeline through which
gas discharged from the top portion 73 of the second nitrogen rectification column
7 is extracted as low-pressure nitrogen gas.
[0063] A waste gas extraction pipeline L412 is a pipeline through which gas discharged from
the top portion 41 of the second nitrogen condenser 4 is extracted as waste gas. The
pipeline L53 merges with the waste gas extraction pipeline L412.
[0064] According to the fourth embodiment, coldness required for the heat balance is obtained
by using the expansion turbine 921 to expand either a portion of the feed air or product
nitrogen gas discharged from the first nitrogen rectification column 2 to the pressure
of the second nitrogen rectification column 7. Motive power obtained by the expansion
turbine 921 may be applied to the motive power of the compressor 911 that compresses
the feed air. It should be noted that the same applies to figures 2 and 3.
[0065] The results of a physical simulation of the air separation apparatus of figure 4
are presented. Feed air (1000 Nm
3/h, 9.9 barA) was introduced.
[0066] 930 Nm3/h of the feed air was introduced into the hot end of the main heat exchanger
1, was cooled to -163°C, and was then introduced into the first nitrogen rectification
column 2.
[0067] Another 70 Nm3/h of the feed air was compressed to 13 barA by the compressor 911,
was introduced into the main heat exchanger 1, was cooled to -130°C, was expanded
to 4.4 barA by the expansion turbine 921, and was introduced into the second nitrogen
rectification column 7.
[0068] Nitrogen gas (330 Nm
3/h, 9.7 barA), liquefied nitrogen (48 Nm3/h, 9.7 barA), oxygen-enriched liquid (552
Nm
3/h, oxygen 35.3%) were discharged from the first nitrogen rectification column 2.
[0069] The liquefied nitrogen and oxygen-enriched liquid were introduced into the second
nitrogen rectification column 7.
[0070] Low-pressure nitrogen gas (311 Nm3/h, 4.3 barA), oxygen-containing liquid (73 Nm3/h,
20.0 % O2), oxygen enriched gas (54Nm3/h, 4.3 barA, 36.3% O2), low-pressure oxygen
enriched liquid (232 Nm3/h, 75.5% O2) were discharged from the second nitrogen rectification
column 7.
[0071] The oxygen enriched gas was used as the heat medium in the oxygen evaporator 6, and
was introduced to the second nitrogen condenser 4 as a coolant.
[0072] The low-pressure oxygen enriched liquid was introduced to the second nitrogen condenser
4 as a coolant.
[0073] The oxygen-containing liquid was introduced to the oxygen rectification column. The
oxygen rectification column 5 was operated at 1.5 barA, and high-purity oxygen (10.8
Nm
3/h, 100%) collected in the bottom portion 51.
[0074] A comparison will be made with a case in which feed air was used as the heat medium
in the oxygen evaporator 6, as presented in
WO2014/173496.
[0075] In order to obtain the same nitrogen gas and high-purity oxygen liquid as in the
above example (Figure 2), whereas the amount of feed air required in the present example
was 1000 Nm
3/h, when feed air was used in the oxygen evaporators, 1027 Nm
3/h of feed air was required.
[0076] This is because the heat medium used in the oxygen evaporator 6 in the present example
has a higher oxygen concentration than the feed air, thus allowing condensation to
occur at a lower pressure such as 4.3 barA for the oxygen enriched gas instead of
9.9 barA for the feed air, and as a result reducing the compression energy required
for the heat medium.
[0077] In addition, since it is not necessary to use the feed air as the heat medium, the
amount of feed air that can be supplied to the first nitrogen rectification column
2 can be increased, also making it possible to improve the nitrogen gas recovery.
[0078] Another comparison will be made with a case of oxygen production at 99.8% content
as presented in
US 2023/0038170.
[0079] As an example, if there is 1 ppm methane (or hydrocarbon) in the air, methane is
distributed to the oxygen stream in the comparative example process because there
is no mechanism to separate methane from oxygen, and the methane concentration in
oxygen will be more than 4.8 ppm when 11 Nm3/h of oxygen is produced from 1000 Nm3/h
of feed air.
[0080] In the present invention, the oxygen-containing liquid supplied to the oxygen rectification
column is derived from the methane-free reflux fluid above the location where the
methane-containing fluid is supplied, so that an oxygen product with a methane content
of less than 1 ppm can be produced.
- (1) Although not explicitly stated, pressure regulating and flow rate control devices,
etc. may be installed in each pipeline in order to regulate pressure and flow rate.
- (2) Although not explicitly stated, control valves and gate valves, etc. may be installed
in each line.
- (3) Although not explicitly stated, pressure regulating and temperature measuring
devices, etc. may be installed in each column in order to regulate pressure and temperature.
1. A method for producing high purity oxygen by cryogenic distillation of air, comprising
steps:
• a nitrogen and oxygen separation step of introducing a feed air cooled by a main
heat exchanger (1) to a lower section of a first nitrogen rectification column (2),
and introducing oxygen-enriched liquid removed from the bottom of the first nitrogen
rectification column into a rectification section (721, 722, 723) of a second nitrogen
rectification column (7), separating the feed air into a nitrogen-enriched component
and an oxygen-enriched component in the first nitrogen rectification column and separating
the oxygen enriched liquid into a nitrogen-enriched component and an oxygen-enriched
component the second nitrogen rectification column;
• a first nitrogen condensation step of condensing vapor stream from the first nitrogen
rectification column in a first nitrogen condenser (3) at the top of the first nitrogen
rectification column;
• a second nitrogen condensation step of condensing vapor stream from the second nitrogen
rectification column in a second nitrogen condenser (4) at the top of the second nitrogen
rectification column;
• a high-purity oxygen production step of introducing an oxygen-containing fluid removed
from the rectification section of the second nitrogen rectification column into a
high-purity oxygen rectification column (5) and producing high-purity product oxygen
by using an oxygen evaporator (6); and
• a heating medium utilization step of using gas removed from the bottom of the second
nitrogen rectification as a heat medium for the oxygen evaporator which evaporates
liquefied oxygen and liquefies the gas, and returning the liquefied gas to the second
nitrogen condenser.
2. Method according to Claim 1 comprising a partial feed air introduction step of compressing
part of the feed air by a compressor, cooling the compressed part of the feed air
in a main heat exchanger.
3. Method according to Claim 2 comprising expanding the feed air by a expansion turbine
(921), and introducing the feed air into the second nitrogen rectification column
(7).
4. Method according to Claim 1 or 2 including the step of expanding in a turbine (92)
a vapor formed by vaporising liquid in the second condenser (4).
5. Method according to any preceding claim including the step of pressuring nitrogen
condensed in the second condenser (5) in a pump (P1) and sending the pressurised condensed
nitrogen to the top of the first nitrogen rectification column (2).
6. Method according to any preceding claim wherein the oxygen-containing fluid removed
from the rectification section of the second nitrogen rectification column (7) is
introduced into the high-purity oxygen rectification column (5) as the sole feed for
the high-purity oxygen rectification column.
7. Method according to any preceding claim comprising a waste gas extraction step in
which gas discharged from the top portion (53) of the high-purity oxygen rectification
column is passed through the main heat exchanger (1) and is extracted as waste gas.
8. An air separation apparatus for producing high purity oxygen by cryogenic distillation,
comprising :
• a main heat exchanger (1)
• a first nitrogen rectification column (2)
• a second nitrogen rectification column (7)
• a first nitrogen condenser (3) at the top of the first nitrogen rectification column
• a second nitrogen condenser (4) at the top of the second nitrogen rectification
column
• a high purity oxygen rectification column (5)
• an oxygen evaporator (6) at the bottom of the oxygen rectification column
• a conduit (L212) for introducing feed air cooled by a main heat exchanger to a lower
section of a first nitrogen rectification column in order to separate the feed air
into a nitrogen-enriched component and an oxygen-enriched component in the first nitrogen
rectification column,
• a conduit for introducing oxygen-enriched liquid removed from the bottom of the
first nitrogen rectification column into a rectification section of a second nitrogen
rectification column in order to separate the oxygen enriched liquid into a nitrogen-enriched
component and an oxygen-enriched component in the second nitrogen rectification column;
• conduit (L231) for sending a nitrogen enriched vapor stream from the first nitrogen
rectification column in the first nitrogen condenser;
• a conduit (L731) for sending a nitrogen enriched vapor stream from the second nitrogen
rectification column in the second nitrogen condenser;
• a conduit (L723) for sending an oxygen-containing fluid, preferably a liquid, removed
from the rectification section of the second nitrogen rectification column into the
high-purity oxygen rectification column and producing high-purity product oxygen at
the bottom of the high purity oxygen rectification column and
• a conduit (L711, L61) for sending gas removed from the bottom of the second nitrogen
rectification column as a heat medium for the oxygen evaporator which evaporates liquefied
oxygen, and returning the gas condensed in the oxygen evaporator to the second nitrogen
condenser.
9. Apparatus according to Claim 8 including a turbine (921), a conduit for sending air
to the turbine and a conduit for sending expanded air from the turbine to the second
nitrogen rectification column (7).
10. Apparatus according to Claim 8 including a turbine (92), a conduit (L411) for sending
gas from the second nitrogen condenser (4) to the turbine and a conduit for sending
expanded gas from the turbine to the atmosphere.
11. Apparatus according to Claim 8 or 10 including a compressor (91), a conduit (L722)
for sending gas from between intermediate stages (721, 722) of the second nitrogen
rectification column (7) to the compressor and a conduit for sending compressed gas
from the compressor to the bottom of the first nitrogen rectification column (2).
12. Apparatus according to Claim 11 where an arrival point for the gaseous air in the
first nitrogen rectification column (2) is above an arrival point for the gas compressed
in the compressor.
13. Apparatus according to Claims 10 and 11 wherein the compressor (91) is coupled to
the turbine (92).
14. Apparatus according to one of Claims 8 to 13 including means (L732, P1) for sending
condensed nitrogen from the second condenser (4) to the top of the first nitrogen
rectification column (2).
15. Apparatus according to one of Claims 8 to 14 including means for sending a top gas
(L53) from the oxygen rectification column (5) to the main heat exchanger (1).