U.S. patent number 3,747,359 [Application Number 05/054,478] was granted by the patent office on 1973-07-24 for gas liquefaction by a fractionally condensed refrigerant.
This patent grant is currently assigned to Linde Aktiengesellschaft. Invention is credited to Martin Streich.
United States Patent |
3,747,359 |
Streich |
July 24, 1973 |
GAS LIQUEFACTION BY A FRACTIONALLY CONDENSED REFRIGERANT
Abstract
A gas stream is liquefied by indirect heat exchange with a
multi-component refrigerant in a closed cooling cycle. The
refrigerant is fractionally condensed and the fractions are
separately evaporated in the closed cycle to cool and liquefy the
gas stream.
Inventors: |
Streich; Martin
(Nieder-Eschbach, DT) |
Assignee: |
Linde Aktiengesellschaft
(Wiesbaden, DT)
|
Family
ID: |
5741575 |
Appl.
No.: |
05/054,478 |
Filed: |
July 13, 1970 |
Foreign Application Priority Data
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Aug 1, 1969 [DT] |
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P 19 39 114.1 |
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Current U.S.
Class: |
62/623 |
Current CPC
Class: |
F25J
1/0022 (20130101); F25J 1/0055 (20130101); F25J
3/0257 (20130101); F25J 1/004 (20130101); F25J
1/0212 (20130101); F25J 3/0233 (20130101); F25J
3/0209 (20130101); F25J 2270/66 (20130101); F25J
2200/70 (20130101); F25J 2250/20 (20130101); F25J
2220/64 (20130101); F25J 2270/18 (20130101); F25J
2200/02 (20130101); F25J 2205/04 (20130101) |
Current International
Class: |
F25J
1/00 (20060101); F25J 3/02 (20060101); F25J
1/02 (20060101); F25j 001/02 (); F25j 003/02 () |
Field of
Search: |
;62/23,24,27,28,40,9,11 |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
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|
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652,208 |
|
Nov 1962 |
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CA |
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110,556 |
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Feb 1961 |
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PK |
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Other References
Kleemenko, One Flow Cascade Cycle, Pergamon Press 1960 Pgs. 34-39
in Prog. In Refrig. Sci. & Tech..
|
Primary Examiner: Yudkoff; Norman
Assistant Examiner: Purcell; Arthur F.
Claims
I claim:
1. A process for the liquefaction of gas or a mixture of gases by
indirect heat exchange with a compressed multi-component
refrigerant circulated in a closed cooling cycle comprising the
following steps:
a. cooling, fractionally condensing and separating said compressed
multi-component refrigerant into higher boiling liquid and lower
boiling gaseous fractions,
b. subcooling all of said higher boiling liquid fractions and
further cooling, liquefying and subcooling said lower boiling
gaseous fractions,
c. expanding all of said subcooled higher boiling and lower boiling
liquid fractions to different pressures, said subcooled higher
boiling liquid fractions being expanded to a higher pressure, and
said subcooled lower boiling liquid fractions being expanded to a
lower pressure,
d. separately evaporating and heating to ambient temperature said
subcooled liquid fractions expanded to different pressures by
indirect heat exchange with said higher boiling and lower boiling
fractions of said multi-component refrigerant and with said gas or
gaseous mixture to be liquefied, without mixing said higher boiling
and lower boiling fractions during evaporation and heating to
ambient temperature,
e. separately recycling said evaporated fractions previously
expanded to different pressures to a multi-stage compressor and
mixing said evaporated fractions only during the compression.
2. A process for the liquefaction of natural gas by indirect heat
exchange with a compressed multi-component refrigerant circulated
in a closed cooling cycle comprising the following steps:
a. cooling, fractionally condensing and separating said compressed
multi-component refrigerant into only a single higher boiling
liquid and a single lower boiling gaseous fraction,
b. subcooling all of said higher boiling liquid fraction and
further cooling, liquefying and subcooling said lower boiling
gaseous fraction,
c. expanding all of said subcooled higher boiling and lower boiling
liquid fractions to different pressures, said subcooled higher
boiling liquid fraction being expanded to a higher pressure, and
said subcooled lower boiling liquid fraction being expanded to a
lower pressure,
d. separately evaporating and heating to ambient temperature said
subcooled liquid fractions expanded to different pressures by
indirect heat exchange with said higher boiling and lower boiling
fractions of said multi-component refrigerant and with said natural
gas to be liquefied, without mixing said higher boiling and lower
boiling fractions during evaporation and heating to ambient
temperature,
e. separately recycling said two evaporated fractions previously
expanded to different pressures to a multi-stage compressor and
mixing said two evaporated fractions only during the
compression.
3. The process of claim 2 wherein the subcooled higher boiling
liquid fraction is expanded to an absolute pressure of not less
than about 5 atmospheres and the subcooled lower boiling liquid
fraction is expanded to a lower absolute pressure of less than
about 5 atmospheres.
4. The process of claim 2 wherein the subcooled boiling liquid
fraction is expanded to an absolute pressure in the range of about
five to 10 atmospheres and the subcooled lower boiling liquid
fraction is expanded to a lower absolute pressure in the range of
about one to five atmospheres.
Description
BACKGROUND OF THE INVENTION
This invention relates to a process for the liquefaction of gases
or gas mixtures by means of a cooling cycle in which is circulated
a cooling medium or refrigerant composed of several components that
are subjected to fractional condensation and in which the condensed
fractions are separately evaporated. The process is especially
suitable for the liquefaction of natural gas.
From German Auslegeschrift 1,272,943, there is known a process of
this type in which cooling media obtained by fractional
condensation of components from the natural gas to be liquefied are
decompressed to a common medium pressure, mixed, recompressed to
the pressure of the natural gas flowing into the plant and again
mixed therewith. It is characteristic of that process that the
several cooling media are decompressed to a common medium
pressure.
From German Offenlegungsschrift 1,501,690, it is also known to
carry out the circulation of the cooling medium in a closed cycle
in such process.
In comparison with the so-called classical cascade process, these
processes have some advantages since only one cooling cycle with
one compressor is needed. However, this single cooling cycle must
be divided up into several circulation branches, with a
corresponding division of the heat exchangers and with complicated
connections resulting therefrom. Furthermore, the utilization of
energy is higher than in the case of the classical cascade
process.
In order to avoid these disadvantages, it has been proposed to
divide up a cooling medium composed of several components and
obtained by fractional condensation, to decompress one partial
stream to a medium pressure and the other partial stream to
approximately atmospheric pressure, to combine again the
decompressed partial streams, to mix the combined streams with the
gas mixture to be liquefied and to compress the total gas. The
process is especially suitable for comparatively small natural gas
liquefaction plants since it does not require a separate natural
gas compressor. In such case, it is necessary that the natural gas
is supplied at low pressure. However, these prerequisites are not
always fulfilled. Thus, for example, the natural gas is frequently
supplied at a pressure which is already sufficiently high.
Furthermore, the mixing of light natural gas and heavy hydrocarbons
always leads to an increased use of energy because of the increased
entropy which arises.
It is an object of this invention to avoid these disadvantages and
to make the process of universal applicability.
SUMMARY OF THE INVENTION
A process has been found for the liquefaction of gas or gas
mixtures by means of a closed cooling cycle in which a circulating
multi-component refrigerant is compressed by a compressor, is
separated by fractional condensation into fractions with different
boiling ranges and these fractions are evaported as separate
streams giving up refrigeration to the refrigerant undergoing
fractional condensation and to the gas or gas mixture undergoing
liquefaction, are recombined and again compressed. According to
this invention, the condensate fractions are separately evaporated
and reheated to about ambient temperature and are again mixed
together during recompression.
The process of this invention is especially advantageous for the
liquefaction of natural gas since only two partial refrigerant
streams fromm a single separator suffice for the liquefaction.
Since the entropy increase by the mixing of cooling medium and
natural gas is avoided, the energy requirement is relatively low.
When using only two partial refrigerant streams, the one with the
higher boiling fraction is decompressed to a medium absolute
pressure, preferably five to 10 ats. (atmospheres), and the one
with the lower boiling fraction is decompressed to a low absolute
pressure, preferably one to five ats. When the gas mixture to be
liquefied is natural gas, the refrigerant or cooling medium is
preferably a hydrocarbon mixture.
When the process of this invention is applied to natural gas and
nitrogen is to be removed therefrom, the natural gas is preferably
subjected, in the course of the cooling thereof, to a preseparation
before being further cooled and fractionated in a nitrogen
rectification column.
BRIEF DESCRIPTION OF THE DRAWING
The invention will now be described on the basis of a specific
embodiment and with reference to the accompanying drawing which
illustrates a process flow diagram for the liquefaction of natural
gas containing nitrogen in which the nitrogen is separated and
discharged in the gaseous state.
DESCRIPTION OF A PREFERRED EMBODIMENT
The natural gas to be liquefied, which has the following
composition:
N.sub.2 14.3% by volume CH.sub.4 82.4% by volume C.sub.z H.sub.6
2.6% by volume C.sub.3 H.sub.8 0.4% by volume C.sub.4 H.sub.10 0.3%
by volume
enters the plant through pipe 1 at an absolute pressure of 20 ats.
and at a temperature of 30.degree. C. In purification plant 2, it
is freed from impurities, especially from water and carbon dioxide,
and then passed via pipe 3 successively through heat exchangers 4,
5 and 6. It is thereby cooled to a temperature of about
-100.degree. C. and the heavy hydrocarbons condense out. These are
separated in separator 7 and withdrawn through pipe 8. The gaseous
portion which remains, consisting preponderantly of methane and
nitrogen, flows through pipe 9 into heat exchanger 10 where it is
cooled to about -120.degree. C. and partially liquefied.
In order to simplify the separation of nitrogen in this stream in
nitrogen rectification column 11, the liquid phase is separated
from the gaseous phase in separator 12. The gaseous phase is
enriched in nitrogen, whereas the liquid phase is depleted in
nitrogen. The liquid and gaseous phases pass via pipes 13 and 14,
respectively, into heat exchanger 15 where they are cooled to about
-140.degree. C. and then used to heat the sump liquid of nitrogen
column 11 by means of coils 17 and 16, respectively, whereby they
are further cooled. The liquid phase is then decompressed via
expansion valve 18 into the middle portion of nitrogen column 11,
whereas the gaseous phase is first still further cooled in heat
exchanger 19 to about -183.degree. C. and thus liquefied before it
is decompressed via expansion valve 20 into the top portion of
nitrogen column 11.
In nitrogen column 11 which is at an absolute pressure of four
ats., the nitrogen contained in the natural gas is completely
separated and withdrawn via pipe 21 from the top of column 11 at a
temperature of -183.degree. C. It successively gives up its
refrigeration in heat exchangers 19, 15, 10, 6, 5 and 4 and is then
available at ambient temperature. It can also previously be
decompressed to atmospheric pressure. Liquefied methane is
withdrawn via pipe 22 from nitrogen column 11. It is then, in known
manner, decompressed into a reservoir which is not illustrated in
the drawing; the resulting flash and evaporation gases can also be
utilized for recovering refrigeration therefrom.
The refrigeration necessary for cooling and liquefying the natural
gas is produced in a closed cooling cycle in which a multicomponent
refrigerant is circulated and subjected to fractional condensation.
The refrigerant or cooling medium is preponderantly composed of
methane, ethane, propane and butane. At about ambient temperature,
one fraction of the refrigerant enters compressor 24 at an absolute
pressure of two ats. and the other fraction enters compressor 24 at
an absolute pressure of seven ats. The fractions thus recombined
are compressed to about 25 ats. absolute and cooled in water cooler
25.degree. to about 30.degree. C. The refrigerant is then further
cooled in heat exchanger 4 to about 0.degree. C., whereby it is
partially liquefied. It passes via pipe 26 into separator 27 in
which the liquid phase is separated from the gaseous phase. The two
separated phases now provide the two fractions or partial
refrigerant streams. The partial refrigerant stream formed from the
liquid phase and containing only a little methane and the heavier
hydrocarbons, ethane, propane and butane in about equal parts, is
first passed by means of pipe 28 through heat exchanger 5 to effect
further cooling of the partial stream and then is decompressed by
expansion valve 29 to an absolute pressure of about 7.5 ats. This
partial stream then evaporates at this pressure while giving up
refrigeration in heat exchangers 5 and 4 and is returned to an
intermediate stage of compressor 24.
The partial refrigerant stream obtained from the gaseous phase
leaving separator 26 consists preponderantly of methane and has a
modest content of ethane and propane, whereas the content of butane
is small. This second partial stream in pipe 30 is first cooled in
heat exchangers 5, 6, 10 and 15 to about -140.degree. C. and thus
liquefied and then, according to this invention, is decompressed by
expansion valve 31 to an absolute pressure of about 2.5 ats.
Thereafter, this second stream evaporates, successively gives up
refrigeration in heat exchangers 15, 10, 6, 5 and 4 and finally
passes via pipe 23 back into compressor 24.
A special advantage of the process of this invention is that it can
be carried out with only a single subdivision of the closed cooling
cycle.
* * * * *