U.S. patent application number 09/819951 was filed with the patent office on 2001-12-20 for process and apparatus for producing a pressurized product by low-temperature fractionation of air.
This patent application is currently assigned to LINDE AKTIENGESELLSCHAFT. Invention is credited to Kunz, Christian, Rottmann, Dietrich.
Application Number | 20010052244 09/819951 |
Document ID | / |
Family ID | 7636828 |
Filed Date | 2001-12-20 |
United States Patent
Application |
20010052244 |
Kind Code |
A1 |
Rottmann, Dietrich ; et
al. |
December 20, 2001 |
Process and apparatus for producing a pressurized product by
low-temperature fractionation of air
Abstract
For producing a pressurized product by low-temperature producing
a pressurized product by low-temperature fractionation of air in a
rectification system which has a high-pressure column (13) and a
low-pressure column (14), a first feed airstream (12) is introduced
into the high-pressure column (13), and an oxygen-rich fraction
(38) from the low-pressure column (14) is brought (39) to pressure
in the liquid state and introduced (41) into a mixing column (16).
A second feed airstream (6, 15) is introduced into the lower region
of the mixing column (16) and brought into countercurrent contact
with the oxygen-rich fraction (41). The mixing column (16) is
operated at a pressure (P.sub.M1S) which is lower than the
operating pressure (p.sub.HDS) of the high-pressure column (13). A
total airstream (1) which comprises the first and second feed
airstreams is compressed (2) to a first pressure (p.sub.1) which is
lower than the operating pressure (p.sub.HDS) of the high-pressure
column (13) and is purified (3) at about this first pressure
(p.sub.2) . The purified total airstream (4) is divided into the
first (5) and the second (6) feed airstream. The first feed
airstream (5) is further compressed (8) separately from the second
feed airstream to a second pressure (P.sub.2) which is at least
equal to the operating pressure (P.sub.HDS) of the high-pressure
column (13).
Inventors: |
Rottmann, Dietrich;
(Muenchen, DE) ; Kunz, Christian; (Muenchen,
DE) |
Correspondence
Address: |
MILLEN, WHITE, ZELANO & BRANIGAN, P.C.
2200 CLARENDON BLVD.
SUITE 1400
ARLINGTON
VA
22201
US
|
Assignee: |
LINDE AKTIENGESELLSCHAFT
Zentrale Patentabteilung
Hollriegelskreuth
DE
82049
|
Family ID: |
7636828 |
Appl. No.: |
09/819951 |
Filed: |
March 29, 2001 |
Current U.S.
Class: |
62/646 |
Current CPC
Class: |
F25J 3/04145 20130101;
F25J 2245/40 20130101; F25J 3/04018 20130101; F25J 2200/06
20130101; F25J 3/04193 20130101; F25J 2235/50 20130101; F25J
3/04303 20130101; F25J 3/04024 20130101; F25J 3/04466 20130101;
F25J 3/0429 20130101; F25J 3/04187 20130101 |
Class at
Publication: |
62/646 |
International
Class: |
F25J 003/00 |
Foreign Application Data
Date |
Code |
Application Number |
Mar 29, 2000 |
DE |
10015602.9 |
Claims
1. A process for producing a pressurized product by low-temperature
fractionation of air in a rectification system which has a
high-pressure column (13) and a low-pressure column (14), in which
a first feed airstream (12) is introduced into the high-pressure
column (13), an oxygen-rich fraction (38) from the low-pressure
column (14) is brought (39) to pressure in the liquid state and
introduced (41) into a mixing column (16), a second feed airstream
(6, 15, 306, 406) is introduced into the lower region of the mixing
column (16) and brought into countercurrent contact with the
oxygen-rich fraction (41), with the mixing column (16) being
operated at a pressure (p.sub.MIS) which is lower than the
operating pressure (p.sub.HDS) of the high-pressure column (13),
and in which a gaseous top product (51) is taken off from the upper
region of the mixing column (16) and produced as pressurized
product (52), characterized in that a total airstream (1) which
comprises the first and second feed airstreams is compressed (2) to
a first pressure (p.sub.1) which is lower than the operating
pressure (p.sub.HDS) of the high-pressure column (13), the total
airstream (4) is divided into the first (5) and the second (6, 306,
406) feed airstreams and in that the first feed airstream (5) is
further compressed (8, 108) separately from the second feed
airstream to a second pressure (p.sub.2) which is at least equal to
the operating pressure (p.sub.HDS) of the high-pressure column
(13).
2. Process according to claim 1, characterized in that the first
pressure (p.sub.1) is about equal to the operating pressure
(p.sub.M1S) of the mixing column (16).
3. Process according to claim 1, characterized in that the first
pressure is lower than the operating pressure (p.sub.M1S) of the
mixing column (16) and in that the second feed airstream (306, 406)
is further compressed (317, 417) separately from the first feed
airstream to a third pressure (p.sub.3) which is at least equal to
the operating pressure (p.sub.M1S) of the mixing column (16).
4. Process according to one of claims 1 to 3, characterized in that
the oxygen-rich fraction brought to pressure in the liquid state,
before the introduction (41) into the mixing column (16), is warmed
in indirect heat exchange (40) with a superheated airstream
(42).
5. Process according to one of claims 1 to 4, characterized in that
a third feed airstream (7, 50, 207, 407, 450) is work-expanded (20,
420) and introduced (21) into the low-pressure column (14).
6. Process according to one of claims l to 5, characterized in that
the third feed airstream (7), before the work expansion (20) , is
recompressed (17) with, in particular, mechanical energy produced
during the work expansion (20) being used for the recompression
(17).
7. Process according to one of claims 1 to 6, characterized in that
the third feed airstream is formed downstream of the purification
(3) by a portion of the total airstream (4) and is fed (7, 207)
directly, or after joint recompression (108) with the first feed
airstream, to the recompression (17).
8. Process according to one of claims 1 to 4, characterized in that
the second feed airsteam (306, 349, 350) is work-expanded (320)
before its introduction into the mixing column.
9. Apparatus for producing a pressurized product by low-temperature
fractionation of air by a rectification system which has a
high-pressure column (13) and a low-pressure column (14) and having
a first feed air line (5, 11, 12) which leads into the
high-pressure column (13), a liquid line (38, 41) for taking off an
oxygen-rich fraction from the low-pressure column (14), which
comprises means (39) for pressure elevation and leads to a mixing
column (16), a second feed air line (6, 15) which leads to the
lower region of the mixing column (16), and having an oxygen
product line which is connected to the upper region of the mixing
column (16), characterized by a total air line which leads via an
air compressor (2) and a purification device (3) and is connected
downstream to the first and second feed air lines and by a
recompressor (8, 108) which is disposed in the first feed air line
(5, 11, 12).
Description
[0001] The invention relates to a process for producing a
pressurized product by low-temperature fractionation of air with
production of a gaseous pressurized product from a mixing column.
In the invention, the mixing column is operated at a pressure which
is lower than the operating pressure of the high-pressure column of
the two-column system which serves for nitrogen-oxygen separation.
separation.
[0002] The rectification system of the invention can be constructed
as a two-column system, for example as a classic double-column
system, or else as a three-column or multiple column system. It
can, additionally to the columns for nitrogen-oxygen separation,
have other apparatuses for producing other air components, in
particular noble gases (for example krypton, xenon and/or
argon).
[0003] The oxygen-rich fraction which is used as feed for the
mixing column has an oxygen concentration which is higher than that
of air and is, for example, 70 to 99.5 mol%, preferably 90 to 98
mol%. Mixing column is taken to mean a countercurrent contact
column in which a more volatile gaseous fraction is charged in
countercurrent to a less-volatile liquid.
[0004] The inventive process is suitable, in particular, for
producing gaseous impure oxygen under pressure. Impure oxygen is
here termed a mixture having an oxygen content of 99.5 mol% or
less, in particular 70 to 99.5 mol%. The product pressures are, for
example, 2.2 to 4.9 bar, preferably 2.5 to 4.5 bar. Obviously, the
pressurized product, as required, can be further compressed in the
gaseous state.
[0005] A process and an apparatus of the type mentioned at the
outset are disclosed by EP 697576 Al Here, the total air is
compressed to about high-pressure column pressure and the mixing
column air is then expanded to the operating pressure of the mixing
column, with a part of the mixing column air being work-expanded.
By this means, although the high pressure of this partial airstream
can be used to produce cold, the known process is not energetically
favourable in all cases.
[0006] The object underlying the invention is to specify a process
of the type mentioned at the outset and a corresponding apparatus
which have a particularly low energy consumption.
[0007] This object is achieved by means of the fact that a total
airstream which comprises at least the first and second feed
airstreams is compressed to a first pressure (p.sub.1) which is
lower than the operating pressure (p.sub.HDS) of the high-pressure
column and is advantageously purified at about this first pressure
(p.sub.1) that the purified total airstream is divided into the
first and second feed airstreams and that the first feed airstream
is further compressed separately from the second feed airstream to
a second pressure (p.sub.2) which is at least equal to the
operating pressure (p.sub.HDS) of the high-pressure column.
[0008] The total airstream is therefore not compressed to the
highest pressure in the system, but to a lower value. The air
fraction or air fractions which require a relatively high pressure,
in particular the high-pressure-column air, are specifically
separately further compressed. As a result, the process can proceed
with the lowest possible energy consumption in compression of the
feed air.
[0009] The lowest equipment costs are achieved if the first
pressure is about equal to the operating pressure of the mixing
column. In this case the mixing column air (second feed airstream)
can be introduced into the mixing column without further
pressure-changing measures.
[0010] Alternatively thereto, the first pressure can be lower than
the operating pressure (p.sub.M1S) of the mixing column. In this
case, the second feed airstream is further compressed separately
from the first feed airstream to a third pressure (p.sub.3) which
is at least equal to the operating pressure (p.sub.M1S) of the
mixing column.
[0011] Preferably, the oxygen-rich fraction brought to pressure in
the liquid state, before being introduced into the mixing column,
is warmed in indirect heat exchange with a superheated airstream.
The superheated airstream is formed, for example, by a portion of
the feed air which is at high-pressure-column pressure. This is
taken off at an intermediate temperature from the main heat
exchanger in which feed air is cooled to about dewpoint, and
brought to the indirect heat exchange with the oxygen-rich liquid
without further temperature-changing measures. In this manner, the
temperature of the liquid which is applied to the mixing column is
optimally matched to the conditions in the countercurrent flow mass
transfer within the mixing column.
[0012] Cold is produced in a favourable manner in the process by a
third feed airstream being work-expanded and introduced into the
low-pressure column. By this means the "natural" pressure drop
between the first pressure or another process pressure can be
utilized to compensate for insulation losses and, if appropriate,
to liquefy a portion of the products.
[0013] Preferably, the third feed airstream, before the work
expansion, is recompressed, in which case, in particular,
mechanical energy produced during the work expansion is used to
drive the recompression. In this case a turbine-booster combination
can be used in which the expansion turbine and recompressor are
mechanically coupled via a shared shaft.
[0014] The third feed airstream can be compressed to the first
pressure and purified together with the first and second feed
airstreams. Then it is either immediately fed to the recompression
or recompressed still together with the first feed airstream.
[0015] Alternatively to injecting the third feed airstream into the
low-pressure column, the second feed airstream, after its further
compression, and before being fed into the mixing column, car be
work-expanded. The further compression is then carried out to a
second pressure which is markedly higher than the mixing column
pressure.
[0016] The invention also relates to an apparatus for conducting
the process.
[0017] The invention and further details of the invention are
described in more detail below with reference to exemplary
embodiments shown in the drawings. In this case:
[0018] FIG. 1 shows a process and an apparatus having work
expansion of a portion of the air compressed to the first
pressure,
[0019] FIG. 2 shows a modified process having work expansion of a
portion of :he air compressed to the second pressure,
[0020] FIG. 3 shows a process having work expansion of the
mixed-column air and
[0021] FIG. 4 shows another variant of FIG. 1 without recompression
of the turbine air.
[0022] In the case of the process shown in FIG. 1, feed air 1 is
brought in a two-stage air compressor 2 with after-cooling to a
first pressure p.sub.1 of, for example, 2.7 to 3.7 bar, preferably
about 3.2 bar and, at preferably this pressure, enters into a
purification device 3, which is preferably formed by a pair of
conventional molecular-sieve adsorbers. The purified total air 4
divided into three partial streams 5, 6, 7.
[0023] The first feed airstream 5 is further compressed in a first
recompressor 8 to a second pressure p.sub.2 of, for example, 4.4 to
7.0 bar, preferably about 5.7 bar, and, after after-cooling 9 flows
into a main heat exchanger 10. The first feed airstream leaves the
main heat exchanger 10 via line 11 at about dewpoint temperature
and is fed via line 12 into a high-pressure column 13. The
operating pressure P,.DS of the high-pressure column 13 is, for
example, 4.3 to 6.9 bar, preferably about 5.6 bar. The
rectification system in addition has a low-pressure column 14 which
is operated at, for example, 1.3 to 1.7 bar, preferably about 1.5
bar.
[0024] The second feed airstream C is also passed through the main
heat exchanger 10 at about the first pressure p.sub.1 (minus pipe
losses and pressure drops in the cleaning device) and finally flows
via line 15 to the mixing column. The feed point is directly above
the bottom of the mixing column 16.
[0025] The third partial stream 7 is recompressed from about the
first pressure P, to a third pressure p, of, for example, 3.8 to
5.6 bar, preferably about 4.7 bar, in a second recompressor 17 and,
after after-cooling 18 is fed via line 19 to the warm end of the
main heat exchanger. However, it is only cooled to an intermediate
temperature and is taken off again from the main heat exchanger 10
before the cold end via line 50 and work-expanded in a turbine 20.
The expanded air 21 is injected into the low-pressure column 14.
Recompressor 17 and turbine 20 are directly mechanically
coupled.
[0026] The rectification system is designed in the exemplary
embodiments as a classic Linde double-column apparatus having a
condenser-evaporator 22 as main condenser. However, the invention
can also be used in rectification systems having other condenser
and/or column configurations.
[0027] Oxygen-enriched liquid 23 from the bottom of the
high-pressure column 13 is cooled in a first sub-cooling
countercurrent heat exchanger 24 and fed, after throttling 25, to
the low-pressure column 14, at an intermediate point 26. Gaseous
nitrogen 27 from the top of the high-pressure column 13 can in part
22 be warmed in the main heat exchanger 10 and produced as
pressurized nitrogen product 29. The remainder 30 Is essentially
completely condensed in the main condenser 22. The liquid nitrogen
31 produced here is at least in part 32 introduced as reflux into
the high-pressure column 13. If required, another portion 33 can be
taken off as liquid product. An intermediate liquid (impure
nitrogen) of the high-pressure column 34 serves, after sub-cooling
24 and throttling 35, as reflux for the low-pressure column.
Gaseous impure nitrogen 36 from the top of the low-pressure column
is warmed in the heat exchangers 24 and 10 and finally taken off
via line 37. It can be used, as shown, as regeneration gas for the
purification device 3.
[0028] Liquid oxygen 38 is taken off from the bottom of the
low-pressure column brought to a pressure of, for example, 5.7 to
6.5 bar, preferably about 6.1 bar, in a pump 39, warmed in a second
sub-cooling countercurrent heat exchanger 40 and finally introduced
(41) into the top of the mixing column 16. In the second
sub-cooling countercurrent heat exchanger 40, in particular, a
superheated airstream 42 is cooled which is branched off from the
first feed airstream upstream of the cold end of the main heat
exchanger, more precisely at an intermediate temperature which is
lower than the inlet temperature of the turbine 20. This airstream,
after its cooling, is recombined via line 43 with the first feed
airstream 11. Via the valve 44, the amount of the airstream flowing
through the second sub-cooling countercurrent heat exchanger is
set.
[0029] From the top of the mixing column 16, gaseous impure
pressurized oxygen 51 is taken off, warmed in the main heat
exchanger 10 and produced as product 52. Bottoms liquid 45 and an
intermediate liquid 46 are taken off from the mixing column and fed
via the lines 47 and 48, respectively, to the low-pressure column
14 at a suitable point.
[0030] FIG. 2 differs from Figure only in that the third feed
airstream 207 is further compressed together with the second feed
airstream in the first recompressor 108. As a result, a higher
inlet pressure is reached at the turbine 20 and correspondingly
more cold is produced.
[0031] In the variant of FIG. 3, the purification device is
operated at a first pressure P, which is higher than the operating
pressure p.sub.M1S of the mixing column. The first pressure
p.sub.1' is here, or example, 2.7 to 3.7 bar, preferably about 3.2
bar. Here the second feed airstream 306 is expanded upstream of its
feed into the mixing column. A third feed airstream which is
injected into the low-pressure column does not exist. The second
feed airstream 306 is further compressed downstream of its
branching off from the purified total air in the second
recompressor 317, which is driven by the turbine 320. The second
feed airstream 349 which is further compressed, for example, to 3.8
to 5.6 bar, preferably about 4.7 bar, is fed via line 350 to the
turbine 320 and is work-expanded there to about
mixed-column-pressure p.sub.M1S
[0032] Similarly to the case in FIG. 3, in the process of FIG. 4,
the purification 3 is operated at a particularly low first pressure
p.sub.1'' of, for example, 2.7 to 3.7 bar, preferably about 3.2
bar. The turbine 420 is, as in FIG. 1, subjected to a third feed
airstream 407, 450 which here, however, is not recompressed, but is
directly work-expanded from about the first pressure p.sub.1to
about low-pressure-column pressure. The recompressor 418 driven by
the turbine is here used for further compression of the second feed
airstream to the second pressure p.sub.2, which is about equal to
the operating pressure p.sub.M1S of the mixing column.
[0033] In all exemplary embodiments, the air compressor and the
recompressor 8, 108 are preferably jointly constructed as a
three-stage machine. In other words, the further compression of the
first feed airstream is carried out in the third stage of a machine
whose first and second stages serve for air compression upstream of
the purification 3. Alternatively thereto, this machine can also be
constructed in four stages, with in tis case the first three stages
being arranged before the purification device 3.
[0034] Referring back to the process, whereas it is advantageous
for the compressed total air stream to be purified at the
compression pressure, it is also possible that purification can be
conducted upstream or downstream for individual feed streams and/or
at different pressures.
[0035] The preceding examples can be repeated with similar success
by substituting the generically or specifically described reactants
and/or operating conditions of this invention for those used in the
preceding examples. Also, the preceding specific embodiments are to
be construed as merely illustrative, and not limitative of the
remainder of the disclosure in any way whatsoever.
[0036] The entire disclosure of all applications, patents and
publications, cited above and below, and of corresponding German
application 10015602.9, are hereby incorporated by reference.
[0037] From the foregoing description, one skilled in the art can
easily ascertain the essential characteristics of this invention,
and without departing from the spirit and scope thereof, can make
various changes and modifications of the invention to adapt it to
various usages and conditions.
* * * * *