[0001] This invention relates to a method for producing gaseous oxygen and to a cryogenic
plant in which said method can be carried out.
[0002] In our UK Patent Application No. 7936637 filed 23 October 1979, we have described
a method of producing gaseous oxygen which method comprises the steps of fractionating
dry compressed air in a double distillation column having a high pressure column operating
at between 5 and 9 bars absolute and a low pressure column operating at between 1.3
and 3 bars absolute, wherein liquid oxygen is withdrawn from the bottom of the low
pressure column, is pressurized and is evaporated against a stream of substantially
pure nitrogen which has been removed from the top of the high pressure column and
compressed to such a pressure that it is at least partially liquified by the evaporation
of the oxygen, and wherein at least part of the liquified nitrogen is expanded and
returned to the high pressure column as reflux.
[0003] The preferred embodiment described in the said UK Patent Application is specifically
designed for producing gaseous oxygen at 2.8 bars absolute although it is indicated
that the general method is applicable for much higher pressures.
[0004] We have found that if the gaseous oxygen is required at pressures in excess of 35
bars, the amount of power consumed by the preferred embodiment described in the said
UK Patent Application increases rapidly over a conventional air separation unit provided
with a gaseous oxygen compressor and in such cases the value of the additional power
outweighs the saving in capital cost.
[0005] In order to reduce the amount of power consumed by our cryogenic plant we have found
it advantageous to compress the nitrogen rich gas from the high pressure column and
divide it into a first sub-stream and a second sub-stream. The first sub-stream is
cooled against the vaporising liquid oxygen and is then expanded to produce a mainly
(on a molar basis) liquid product at least part of which is returned to the high pressure
column as reflux. The second sub-stream is cooled, expanded in an expander, and at
least part of the product leaving the expander is used to assist cooling the first
sub-stream and is then recycled to the compressor. The nitrogen rich gas is preferably
taken from the top of the high pressure column where it is substantially pure. This
enables a substantially pure stream of nitrogen to be drawn off the plant at an elevated
pressure if desired.
[0006] Whilst this method will work at all pressures it is particularly advantageous at
pressures of 35 bars A and above.
[0007] The first sub-stream and the second sub-stream may be compressed to the same pressure
although normally the first sub-stream will be compressed to a pressure 7 to 40 bars
above the second sub-stream.
[0008] We have found it particularly desirable to arrange for fluid leaving the expander
to contain up to 15 mole percent liquid and preferably between 8 and 10 mole percent
liquid. In such a case the liquid is preferably separated from the gas and the liquid
returned to the high pressure column as additional reflux.
[0009] Typically, the pressure of the first sub-stream will be between 40 and 80 bars absolute
whilst the pressure of the second sub-stream will be between 30 and 50 bars absolute.
[0010] The present invention also provides a cryogenic plant for producing gaseous oxygen,
which plant comprises a high pressure column and a low pressure column for distilling
air, a heat exchanger in which liquid oxygen can evaporate, a pump for, in use, receiving
liquid oxygen from the bottom of said low pressure column and introducing it into
said heat exchanger, a compressor, a conduit for carrying nitrogen rich gas from said
high pressure column to said compressor, a conduit for conveying a first sub-stream
of compressed nitrogen rich gas from said compressor through said heat exchanger in
countercurrent flow to said liquid oxygen, an expansion valve for, in use, expanding
cold nitrogen rich gas leaving said heat exchanger and a conduit for conveying liquified
nitrogen rich gas from said expansion valve to said high pressure column, characterized
in that a further conduit is provided for conveying a second sub-stream of compressed
nitrogen rich gas from said compressor to said heat exchanger to cool said compressed
nitrogen rich gas, an expander for allowing compressed nitrogen rich gas from said
heat exchanger to'expand, a conduit for conveying nitrogen rich gas from said expander
to said heat exchanger to assist in cooling said first sub-stream of compressed nitrogen
rich gas and a conduit for carrying said nitrogen rich gas from said heat exchanger
to said compressor.
[0011] There is also provided a cryogenic plant for producing gaseous oxygen, which plant
comprises a high pressure column and a low pressure column for distilling air, a heat
exchanger in which liquid oxygen can evaporate, a pump for, in use, receiving liquid
oxygen from the bottom of said low pressure column and introducing it into said heat
exchanger, a compressor, a conduit for carrying substantially pure gaseous nitrogen
from the top of said high pressure column to said compressor, a conduit for conveying
a first sub-stream of substantially pure compressed nitrogen from said compressor
through said heat exchanger in countercurrent flow to said liquid oxygen, an expansion
valve for, in use, expanding substantially pure cold nitrogen leaving said heat exchanger
and a conduit for conveying substantially pure liquid nitrogen from said expansion
valve to said high pressure column, characterized in that a further conduit is provided
for conveying a second sub-stream of substantially pure compressed nitrogen from said
compressor to said heat exchanger to cool said compressed nitrogen, an expander for
allowing substantially pure compressed nitrogen from said heat exchanger to expand,
a conduit for conveying substantially pure gaseous nitrogen from said expander to
said heat exchanger to assist in cooling said first sub-stream of substantually pure
compressed nitrogen and a conduit for carrying said substantially pure gaseous nitrogen
from said heat exchanger to said compressor.
[0012] The present invention further provides a cryogenic plant for producing gaseous oxygen
which plant comprises a high pressure column and a low pressure column for distilling
air, a first heat exchanger in which liquid oxygen can evaporate, a pump for, in use,
receiving liquid oxygen from the bottom of said low pressure column and introducing
it into said first heat exchanger, a compressor, a conduit for carrying nitrogen rich
gas from said high pressure column to said compressor, a conduit for conveying a first
sub-stream of compressed nitrogen rich gas from said compressor through said first
heat exchanger in countercurrent flow to said liquid oxygen, an expansion valve for,
in use, expanding cold nitrogen rich gas leaving said heat exchanger and a conduit
for conveying liquified nitrogen rich gas from said expansion valve to said high pressure
column, characterized in that a further conduit is provided for conveying a second
sub-stream of compressed nitrogen rich gas from said compressor to a second heat exchanger
to cool said compressed nitrogen rich gas, an expander for allowing compressed nitrogen
rich gas from said second heat exchanger to expand, a conduit for conveying nitrogen
rich gas from said expander to said first heat exchanger to assist in cooling said
first sub-stream of compressed nitrogen rich gas, and a conduit for carrying said
nitrogen rich gas from said first heat exchanger to said compressor.
[0013] There is also provided a cryogenic plant for producing gaseous oxygen which plant
comprises a high pressure column and a low pressure column for distilling air, a first
heat exchanger in which liquid oxygen can evaporate, a pump for, in use, receiving
liquid oxygen from the bottom of said low pressure column and introducing it into
said first heat exchanger, a compressor, a conduit for carrying substantially pure
gaseous nitrogen from the top of said high pressure column to said compressor, a conduit
for conveying a first sub-stream of substantially pure compressed nitrogen from said
compressor through said first heat exchanger in countercurrent flow to said liquid
oxygen, an expansion valve for, in use, expanding substantially pure cold nitrogen
leaving said heat exchanger and a conduit for conveying substantially pure liquid
nitrogen from said expansion valve to said high pressure column, characterized in
that further conduit is provided for conveying a second sub-stream of substantially
pure compressed nitrogen from said compressor to a second heat exchanger to cool said
substantially pure compressed nitrogen, an expander for allowing substantially pure
compressed nitrogen from said second heat exchanger to expand, a conduit for conveying
substantially pure gaseous nitrogen from said expander to said first heat exchanger
to assist in cooling said first sub-stream of substantially pure compressed nitrogen,
and a conduit for carrying said substantially pure gaseous nitrogen from said first
heat exchanger to said compressor.
[0014] Preferably, the first heat exchanger is a wound coil heat exchanger and the second
heat exchanger is a plate-fin heat exchanger.
[0015] For a better understanding of the invention reference will now be made, by way of
example, to the accompanying drawings, in which:
Figure 1 is a simplified flowsheet of one embodiment of a cryogenic plant in accordance
with the invention; and
Figure 2 is a second embodiment of such a cryogenic plant.
[0016] Referring to Figure 1, air at a flowrate of 5934 Kg moles/hour is compressed to 6.5
bars absolute (bars A) in compressor 1 and is subsequently passed through molecular
sieve adsorbers 2 where water, carbon dioxide and any heavy hydrocarbons present are
adsorbed. The air leaves the molecular sieve adsorbers 2 through conduit 3 at 6.1
bars A and 10°C. It is then cooled to -172 C in heat exchanger 4 which it leaves through
conduit 5 at a condition close to saturation. The stream in conduit 5 is then introduced
into the high pressure column 6 of a double column 7.
[0017] A crude liquid oxygen stream is withdrawn from the bottom of the high pressure column
6 through conduit 8 and after being subcooled to -177°C in subcooler 9 is expanded
to 1.5 bars A at valve 10 and introduced into low pressure column 11 which is provided
with a reboiler 12. Liquid oxygen at 98 molar % purity accumulates in the bottom of
the low pressure column 11 and passes to the inlet of pump 13 through conduit 14.
The liquid is then pumped at a rate of 1162 Kg moles/hour to heat exchanger 15 where
it vaporizes and leaves through conduit 16 at 69 bars A and 20°C to form the gaseous
oxygen product stream.
[0018] Gaseous nitrogen is withdrawn from the top of the high pressure column 6 through
conduit 17. A portion of this nitrogen is condensed in reboiler 12 and returned to
the high pressure column 6 through conduit 18 and the remainder through conduit 19
and sub-cooler 9 to product at the rate of 17 kg. moles/hour. The remaining nitrogen
in conduit 17 passes through conduit 20. It is joined at junction 21 by nitrogen from
conduit 22 and the combined stream is passed through conduit 23 to heat exchanger
4. After being warmed to -125
oC, a portion of the nitrogen is withdrawn through conduit 24 and the balance leaves
the heat exchanger 4 through conduit 25 at 6°C. It is joined by nitrogen from conduit
26 at junction 27 and the combined stream is introduced into the first stage 28 of
a compressor 29. The nitrogen is compressed to 41 bars A and leaves the first stage
28 through conduit 30. A second sub-stream 31 is then withdrawn and the balance is
compressed to 61 bars A in second stage 32 and product nitrogen at a flowrate of 1367
Kg moles/hour is withdrawn through conduit 33. The remaining nitrogen is compressed
to 80 bars A in the third stage 34 of compressor 29 which is leaves through conduit
35 as a first sub-stream.
[0019] The first sub-stream is cooled to -169°C in heat exchanger 15 which it leaves as
a sub-cooled vapour as it is above its critical pressure. It is then expanded to 5.9
bars A at valve 36 and the two phases thus formed are separated in phase separator
37.
[0020] Liquid nitrogen is withdrawn from the bottom of the phase separator 37 and is returned
to the high pressure column 6 through conduit 39 as reflux.
[0021] Turning now to the second sub-stream 31, the nitrogen at 41 bars A is cooled to -123°C
in heat exchanger 15 and is then expanded through generator loaded expander 40 to
5.9 bars A. The two phase nitrogen leaving the expander 40 through conduit 41 contains
8 mole percent liquid and is introduced into phase separator 37. The gaseous nitrogen
in the phase separator 37 passes to junction 42. Gaseous nitrogen is passed through
conduit 22 to junction 21 whilst the balance is introduced into the cold end of heat
exchanger 15 through conduit 43. After being warmed to -125°C the nitrogen is joined
by nitrogen from conduit 24 at junction 44. The combined stream is then warmed and
enters conduit 26.
[0022] Of the remaining features a nitrogen-rich liquid fraction is taken from the high
pressure column 6 through conduit 44 to sub-cooler 9 which it leaves through conduit
45. It is then expanded at valve 46 and the resulting two phase mixture is introduced
into the low pressure column 11. Waste nitrogen leaves the top of the low pressure
column 11 through conduit 47 and after being warmed in sub-cooler 9, enters heat exchanger
4 via conduit 47. The waste nitrogen leaves heat exchanger 4 through conduit 48 and
a portion is used for regenerating the molecular sieves 2. The remainder is vented
to atmosphere through conduit 49.
[0023] Various modifications to the cryogenic plant described are currently envisaged, for
example, whereas heat exchangers 4 and 15 will normally be plate-fin heat exchangers
where pressure permit, it may be necessary for heat exchanger 15 to be a wound coil
heat exchanger (generally where the pressure of the oxygen stream exceeds 81 bars
A). However, since wound coil heat exchangers are relatively expensive, it may be
desirable to use a plate-fin heat exchanger in combination with a wound coil heat
exchanger in place of a single wound coil heat exchanger 15.
[0024] In this connection reference is made to Figure 2 which shows a cryogenic plant which
is generally similar to that shown in Figure 1 except that the liquid oxygen is pumped
to 98 bars A by pump 13. In this particular embodiment the second and third stages
of the compressor have been combined into a single second stage 51 which compresses
the nitrogen to 74 bars A. For this embodiment the heat exchanger 15 is of the wound
coil type. Because of the cost and complexity of building a wound coil heat exchanger
with the flows arranged as shown in Figure 1, the second sub-stream 31 is cooled in
a separate plate-fin heat exchanger 52 before being expanded as before. Cooling of
the second sub-stream is effected by a stream 53 taken from conduit 24, passed through
plate-fin heat exchanger 52 and returned to conduit 26 as shown.
[0025] If desired, in either of the cryogenic plants described, heat exchanger 4 may be
replaced with a reversing heat exchanger the and molecular sieve adsorbers omitted.
In such an embodiment it will be necessary to place a hydrocarbon absorber in conduit
8 downstream of subcooler 9.
[0026] If desired the second stage 32 and/or third stages 34 of the compressor 29 could
be separate and distinct from the first stage 28 and driven, for example completely,
or in part, by expander 40.
1. A method for producing gaseous oxygen which method comprises the steps of fractionating
dry compressed air in a double distillation column having a high pressure column operating
at between 5 and 9 bars absolute and a low pressure column operating at between 1.3
and 3 bars absolute, wherein liquid oxygen is withdrawn from the bottom of the low
pressure column, is pressurized and is evaporated against a stream of nitrogen rich
gas which has been removed from the high pressure column and compressed in a compressor
characterized in that the compressed nitrogen rich gas is divided into a first sub-stream
and a second sub-stream; the first sub-stream is cooled against the vaporising liquid
oxygen and is then expanded to produce a mainly (on a molar basis) liquid product
at least part of which is returned to the high pressure column as reflux; and the
second sub-stream is cooled, expanded in an expander, and at least part of the product
leaving the expander is used to assist cooling the first sub-stream and is then recycled
to said compressor.
2. A method for producing gaseous oxygen which method comprises the steps of fractionating
dry compressed air in a double distillation column having a high pressure column operating
at between 5 and 9 bars absolute and a low pressure column operating at between 1.3
and 3 bars absolute, wherein liquid oxygen is withdrawn from the bottom of the low
pressure column, is pressurized and is evaporated against a stream of substantially
pure nitrogen which has been removed from the top of the high pressure column and
compressed in a compressor characterized in that the compressed nitrogen is divided
into a first sub-stream and a second sub-stream; the first sub-stream is cooled against
the vaporising liquid oxygen and is then expanded to produce a mainly (on a molar
basis) liquid product at least part of which is returned to the high pressure column
as reflux; and the second sub-stream is cooled, expanded in an expander, and at least
part of the product leaving the expander is used to assist cooling the first sub-stream.and
is then recycled to said compressor.
3. A method according to Claim 1 or 2, characterized in that the first sub-stream
is compressed to a higher pressure than the second sub-stream.
4. A method according to Claim 1 or 2, characterized in that said second sub-stream
leaving said expander contains up to 15 mole percent liquid.
5. A method according to Claim 1, 2, 3 or 4, characterized in that the pressure of
said first sub-stream is in excess of 40 bars absolute.
6. A method according to Claim 1, 2, 3, 4, or 5, characterized in that the pressure
of said second sub-stream is in excess of 30 bars absolute.
7. A cryogenic plant for producing gaseous oxygen, which plant comprises a high pressure
column and a low pressure column for distilling air, a heat exchanger in which liquid
oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the bottom
of said low pressure column and introducing it into said heat exchanger, compressor,
a conduit for carrying nitrogen rich gas from said .high pressure column to said compressor,
a conduit for conveying a first sub-stream of compressed nitrogen rich gas from said
compressor through said heat exchanger in countercurrent flow to said liquid oxygen,
an expansion .valve for, in use, expanding cold nitrogen rich gas leaving said heat
exchanger and a conduit for conveying liquified nitrogen rich gas from said expansion
valve to said high pressure column, characterized in that a further conduit is provided
for conveying a second sub-stream of compressed nitrogen rich gas from said compressor
to said heat exchanger to cool said compressed nitrogen rich gas, an expander for
allowing compressed nitrogen rich gas from said heat exchanger to expand, a conduit
for conveying nitrogen rich gas from said expander to said heat exchanger to assist
in cooling said first sub-stream of compressed nitrogen rich gas and a conduit for
carrying said nitrogen rich gas from said heat exchanger to said compressor.
8. A cryogenic plant for producing gaseous oxygen, which plant comprises a high pressure
column and a low pressure column for distilling air, a heat exchanger in which liquid
oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the bottom
of said low pressure column and introducing it into said heat exchanger, a compressor,
a conduit for carrying substantially pure gaseous nitrogen from the top of said high
pressure column to said compressor, a conduit for conveying a first sub-stream of
substantially pure compressed nitrogen from said compressor through said heat exchanger
in countercurrent flow to said liquid oxygen, an expansion valve for, in use, expanding
substantially pure cold nitrogen leaving said heat exchanger and a conduit for conveying
substantially pure liquid nitrogen from said expansion valve to said high pressure
column, characterized in that a further conduit is provided for conveying ssecond
sub-stream of substantially pure compressed nitrogen from said compressor to said
heat exchanger to cool said compressed nitrogen, an expander for allowing substantially
pure compressed nitrogen from said heat exchanger to expand, a conduit for conveying
substantially pure gaseous nitrogen from said expander to said heat exchanger to assist
in cooling said first sub-stream of substantually pure compressed nitrogen and a conduit
for carrying said substantially pure gaseous nitrogen from said heat exchanger to
said compressor.
9. A cryogenic plant for producing gaseous oxygen which plant comprises a high pressure
column and a low pressure column for distilling air, a first heat exchanger in which
liquid oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the
bottom of said low pressure column and introducing it into said first heat exchanger,
a compressor, a conduit for carrying nitrogen rich gas from said high pressure column
to said compressor, a conduit f.or conveying a first sub-stream of compressed nitrogen
rich gas from said compressor through said first heat exchanger in countercurrent
flow to said liquid oxygen, an expansion valve for, in use, expanding cold nitrogen
rich gas leaving said heat exchanger and a conduit for conveying liquified nitrogen
rich gas from said expansion valve to said high pressure column, characterized in
that a further conduit is provided for conveying a second sub-stream of compressed
nitrogen rich gas from said compressor to a second heat exchanger to cool said compressed
nitrogen rich gas, an expander -for allowing compressed nitrogen rich gas from said
second heat exchanger to expand, a conduit for conveying nitrogen rich.gas from said
expander to said first heat exchanger to assist in cooling said first sub-stream of
compressed nitrogen rich gas, and a conduit for carrying said nitrogen rich gas from
said first heat exchanger to said compressor.
10. A cryogenic plant for producing gaseous oxygen which plant comprises a high pressure
column and a low pressure column for distilling air, a first heat exchanger in which
liquid oxygen can evaporate, a pump for, in use, receiving liquid oxygen from the
bottom of said low pressure column and introducing it into said first heat exchanger,
a compressor, a conduit for carrying substantially pure gaseous nitrogen from the
top of said high pressure column to said compressor, a conduit for conveying a first
sub-stream of substantially pure compressed nitrogen from said compressor through
said first heat exchanger in countercurrent flow to said liquid oxygen, an expansion
valve for, in use, expanding substantially pure cold nitrogen leaving said heat exchanger
and a conduit for conveying substantially pure liquid nitrogen from said expansion
valve to said high pressure column, characterized in that further conduit is provided
for conveying a second sub-stream of substantially pure compressed nitrogen from said
compressor to a second heat exchanger to cool said substantially pure compressed nitrogen,
an expander for allowing substantially pure compressed nitrogen from said second heat
exchanger to expand, a conduit for conveying substantially pure gaseous nitrogen from
said expander to said first heat exchanger to assist in cooling said first sub-stream
of substantially pure compressed nitrogen, and a conduit for carrying said substantially
pure gaseous nitrogen from said first heat exchanger to said compressor.
ll. A cryogenic plant according to Claim 9 or 10, characterized in that said first
heat exchanger is a wound coil heat exchanger and said second heat exchanger is a
plate-fin heat exchanger.