U.S. patent application number 09/828354 was filed with the patent office on 2002-01-31 for column for the cryogenic separation of gaseous mixtures and method for the cryogenic separation of a mixture containing hydrogen and co using this column.
This patent application is currently assigned to L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE. Invention is credited to Cam, Francois, Gallarda, Jean.
Application Number | 20020011077 09/828354 |
Document ID | / |
Family ID | 8849006 |
Filed Date | 2002-01-31 |
United States Patent
Application |
20020011077 |
Kind Code |
A1 |
Gallarda, Jean ; et
al. |
January 31, 2002 |
Column for the cryogenic separation of gaseous mixtures and method
for the cryogenic separation of a mixture containing hydrogen and
CO using this column
Abstract
Column for the cryogenic separation of gaseous mixtures
comprising: liquid traps (10, 26, 27) located between two active
zones (5, 14, 28, 29) consisting of a cylindrical container with a
perforated bottom (11) and defining, with the column, an annular
space (9) through which the ascending gases pass; internal linings
(30, 31) of the column, means (15) for causing the ascending gases
to pass into the said internal linings (30, 31) and means (18) for
causing the said gases and the liquid they contain to leave the
said linings (30, 31), returning them to the interior of the column
above the said liquid trap (10, 26, 27); external jackets (21, 32,
33) of the column, comprising means (22, 34, 35) of introducing a
cooling fluid (23) into their lower part and means (24, 36, 37) of
extracting the said fluid from their upper part, the said external
jacket (21, 32, 33) allowing heat transfers between the said fluid
(23) and the matter circulating in the internal lining (30, 31);
and means (38) for introducing a liquefied gas to scrub the gas
extracted at the top of the column.
Inventors: |
Gallarda, Jean; (Joinville
Le Pont, FR) ; Cam, Francois; (Drancy, FR) |
Correspondence
Address: |
YOUNG & THOMPSON
745 SOUTH 23RD STREET 2ND FLOOR
ARLINGTON
VA
22202
|
Assignee: |
L'AIR LIQUIDE, SOCIETE ANONYME POUR
L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE
|
Family ID: |
8849006 |
Appl. No.: |
09/828354 |
Filed: |
April 9, 2001 |
Current U.S.
Class: |
62/617 |
Current CPC
Class: |
F25J 3/0295 20130101;
F25J 3/0261 20130101; B01J 2219/00094 20130101; B01J 19/02
20130101; B01D 3/225 20130101; B01D 3/22 20130101; B01D 3/20
20130101; F25J 3/0252 20130101; F25J 3/0223 20130101; B01J
2219/0236 20130101; B01J 19/006 20130101; C01B 2203/047 20130101;
F25J 2270/02 20130101; B01J 2219/00765 20130101; F25J 2270/24
20130101; B01J 2219/00768 20130101; B01J 19/32 20130101; C01B
2203/046 20130101; C01B 2203/048 20130101; F25J 2205/30 20130101;
C01B 3/506 20130101; F25J 2200/80 20130101; F25J 2200/90 20130101;
F25J 2290/40 20130101 |
Class at
Publication: |
62/617 |
International
Class: |
F25J 003/00 |
Foreign Application Data
Date |
Code |
Application Number |
Apr 7, 2000 |
FR |
00 04486 |
Claims
1. Column for the cryogenic separation of gaseous mixtures,
characterized in that it comprises: a cylindrical wall (1); means
(2) of introducing the gaseous mixture into the said column; at
least one assembly consisting of: two active zones (5, 14, 28, 29)
spaced staggered along the height of the column and filling the
entire cross section thereof; a liquid trap (10, 26, 27) located
between the said active zones (5, 14, 28, 29), consisting of a
cylindrical container with a perforated bottom (11) and the outer
side wall of which defines, with the cylindrical wall (1) of the
column, an annular space (9) in which the gases circulating upwards
inside the column can pass after they have passed through the
active zone (5, 14, 28, 29) above which the said liquid trap (10,
26, 27) is positioned; an internal lining (30, 31) of the
cylindrical wall (1) of the column, having its lower end (13)
located level with the upper edge of a liquid trap (10, 26, 27),
means (15) for causing the gases leaving the active zone (5, 14,
28) located below the said liquid trap (10, 26, 27) to pass into
the said internal lining (30, 31), and means (18) for causing the
said gases and the condensed liquid they contain to leave the said
internal lining (30, 31), returning them to the interior of the
column above the said liquid trap (10, 26, 27); an external jacket
(21, 32, 33) of the cylindrical wall (1) of the column, located
facing the said internal lining, comprising means (22, 34, 35) of
introducing a cooling fluid (23) into its lower part and means (24,
36, 37) of extracting the said fluid at its upper part, the said
external jacket (21, 32, 33) allowing heat transfers between the
said cooling fluid (23) and the gaseous and liquid matter
circulating in the internal lining (30, 31) via the cylindrical
wall (1) of the column; means (38) for introducing a liquefied gas
into the upper part of the column to scrub the gas extracted at the
top of the column; means (39) of extracting the most volatile gas
from the said gaseous mixture at the top of the said column, and
means (6, 7) of extracting, in the liquid state, the least volatile
gas or gases of the said gaseous mixture at the bottom of the said
column.
2. Column according to claim 1, characterized in that the said
internal lining (30, 31) and the said external jacket (21, 32, 33)
have their upper ends located at or above the upper end of the
active zone (14, 28, 29) hanging over the said liquid trap (10, 26,
27).
3. Column according to claim 1 or 2, characterized in that the said
internal linings (30, 31) comprise, distributed alternately about
the internal circumference of the column, first portions which open
at their lower part through orifices (15) into the said annular
space (9) and through which the gases circulating upwards inside
the column can pass, and second portions opening, in their lower
part, through orifices (18) above the upper edge of the said liquid
trap (10, 26, 27) so as to convey the circulating gases and the
liquid which is condensed in the said second portions into the
column, the said first and second portions being placed in
communication in the upper end (17) of the said internal
lining.
4. Column according to claim 3, characterized in that the said
portions of the internal linings are lined with heat exchange
fins.
5. Column according to claim 4, characterized in that the said heat
exchange fins are of the "straight fin" type (16) in the case of
the said first portions, and are of the "serrated fin" type (20) in
the case of the said second portions.
6. Column according to claim 1 or 2, characterized in that its
cylindrical wall (1) is made, at least in its parts lying facing
the said external jackets (21, 32, 33), of a material which is a
good conductor of heat, particularly aluminium or aluminium
alloy.
7. Method for the cryogenic separation of a mixture containing
hydrogen and CO, of the type comprising a stage of scrubbing the
hydrogen present at the top of the column with a liquefied gas
before it is extracted, characterized in that: it is performed
using a column according to one of claims 1 to 6 into which the
said CO mixture is introduced; the cooling fluid (23) introduced
into the external jackets of the wall of the column is liquid CO;
and the liquefied scrubbing gas introduced into the upper part of
the column is a hydrocarbon.
8. Method according to claim 7, characterized in that the said
liquid CO (23) introduced into the external jackets of the wall of
the column consists of CO initially present in the mixture which
was introduced into the said column.
9. Method according to claim 7 or 8, characterized in that the said
scrubbing hydrocarbon introduced into the upper part of the column
consists of a hydrocarbon which was initially present as an
impurity in the mixture which was introduced into the said
column.
10. Method according to claim 7 or 8, characterized in that the
said liquefied scrubbing hydrocarbon is methane.
Description
[0001] The invention relates to columns for the cryogenic
separation of gaseous mixtures. More precisely, it relates in
particular to columns in which hydrogen can be separated from the
CO and from the methane contained in a synthesized gas, by
scrubbing the hydrogen with liquid methane to purify it.
[0002] It will be noted in what follows that all the pressures
mentioned are absolute pressures.
[0003] One of the main methods of producing hydrogen on an
industrial scale consists in using water vapour to reform a light
hydrocarbon such as methane. This yields a hydrogen/CO mixture
containing residual methane, which can then be treated in various
ways to extract hydrogen in the pure state from it.
[0004] In one of these methods, the synthesized gas containing
about 70% hydrogen, 25% CO and 5% methane is introduced into a
column for the cryogenic separation under high pressure (of the
order of 15 to 45 bar) by scrubbing with methane. The synthetic gas
is then at a temperature of -180.degree. C. The CO and the methane,
containing a little dissolved hydrogen, are carried to the bottom
of the column in the liquid state and are extracted therefrom,
while the hydrogen is extracted from the top of the column in the
gaseous state. The CO/methane/dissolved hydrogen mixture is
introduced into a second column where it undergoes stripping at
medium pressure (of the order of 10 bar). The hydrogen is collected
in the gaseous state at the top of the column, and the CO/methane
liquid mixture is collected at the bottom of the column. This
mixture is -then introduced into a column at low pressure (of the
order of 2.5 bar). The gaseous CO is collected at the top of the
column and the liquid methane is collected at the bottom of the
column.
[0005] The liquid methane collected from the third column is pumped
and introduced in the liquid state into the top of the first column
so as to scrub the hydrogen with methane in order to purify this
hydrogen. The lower the temperature at which this operation is
carried out, the more effective it is. In this particular case, the
desire is to keep the temperature in the entirety of the first
column as close as possible to -180.degree. C., this limit being
imposed by the temperature at which methane solidifies, which is
-182.5.degree. C. For this purpose, as the scrubbing is exothermal,
heat has to be extracted from the circulating matter at various
points in the column. To do this, it is sensible to use liquid Co
produced in a refrigeration cycle.
[0006] Certain devices currently in use for this purpose operate on
the following principle. The synthetic hydrogen/CO/methane gas is
introduced at a given level into the lower part of the column at a
temperature of -180.degree. C. It passes, as it rises up inside the
column, through an active zone of the column, such as a first
packing, where it becomes impoverished in CO and heats up to
-175.4.degree. C. The gaseous mixture is extracted for a first time
from the column above this first packing; it is introduced into a
first passage of a plate-type heat exchanger where its temperature
is brought back down to -180.9.degree. C. and is reintroduced into
the column above its first point of extraction. It continues to
ascend in the column, passing through a second packing where it
becomes impoverished in CO and heats up to -176.1.degree. C. The
gaseous mixture is once again extracted from the column above this
second packing and sent to a second passage of the plate-type heat
exchanger where it is cooled to -180.9.degree. C. then reintroduced
into the column above its second point of extraction. As it
continues to ascend, it passes through a third packing, after which
it is extracted once again from the column to be cooled in a third
passage of the plate-type heat exchanger and is reintroduced at
-180.9.degree. C. into the column above its third point of
extraction. As it continues to ascend, the gas passes through a
fourth and last packing, above which the scrubbing liquid methane
is introduced. As has been stated, the scrubbing of the hydrogen
with liquid methane, which causes CO to condense and mix in with
the liquid methane causes an increase in the temperature of the
ascending gases, entailing extracting them to cool them after each
passage through an active zone such as a packing. It is the
hydrogen purified of its CO under high pressure which is collected
at the top of the column.
[0007] Liquid traps with perforated bottoms, placed between the
various packings are there to collect the descending liquid leaving
a packing and to distribute it over the upper surface of the
packing immediately below it. They also make it possible to
compensate for the pressure drops in the aforementioned cooling
circuits.
[0008] The number of packings, the number of levels at which the
gases are extracted from the column and to which they are returned
after cooling, and the number of passages in the heat exchanger are
given by way of indication. The numbers may be higher or lower than
those which have been described.
[0009] The plate-type exchanger optimally works on the CO collected
at the top of the third column, which is in the liquid state at a
temperature of -182.degree. C. and is vaporized at 2.6 bar under
the effect of heat transfers which take place between it and the
gases extracted from the first column. The exchanger is supplied
with liquid CO by a thermosiphon into which the liquid CO from the
third column is introduced and to which the gaseous CO is returned
after it has passed through the heat exchanger before being
extracted therefrom.
[0010] This first column and the heat exchanger and the
thermosiphon which are appended to-it, constitute a bulky assembly.
In particular, the pipework conveying the synthetic gases from the
column to the heat exchanger and from the exchanger to the column
constitute a complex circuit that it would be desirable to
eliminate.
[0011] The object of the invention is to propose a column for
cryogenic separation, that can be used in a method for producing
hydrogen from a mixture containing hydrogen and CO using scrubbing
of the gases with liquid methane, which is notably less bulky and
less complex than the columns and their auxiliaries customarily
used for implementing this method.
[0012] To this end, the subject of the invention is a column for
the cryogenic separation of gaseous mixtures, characterized in that
it comprises:
[0013] a cylindrical wall;
[0014] means of introducing the gaseous mixture into the said
column;
[0015] at least one assembly consisting of:
[0016] two active zones spaced staggered along the height of the
column and filling the entire cross section thereof;
[0017] a liquid trap located between the said active zones,
consisting of a cylindrical container with a perforated bottom and
the outer side wall of which defines, with the cylindrical wall of
the column, an annular space in which the gases circulating upwards
inside the column can pass after they have passed through the
active zone above which the said liquid trap is positioned;
[0018] an internal lining of the cylindrical wall of the column,
having its lower end located level with the upper edge of a liquid
trap, means for causing the gases leaving the active zone located
below the said liquid trap to pass into the said internal lining,
and means for causing the said gases and the condensed liquid they
contain to leave the said internal lining, returning them to the
interior of the column above the said liquid trap;
[0019] an external jacket of the cylindrical wall of the column,
located facing the said internal lining, comprising means of
introducing a cooling fluid into its lower part and means of
extracting the said fluid at its upper part, the said external
jacket allowing heat transfers between the said cooling fluid and
the gaseous and liquid matter circulating in the internal lining
via the cylindrical wall of the column;
[0020] means for introducing a liquefied gas into the upper part of
the column to scrub the gas extracted at the top of the column;
[0021] means of extracting the most volatile gas from the said
gaseous mixture at the top of the said column,
[0022] and means of extracting, in the liquid state, the least
volatile gas or gases of the said gaseous mixture at the bottom of
the said column.
[0023] According to a preferred embodiment, the said internal
linings comprise, distributed alternately about the internal
circumference of the column, first portions which open at their
lower part through orifices into the said annular space and through
which the gases circulating upwards inside the column can pass, and
second portions opening, in their lower part, through orifices
above the upper edge of the said liquid trap so as to convey the
circulating gases and the liquid which is condensed in the said
second portions into the column, the said first and second portions
being placed in communication in the upper end of the said internal
lining.
[0024] The said portions of the internal linings are preferably
lined with heat exchange fins of the "straight fin" type, in the
case of the first portions, and of the "serrated fin" type in the
case of the second portions.
[0025] Another subject of the invention is a method for the
cryogenic separation of a mixture containing hydrogen and CO, of
the type comprising a stage of scrubbing the hydrogen present at
the top of the column with a liquefied gas before it is extracted,
characterized in that:
[0026] it is performed using a column into which the said mixture
is introduced;
[0027] the cooling fluid introduced into the external jackets of
the wall of the column is liquid CO; and
[0028] the liquefied scrubbing gas introduced into the upper part
of the column is a hydrocarbon.
[0029] As will have been appreciated, the invention consists in
cooling the ascending gaseous mixture not now outside the column in
a separate exchanger, but inside the column itself. This is
achieved by means of a series of jackets external to the wall of
the column, through which the cooling fluid, such as liquid CO,
needed for cooling the gases is circulated. Liquid traps of a
suitable configuration and internal linings of the wall of the
column direct the ascending gases along the wall of the column,
facing the zones at which the external jackets are located, so as
to achieve the desired heat exchange. The internal linings also
reintroduce cooled matter into the central part of the column.
[0030] The invention will be better understood from reading the
description which follows, given with reference to the following
appended figures:
[0031] FIG. 1, which shows, in longitudinal section, a column for
cryogenic separation according to the invention;
[0032] FIGS. 2A and 2B which show, in section and in perspective,
two portions of the column according to the invention viewed as
enlargements of II of FIG. 1, the two portions being offset
angularly according to the planes of section IIA-IIA and IIB-IIB of
FIG. 3;
[0033] FIG. 3 which shows a cross section on III-III of the
column;
[0034] FIG. 4 which schematically shows, in a developed front view
on IV-IV, a portion of the interior of the internal lining of the
column.
[0035] The exemplary embodiment of the invention which will now be
described in detail relates precisely to the cryogenic separation
of hydrogen from a hydrogen/CO/residual methane mixture, with the
hydrogen scrubbed with liquid methane, performed in an example of a
column according to the invention.
[0036] The column for cryogenic separation depicted in FIG. 1
conventionally comprises a cylindrical wall or barrel 1
constituting its main framework. It is made at least partially of a
metal which is a good conductor of heat, such as aluminum or one of
its alloys (in preference to stainless steel) so as to allow easy
heat transfers at least at certain portions of its height, between
its internal medium and the external medium under conditions which
will be seen later on. The lower part of this column is not
appreciably different from known cryogenic separation columns. It
comprises means 2 of introducing the hydrogen/CO/methane mixture
that is the subject of the cryogenic separation treatment into the
column. Typically, this mixture contains 70% hydrogen and 25% CO,
with 5% residual methane which does not react during the operation
of reforming with steam the methane used as starting compound for
the production of the hydrogen/CO mixture. The mixture is
introduced at a temperature of -180.degree. C. into the upper part
of a separator pot 3. The vapours resulting from this mixture pass
through a manifold 4 with a perforated bottom, of conventional
design, located underneath a first packing 5. This manifold 4
extends over the entire internal cross section of the column, as
does the packing 5. Extraction means 6, 7 are provided for
respectively collecting the liquid CO/methane mixtures deposited,
on the one hand, in the bottom of the separator pot 3, and also in
the bottom 8 of the column in the case of the fraction of
CO/methane mixture originating from the manifold 4.
[0037] Having passed through the first packing 5, the ascending
gaseous mixture enters the column portion designed according to the
invention. The gaseous mixture passes into an annular space 9
formed between the wall 1 of the column and a liquid trap 10
consisting of a single cylindrical container with a bottom 11
perforated with holes of small diameter (approximately 4 mm for
example). The outside diameter of the liquid trap 10 is smaller
than the inside diameter of the column so as to define the annular
space 9, the width of which may be a few cm. The upper edge 12 of
the liquid trap 10 rests on a support 13 secured to the wall 1 of
the column, so as to hold the liquid trap 10 in position inside the
column.
[0038] At a level appreciably higher up than that of the upper edge
12 of the liquid trap 10, begins a second packing 14 extending over
a given height H. The wall of the column has an internal lining,
the lower end of which is located at the same level as the upper
edge 12 of the liquid trap 10 and the upper end of which is
preferably located at the same level as or (as depicted), slightly
above, the upper end of the second packing 14. The configuration of
this internal lining differs according to the angular sector of the
cross section of the column being considered. Two types of
configuration are present, these alternating along the internal
circumference of the column which is split into an even number of
angular sectors, twelve of these in the example depicted (see FIG.
3).
[0039] According to a first configuration, demonstrated in FIG. 2a,
the internal lining of the column comprises a portion within which
the gas, leaving the first packing 5, passes through at least one
orifice 15 formed in the lower edge of the internal lining. In the
example depicted, this lower edge is coincident with the support 13
on which the liquid trap 10 rests. As a preference, the interior of
this portion of the internal lining is lined with heat exchange
fins 16. In the preferred example depicted, these heat exchange
fins 16 are of the type conventionally known as "straight fins",
defining approximately straight "corridors" along which the liquid
which condenses inside the lining can descend unimpeded to drop
onto the first packing 5. Likewise, the ascending gaseous mixture
can progress unimpeded between these heat exchange fins, because it
is not hampered by the descending liquid, the latter not being in a
turbulent condition because of the configuration of the straight
fins.
[0040] When the ascending gaseous mixture reaches the upper end 17
of the internal lining, which is not lined with the heat exchange
fins, it has the possibility of redescending, passing through a
portion of the internal lining adjacent to the previous portion,
which is produced according to the second type of configuration
shown in FIG. 2B. When the gaseous mixture, which in the meantime
has partially condensed, reaches the lower zone of the internal
lining, it returns to the internal space of the column, passing
through an orifice 18 formed in the wall 19 of the internal lining
facing towards the inside of the column. The condensed liquid, rich
in CO and in methane, can flow into the liquid trap 10. The
hydrogen-enriched gas continues to ascend in the internal space of
the column and passes through the second packing 14.
[0041] As a preference, as depicted, this portion of the internal
lining produced according to the second type of configuration is
lined with heat exchange fins 20 of the type known as "serrated
fins", which provide a large heat-exchange area and create intense
turbulence within the fluid passing through the lining.
[0042] Heat exchanges intended to return the temperature of the
hydrogen-enriched gaseous mixture to about -180.degree. C. with a
view to encouraging the scrubbing of the hydrogen with the liquid
methane introduced at the top of the column take place between the
mixture present inside the aforementioned lining and a cooling
fluid preferably consisting of liquid CO at -182.degree. C. For
this purpose, according to the invention, facing the said internal
lining, the column has an external jacket 21, defining an annular
space with the wall 1 of the column. The external jacket 21
comprises, in its lower part, means 22 of conveying liquid CO 23.
In its upper part, it comprises means 24 of extracting the gaseous
CO 25 at a pressure of 2.6 bar which forms following the heat
exchanges which take place between the fluids present in the jacket
and in the lining. During these exchanges, the liquid CO gives up
cooling energy to the hydrogen-rich gaseous mixture present in the
internal lining, to bring it down to a temperature very close to
-180.degree. C., before it passes into the second packing 14.
[0043] This operation which, in the prior art, took place in a heat
exchanger separate from the column and required the gaseous mixture
to be extracted from the column, is here performed actually inside
the column. This appreciably reduces the overall bulk of the
installation and simplifies its design.
[0044] To make the installation more efficient, it is advantageous
for the internal lining and external jacket 21 of the column to be
located facing the entire height of the second packing 14. In other
words, the internal lining and the external jacket 21 have their
upper ends located level with or above the upper end of the second
packing 14. In this way it is possible to compensate for the
reheating of the ascending gases over the entirety of the levels at
which it occurs in a favoured way.
[0045] As in the prior art, the liquid CO used as cooling fluid is
advantageously produced from the CO collected at the top of the
low-pressure column where the CO initially present in the synthetic
gas, and collected at the bottom of the column of the invention, is
separated from the methane it contains. This methane is itself used
to scrub the hydrogen in the column of the invention.
[0046] In the example depicted in FIG. 1, the column according to
the invention comprises two other stages similar to the one which
has just been described and which therefore each comprise:
[0047] a liquid trap 26, 27;
[0048] a packing 28, 29 (or, in general, an active zone);
[0049] an internal lining 30, 31;
[0050] an external jacket 32, 33;
[0051] means 34, 35 for conveying liquid CO into the external
jacket 32, 33;
[0052] and means 36, 37 of extracting the gaseous CO from the
external jacket 32, 33.
[0053] It would still be in accordance with the invention if a
greater or lesser number of such stages were to be provided. In
certain cases, one single stage might be sufficient.
[0054] In its upper part, above the last stage at which the cold
energy is supplied to the fluid present in the column, there are
means 38 known per se to allow the liquid methane to be introduced
into the column and to bring it into contact with the gaseous
hydrogen in order to purify the latter. Finally, there are means 39
for collecting the gaseous hydrogen at high pressure present at the
top of the column in the pure state.
[0055] It goes without saying that the column comprises all the
other elements necessary or beneficial to its correct operation
which it is common practice to install in cryogenic separation
columns. In particular, it comprises means 40 for supporting the
packings 5, 14, 28, 29 to allow these to be held in position.
[0056] The head of liquid 41 present in a liquid trap 10
corresponds to the pressure drop experienced by the ascending gases
between the point at which they are withdrawn and the point at
which they are reintroduced into the column.
[0057] By way of indication, a column such as has just been
described, comprising three liquid traps/packing/lining/jacket
assemblies, can afford a reduction of about 20% in the height of
the active part of the column by comparison with the case of an
equivalent column of the conventional type in which the stages of
cooling the ascending gases are performed in an external exchanger.
If the elimination of the exchanger external to the column and of
the pipes connecting it to the column are also taken into
consideration, it can be seen that the column according to the
invention and its auxiliaries may be appreciably less bulky than
the installations of the prior art.
[0058] The example which has just been described is one preferred
embodiment of the invention, and changes may be made thereto
without departing from the spirit of the invention. In particular,
the design of the internal lining of the column may be simplified,
the essential thing being that heat exchanges by the supply of cold
energy to the fluid present in the column should take place through
the wall of the column itself, using a fluid filling a jacket
formed around the external face of the column.
[0059] It goes without saying that the use of the column according
to the invention is not restricted to the application which has
been described and that such a column can be used for types of
cryogenic separation other than the extraction of hydrogen from a
hydrogen/Co/methane mixture. Likewise, the use of methane as
scrubbing gas in this operation is not exclusive. Propane, in
particular, may also be used. Finally, cooling fluids other than
the liquid CO can be used to provide the cold energy to the
ascending gas. For example, liquid nitrogen may be used.
* * * * *