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Патент USA US3083554

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April 2, 1963
F. JAKOB
3,083,544
RECTIFICATION 0F GASES
Filed Sept. 25, 1959
I
3 Sheets-Sheet 1
Fig.
I
21?24
25/
' April 2, 1963
F. JAKOB
3,083,544
RECTIFICATIQN OF GASES
Filed Sept. 23, 1959
S'ShQetS-Sheet 2
‘Fig.2
April 2, 1963
F. JAKOB
3,083,544
RECTIFICATION OF GASES
Filed Sept. 23, 1959
3 Sheets-Sheet 3
ilnited grates Patent:
3,683,544?
Fatented Apr. 2, 1§$3
1
gas mixture under higher pressure, lique?ed, supercooled,
3,083,544
RECTIFICATIGN 0F GASES
Fritz Jakob, Puliach, near Munich, Germany, assignor to
Gesellschatt fur Linde’s Eismaschinen Alrtiengeseli
schatt Hoilriegelkreuth, near Munich, Germany, a
company of Germany
Filed Sept. 23, 1959, Ser. No. 841,749
Claims priority, application Germany Sept. 24, E58
10 Claims. ((11. 62-28)
This invention relates to the art of rectifying gaseous
mixtures, and is concerned with the provision of a process
and apparatus for obtaining a balanced cold economy in
the production of gas mixtures and/ or gas mixture com
ponents, which are under a higher pressure, through recti
?cation.
The known methods for obtaining a balanced cold
economy in the production of oxygen, which is under an
elevated pressure, involve the recti?cation of air by ex
traction in the liquid state and bringing it to the desired
gaseous pressure state, for example, tempered to ambient
air; compressing an amount of gas——tal<en from the pre
liminary recti?cation and heated again in counter?ow in
the heat exchangers for the incoming air-to a high pres
sure, before it is fed to the liquid oxygen, compressed to a
higher pressure, for its evaporation and heating; and trans
forming it subsequently (if necessary, after additional heat
exchange and expansion) into the preliminary or low
pressure recti?cation. This method requires the arrange
ment of high-pressure compressors whose particular dis
advantage is the contamination of the gases by oil and
moisture. Besides, the high-pressure compressors are
very expensive, and are uneconomical in operation.
According to the present invention, the method for
obtaining a balanced cold economy in the production of
compressed gaseous mixtures and/ or gas mixture compon—
cuts from the recti?cation of one or several gas mixtures
by extraction in the liquid low-pressure stage and by bring
ing them to the desired gaseous, medium- or high-pressure
fed to the rectifying and washing device for said gas
mixture and then mixed with the resulting gas mixture,
one has an example of an open medium-pressure circuit.
These medium-pressure circuits, in which the pressure
rarely attains or exceeds 30 atmospheres absolute, are of
particular advantage because of the possibility of using
dry-running compressors, since the gas to be compressed
is not contaminated and, therefore, needs no after-treat
ment or complicated puri?cation.
An open medium-pressure circuit may, however, be ac
companied by a displacement of cold, so that in order to
return it from the recti?cation of one gas mixture to that
of the other, an amount of gas must be extracted from the
preliminary recti?cation, lique?ed in indirect heat-ex
change against the gas mixture formed by the supply of
a part of the lique?eld gas effecting the partial heating,
and subjected again to a preliminary recti?cation. An
other possibility of exchanging cold between the two gas
mixtures taken from a recti?cation of each consists in that
the complete heating of the component brought to a
higher pressure and the preliminary cooling of the com
pressed gas mixture which is to be separated is eifected in
mutual heat exchange, preferably by the interposition of a
so-called “brine circuit,” because of the ?re and explosion
hazard.
Embodiments of the invention are represented in the
accompanying drawings to enhance the understanding.
Similar parts have been designated with the same refer
ences.
In the drawing,
FIG. 1 is a diagrammatic representation of an apparatus
organization for carrying out the above~described process,
with particular applicability to the separation of the com
ponents of air;
PEG. 2 is a diagrammatic representation of a modi?ed
form of the apparatus organization shown in FIG. 1;
and
FIG. 3 is a diagrammatic representation of a further
state, for example, tempered to ambient air, is character 40 modi?cation of the apparatus organization shown in FIG.
1, with particular applicability to the provision of com
ary recti?cation, heated in counter?ow to the incoming
pressed nitrogen for production of synthetic ammonia
gas mixture, cooled by heat exchange ‘for evaporation and
gas.
heating of the liquid component, compressed to a higher
FIGURE 1 shows the most important parts of an ap
pressure, and subjected to partial heating and subsequent
paratus for the decomposition of gas mixtures, air being
work-producing expansion, after the lique?ed components
used as the example.
ized in that an amount of gas is taken from the prelimin
have been separated and returned.
In contrast to the
existing methods, this new method has the advantage that
the gas taken from the preliminary recti?cation is brought,
without pressure increase, by heat exchange to the com
ponent compressed to a higher pressure, and expanded
work-producingly after partial heating. This gas is thus
maintained in its pure state and requires no further treat
ment. It is not particularly characteristic of the process
according to the invention where the expanded gas is con
ducted, but preferably it can be conducted to the low
pressure recti?cation or at least partly exhausted, if nec—
essary after further heat exchange in counter?ow with
production gases, and after heating in the regenerators,
etc. The partial heating of the gas before the work
producing expansion is effected preferably by heat ex
change with a compressed gas of a so-called closed or open
medium-pressure circuit. The quantity of gas effecting the
partial heating for the work-producing expansion has its
pressure reduced and is subjected to recti?cation, for ex
ample, in the preliminary or in the low-pressure stage.
Compression under medium pressure preceded by heating
The apparatus consists essentially of an intake pipe 1
for air compressed to about 5.3 to 6.5 atmospheres ab
solute; a pair or" periodicallly reversible regenerators 2 for
cooling the incoming air; a connecting pipe 3‘ to the sump
of a rectifying column 4, with a pressure column 5; a low
pressure column 6 and a condenser 7; a line 8, with an
expansion valve 9, vfrom the sump of the pressure column
5, to the low-pressure column 6 for the lique?ed gas
mixture; a pipe ill’, with an expansion valve 11, from the
pressure side of the condenser '7 to the head of the low
pressure column ‘6, for lique?ed nitrogen with connected
counter-flow heat exchanger 12, an extraction pipe extend
ing through this to the regenerators 2; a second inter
posed counter?ow heat exchanger 14; a discharge pipe 15
for the nitrogen produced; an extraction pipe 16, from
the low-pressure part of the condenser 7, for liquid oxy
gen; a liquid gas pump 17 for compressing oxygen to the
desired higher pressure; a pressure pipe 18 to a counter
?ow heat exchanger 19, in which the lique?ed component
(here oxygen), compressed to a higher pressure, is heated;
and an oxygen pipe 29 with an addition to the apparatus
and followed by cooling of the gas in counter-?ow to itself
according to the invention, which is characterized by an
conveniently forms a closed medium-pressure circuit. But
extraction pipe 21 from the pressure column 5, to the
if the gas which e?ects the partial heating of the gas 70 regenerators 2 for extracting and heating air from the
destined for work-producing expansion is compressed to a
pressure column, heating coils 22 in the regenerators 2;
pressure suitable for obtaining the desired compressed
a line 23 to the counter?ow heat exchanger 19; a post
3,088,544;
3
connected liquid separator 24, with a return pipe 25 for
the condensate and a gas pipe 26, to a heat exchanger 27,
Whose opposite faces are under medium pressure; a feed
4%
heat exchanger 68, thereby giving o?" again (as in the
preceding example) its heat of liquefaction to the air to
be expanded in the turbine 29. This nitrogen, which is
lique?ed in the counter?ow heat exchanger 68, is slightly
pipe 28; an expansion turbine 29; an outlet 30 with a
branch pipe 31; an extraction pipe 32 for air from the 5 supercooled in the counter?ow heat exchanger 69 against
residual gas, and then arrives through the line 70 in the
pressure column; a counter?ow heat exchanger 33 for
liquid state in the gas plant 62, where one part of is
heating this air; a pipe 34; a dry-running compressor 35
used for washing in the wash column, 71 while the other
with a post-connected cooling device; a pipe 36 to the
part is fed directly to the hydrogen-nitrogen mixture in 72. ‘
pounter?ow heat exchanger 33 for cooling the air com~
A great amount of liquid nitrogen has thus been fed to
pressed to medium pressure; ‘a pipe 37 to the heat ex
changer 27 for partial heating of the work-producing,
expanding air; a discharge pipe 38 with ‘an expansion
valve 39, to the pipe 3 and into the pressure column 5,
respectively; and a pipe 49 with a cut-oil member 41 is
provided between the pipes 21_and 26 to transfer com- ,
pressed air, if necessary.
The medium-pressure circuit, represented by the parts
.32, 33, 34, 35, 3'6, 37, 38 and 39, which is self-contained
by the extension into the parts 3, 5 and 21, is arranged
because the regenerators 2 work with excess discharge
.so that there is no excess heat available that can be used
for heating the air to be expanded in the turbine 29.
The partial heating of the air to be expanded in the tur
the gas apparatus 62, much more than it needs to com
pensate for its own cold losses. A corresponding amount
of liquid must, therefore,‘ be again removed from the
apparatus 62 in order to balance its cold economy. To
this end, nitrogen is extracted from the pressure column
5 and is fed to the counter?o-w heat exchanger 72.. In
counter?ow heat exchanger 72 this nitrogen, taken from
the pressure column 5, is lique?ed by heat exchange with
the liquid nitrogen evaporating in the hydrogen mixture,
‘and is introduced again into the air plant. The cold,
which the liquid nitrogen has conducted from the counter
?ow heat exchanger 69 to the gas apparatus 62, has now
returned to a great extent to the air separation plant 61,
and only so much is left in the gas plant 62 as is necessary
bine 29 ‘is therefore effected in the counter-?ow heat
exchanger 27, which is interposed in the medium pressure
circuit, by taking over the heat of liquefaction from the air
' for compensating for the cold losses in the gas plant 62.
The crude gas is cooled in the counter?ow heat ex
conducted in the medium-pressure circuit. If the amount
of air issuing from the separator 24 is not su?irc-ient to
produce the necessary cold in the work-producing ex
nitrogen mixture issuing through the line 75. a The crude
gas arrives in line 76, and is cooled in a counter?ow
pansion taking place after the partial heating, the amount
30 precooler 73 to about '5‘? C. and the condensed water is
is increased by adding pressure-column air by way of
the pipe 40 and the valve 41. Through'the pipe 3% a
portion (usually a small portion) of the expanding air
‘is injected into the low-pressure column, another (usually
larger) portion is added to the nitrogen issuing through
the pipe 13 by Way of the branch line 31.
FIGURE 2 shows, in a practically identical device for
carrying out the same process, a'variation in the arrange
changers 73 and 74, in counter?owrwith the hydrogen
stripped off in the separator 77. In' the following counter
?ow-cooler 74, the gas is cooled to about ——5_0° C. It
then enters a gel drier and from there-in the counter?ow
heat ‘exchangers proper 79 and 8.0, namely the hot leg
(79) and the cold leg (80). From the cold leg 80 it is V
transferred to the evaporating vessel 81, where it is cooled
to a constant temperature of about 85° K. by means of
liquid nitrogen or residual gas evaporating .without'pre‘s
sure. The crude gas arrives at this temperature through
variation instead of a medium-pressure circuit for air 40 the line 82 in the wash column 71, and is here converted
to pure hydrogen-nitrogen mixture. The washed-out'co'n
from the pressure column, a closed medium-pressure cir
stituents leave the wash column 71 at the sump 83' as
cuit ‘for nitrogen from the pressure column-is provided.
residual gas in liquid form through the line' 84. This
.Nitrogen is extracted from the condenser 7, through the
lique?ed residual gas is fed to the evaporating vessel 81
pipe ‘51, of the pressure column 5: it is heated in the
and is used there for cooling the crude gas, another por
heatexchanger‘SZ and conducted through the line 53 to
ment of the medium-pressure circuit, according'to which
'the medium-pressure, dry-running compressor 54, after
cooled and cooled by the line 55 in the heat exchanger
52 in counter?ow to itself, conducted through the line
tion arrives in liquid form in the air separation plant 61
. and is heated there in the counter?ow heat exchanger 69
and in the counter?ow heat exchanger 66, against the
entering medium-pressure nitrogen. The heated residual
56 to the counter?ow heat exchanger 27 for liquefaction,
where the partial heating of the air to be expanded is 50 gas leaves the plant 61 byway of the line 85. -In order
.to utilize the cold still contained in the oxygen after pass
reflected, and returned to the pressure column 5 through
ing through the heat exchanger 19, a brine circuit is inter
posed between the oxygen line 29 and the counter?ow
‘heat exchanger 73 and 74 of the gas separation part. This
connection of an air separation plant 61 for the produc
tion of compressed oxygen and compressed nitrogen with 55 brine circuit 86 transfers the cold-still contained in the
oxygen—over the heat exchanger 37 to the crude gas
a gas separation plant 62, for the production of synthetic
and serves to precool the crude gas. Because the com
ammonia gas from converter gas which consists of hy
: pressed oxygen leaves the counter?ow heat-exchanger
drogen, nitrogen, carbon monoxide and methane. The
the line 57 and the expansion valve 58.
.
The embodiment according’ to FIGURE 3 shows the
"19 relatively cold in this method of low-pressure heatre'x
‘oxygen is to be supplied with a pressure of about 40
atmospheres, and the nitrogen ‘is to be brought to the 60 'change, the great cold supply can be utilized with ad
pressure of the crude gas, that is, about 25 atmospheres.
For heating the turbine gas there is used the nitrogen
which must, in any event, be transferred to the gas plant,
that is, the “production nitrogen.” The production nitro
gen is extracted in the line 63 from the pressure column
5, under its pressure, conducted in counter?ow to the
vantage and the otherwise necessary cooling ,by ammonia,
which requires energy, can be avoided.
I claim:
" 'V
.
1. In a process vof separating compressed gas mixtures
by recti?cation in a preliminary ‘recti?cation column and
incoming air in spirals 64 and heated, brought outside
the separation apparatus, for example, by means of the
at least one further recti?cation column at low tempera
ture and the production of high pressure gases thereof,
‘ ?ow heat exchangers“: and 67, approximately ‘to the start
it in counter-?ow to the incoming gas mixture, vaporizing
the method of producing cold which comprises withdraw- ‘dry-running compressor 65 to about 25 atmospheres ab
solute, and’is subjected to a heat exchange, after recool 70 ing a component of a gas mixture to ,be separated from
a rectifying column at low' pressure in the .liquid's'tate, '
ing in an after-cooler (not shown) in counter?ow with
pumping
said liquid to said high pressure;-w_ithdrawing a
the residual gas arriving from the gas plant and with the
gas from the preliminary recti?cation column and heating
hydrogen-nitrogen mixture. It is cooled, in the counter
of its liquefaction, and then lique?ed in the counter?ow
said high pressure liquid .byheat-exchange with said gas,
3,083,544
5
6
thereby condensing said gas at least partially to form a
changer and from there through a third heat-exchanger,
liquid part and a gaseous part thereof, separating the
gaseous part from the condensed and lique?ed part of
said gas, leading the lique?ed part of said gas into said
preliminary recti?cation column, warming the gaseous
part of said gas and expanding it by the production of
external work.
2. vIn a process of the separation of compressed air by
recti?cation in a preliminary recti?cation column and at
means connecting said heat-exchanging line with an ex
pansion device and with a condenser of said washing
device, means connecting said expansion device with said
high pressure column, means connecting the foot of the
washing tower of said other separation unit with said
third heat-exchanger, means connecting said third heat
exchanger with the one of said two ?rst-exchangers, means
connecting said washing device with the other of said two
least one further recti?cation column at low temperature 10 ?rst heat-exchangers.
7. "In a process of separating a compressed gas mix
and the production of high pressure oxygen thereof, the
ture by recti?cation in a preliminary recti?cation column
method of producing cold which comprises withdrawing
and at least one further recti?cation column at low tem
oxygen from a rectifying column at low pressure in the
perature and the production of high pressure gases there
withdrawing a gas from the preliminary recti?cation 15 of, cooperating with a process of recti?cation and puri
?cation of a compressed crude synthesis gas mixture to be
column and heating it in counter-?ow to the incoming
washed with a liquid component of said gas mixture to
gas mixture, vaporizing said high pressure liquid by heat
be separated, which comprises withdrawing said gas from
exchange with said gas, thereby condensing said gas at
a rectifying column at low pressure in the liquid state;
least partially to form a liquid part and a gaseous part
thereof, separating the gaseous part from the condensed 20 pumping said liquid to said high pressure; withdrawing a
gas from the preliminary recti?cation column and heat
and liquefied part of said gas, leading the lique?ed part
ing it in counter-?ow to the incoming gas mixture; va
of said gas into said preliminary recti?cation column,
porizing said high pressure liquid by heat-exchange with
warming the gaseous part of said gas and expanding it
said gas, thereby condensing the latter at least partially
by the production of external work.
3. Apparatus for the separation of gas mixtures com 25 to form a liquid part and a gaseous part thereof; separat
liquid state, pumping said liquid to said high pressure;
prising a conventional gas separation device with a two
column rectifying device and a regenerator arrangement
for heat-exchange and cooling of the gas mixture, at gas
conduit connecting the lower part of the high pressure
column of said rectifying device with the cold ends of
heating coils inside the regenerators, a pump connected
to the sump of the low pressure column, a heat-exchanger
for evaporating the high pressure liquid, means connect
ing the high pressure side of said pump to said heat-ex
changer, means connecting the warm ends of said heat
ing coils to the second channel of said heat-exchanger,
ing the lique?ed part and leading it into said preliminary
recti?cation column; warming the gaseous part of said
gas and expanding it by the production of external Work;
withdrawing a higher boiling component from the recti?
cation column and heating it in counter-?ow to said in
coming compressed gas mixture; compressing said compo
nent and cooling at least part of said compressed gas by
heat-exchange with the residual gas withdrawn from a
further rectifying and washing device employed for wash
ing a compressed crude gas mixture; liquefying said com
pressed gas by heat-exchange with the gas to be expanded,
warming said gas thereby; supercooling said lique?ed
means connecting the cold end of said second channel to
compressed gas by heat-exchange with said residual gas
a liquid separator, conduit means for returning the con
and passing it into said rectifying and washing device
densate from said separator to the pressure column, gas
lines from the upper end of said separator to the cold 40 and washing therein said compressed crude gas mixture,
an amount of cold being returned from the rectifying and
end of a second heat-exchanger, means for passing com
washing device for said compressed crude gas mixture to
pressed gas through the second channel of said second
the recti?cation column of line other gas mixture by with
heat-exchanger, means connecting the warm end of said
drawing a quantity of gas from the preliminary recti?ca
second heat-exchanger with the inlet of an expansion tur
tion column of the latter, liquefying said gas by indirect
‘nine and means connecting the outlet of said turbine with
45
the low pressure column.
heat-exchange with the washed compressed gas mixture,
and passing said lique?ed gas into the preliminary recti
4. Apparatus as claimed in claim 3 in which said
fying column.
second channel of said second heat-exchanger is con
8. Apparatus for the separation of gas mixtures com
nected into a closed pressure circuit, consisting of a com
pressor and at least one further heat-exchanger.
prising a conventional gas sepanation device with a two
5. Apparatus as claimed in claim 3 in which said sec 50 column rectifying device and a regenerator arrangement
ond channel of said second heat-exchanger is connected
for heatexchange and cooling of the gas mixture in con
into a pressure circuit, the pressure circuit consisting of
nection with another gas separation unit consisting of
the high pressure column of the two-stage rectifying
heat exchangers for cooling a gas to be washed and a
device, means for conducting gas from said high pressure
column through a ?rst channel of a heat-exchanger to a
compressor combined with a cooler, means for conduct
ing high pressure gas from the compressor combined with
washing device, a gas conduit connecting the lower part
of the high-pressure column of said rectifying device with
the cold ends of heating coils inside the regenerators, a
pump connected to the sump of the low-pressure column
of said rectifying device, a heat-exchanger for evaporat
a cooler through a second channel of said heat exchanger
and from said following second channel of said second
heat-exchanger to an expansion device, means for con
ing high-pressure liquid, means connecting the high
ducting expanded gas from said expansion device to said
high pressure column.
6. Apparatus according to claim 3 in connection with
another gas separation unit consisting of heat—exchangers
second channel of said heat-exchangers, means connecting
pressure side of said pump to said heat-exchanger, means
connecting the warm ends of said heating coils to a
[the cold end of said second channel to a liquid separator,
conduit means for returning condensate from said sepa
for cooling a gas to be washed and a washing device, the
rator to the pressure column, gas lines from the upper
connection consisting of means connecting the head of the
end of said separator to the cold end of a second heat
high pressure column of the conventional gas separation
exchanger, means for passing compressed gas through a
device with heating coils contained in the regenerators,
second channel of said second heat-exchanger, means con—
means connecting the warm ends of said coils with a
70 meeting the warm end of said second heat-exchanger with
compressor and an aftercooler, means connecting the
the inlet of an expansion turbine and means connecting
aftercooler with a heat-exchanging line conducting
the outlet of said turbine with the low-pressure column,
through one ?rst heat-exchanger as well as another first
means connecting the head of a high-pressure column of
heat-exchanger connected to the one heat~exchanger in
said ‘conventional gas separation device with heating coils
parallel and from there through said second heat-ex
contained in the regenerators, means connecting the warm
3,083,544
8
7
prising .a conventional gas separation device with a two
ends of said coils with a compressor and an aftercooler,
means connecting the aitercooler with a heat-exchanging
column rectifying device and a regenerator arrangement
for heat-exchange and cooling of the‘ gas mixture in con
line conducting through one ?rst heat~exchanger tasiwell
nection with ‘another gas separation unit consisting of
as another ?rst heat-exchanger connected to the one heat
heat exchangers for cooling a gas to be 'washed and a
exchanger in parallel and from there through said sec
ond heat-exchanger and'from there through a third heat
washing device, a gas conduit connecting the lower part
of the high-pressure column of said rectifying device
with'the cold ends‘ of heating coils inside the regenena
exchanger, means connecting said heat-exchanging line
with an expansion device and with a condenser of said
tors, a pump connected to the sump of the low-pressure
washing device, means connecting said expansion device
with said high~pressure column, means connecting ‘the 10 column of said rectifying device, va heat-exchanger for
evaporating high~pressure liquid, meansconnecting the
foot of the washing tower‘of said other ‘separation unit
high-pressure side of said pump to said heat-exchanger,
with said third heat-exchanger, means connecting said
third heat-exchanger with the one of said two ?rst heat
means connecting the warm ends of said heating coils
exchangers, means connecting said washing device with
to a second channel of said heat-exchangers, means con
the other of'said two ?rst heat-exchangers, means con 15 necting the cold end of said second channel 'to a liquid
separator, conduit means for returning condensate from
' necting a line for withdrawing part of a separation prod
said separator'to the pressure column, gas lines from the
not from 'the top of the high-pressure column, a ?rst
upper end of said separator to the cold end of a second '
heat-exchange channel in an evaporation heat-exchanger
heat-exchanger, means for passing compressed gas
of said separation product lique?ed‘the-rein to the top‘ of 20 through a second channel of said second heat-exchanger,
means connecting the warm end of said second heat
said high-pressure column, the second channel of said
exchanger with the inlet of an expansion turbine and
evaporation-heat-exchanger being connected with the top
means connecting the outlet of said turbine with the low
of said washing‘ tower and with said heat-exchanging line
pressure column, means connecting the head of a high
back of said third heat-exchanger and with said other
heat-exchanger of said two ?rst heat—exchangers,‘ and with 2,5 pressure column of said conventional gas separation de
vice with heating coils contained in the regenerators,
the heat-exchanger cooling the :gas to 'be Washed, said
of said other gas separation unit and a line for the return
means connecting the warm ends of said coils with a
compressor and an 'aftercooler, means connecting the
apparatus further including a heat-exchanger one chan
ml of which is connected in series with heat-exchangers
aftercooler with a heat-exchanging line conducting
of a' precooling arrangement for the compressed crude
'g'as mixture'to be washed and the other channel of which 30 through one ?rst heat-exchanger as well as another ?rst
heat-exchanger connected to the one heat-exchanger in
is connected to the heat-exchanger in which the compo‘
parallel and from there through said second heat-.
nent pumped to higher pressure is evaporated.
'
exchanger and from there through a third heat-exchanger,
' 9. In 'a process of separating a compressed gas mix
means ‘connecting said heat~exchanging line with an ex
ture by recti?cation in a preliminary recti?cation column
and at least one further recti?cation column at low tem 35 pansion device and with a condenser of said washing
device, means connecting said expansion device with said
high~pressure column, means connecting the foot ‘of the
perature and the production of high pressure‘ gases
thereof, cooperating with a process of recti?cation and
washing tower of said other separation unit with said
third heat-exchanger, means connecting said third heat-V
[puri?cation of a compressed crude synthesis gas mixture
‘to be washed with a liquid component of'said'ga's mix
exchanger with the oneof said two ?rst heat-exchangers,
means connecting ‘said washing‘device with the other of
ture to be separated, which comprisesvvithdnawing a
lower boiling component of the gas mixture to he sepa
' ‘liquid
rated from
state; apumping
rectifyingthecolumn
liquid‘atto low
saidpressure'in
high pressure;
said two ?rst heat-exchangers, means connecting a line
for withdrawing part of ‘a separation product from the
top of the high-pressure column,‘ a ?rst heat-exchange
‘withdrawing a gas from the preliminary recti?cation col
umn and heating it in counter-?ow to the‘ incoming gas 45 channel in an evaporation-heat-exchanger of said other
gas separation unit and a line for the return of said sepa
nation product lique?ed therein to the top of said high
‘exchange with said gas, thereby condensing said gas at
pressure' column, the second channel of said evaporation
least partially to ‘form a liquid part and :a gaseous part
mixture; vaporizing said‘ high pressure liquid‘ by heat—
heatexchanger ‘being connected with the top’ of said
thereof; separating the gaseous part from the condensed
and lique?ed part of said gas; leading the‘ lique?ed part 59 washing tower and with‘ said heat-exchanging line back ,
of said third heat-exchanger and with said other heat-'
of said gas into’ said preliminary recti?cation column;
exchanger of said ?rst two heat-exchangers, and with the
‘warming the gaseouspart of said gas‘tand'expandin‘g‘i‘t
by the production of external work; withdrawing a higher
boiling component, fromthe recti?cation columnand
heating it in counter-?ow to said incoming compressed
gas mixture; compressing said component and cooling ‘it
at'least partly by heat-exchange with a residual gas, ‘the
hearty-exchanger cooling the gas to be washed.
55
residual gas withdrawn from a device of said puri?cation
of said crude gas; liquefying said higher boiling compo
nent withdrawn from said recti?cation column by heat
exchange' with the gas to 'be expanded; supercooling'said
60
’ ' '
'
'
References Cited in the ?le of this patent
UNITED STATES PATENTS
2,122,238
Poll-itzer _____________ __ June 28, 1938
2,708,831)
2,785,548
2,822,675
Wilkinson ____ _..'_.__'_____ May 24, 1955
Becker .- ___________ _.'._'_ Mar. '19, 1957
Grenier ____'_ ____ __'_____ Feb. 111, i958
lique?ed higher boiling component by heat-exchange with
2,827,775
‘said residual gas; passing at least‘part of said supercooled
liquid into said device of said puri?cation; and washing
2,895,304
Wucherer et al; ________ __ July 21, v1959
884,203
Germany ____________ __ June 11, 1953
therein said compressed crude gas mixture.
Linde _______ ..;. ______ __ Mai‘. 25, 1958
FOREIGN ‘PATENTS-
'
10. ‘Apparatus for the separation of ‘gas mixtures com
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