U.S. patent number 3,596,473 [Application Number 04/786,595] was granted by the patent office on 1971-08-03 for liquefaction process for gas mixtures by means of fractional condensation.
This patent grant is currently assigned to Messer Griescheim GmbH. Invention is credited to Martin Streich.
United States Patent |
3,596,473 |
Streich |
August 3, 1971 |
LIQUEFACTION PROCESS FOR GAS MIXTURES BY MEANS OF FRACTIONAL
CONDENSATION
Abstract
A process for the liquefaction of gas mixtures by at least two
open partial cycles with different boiling points includes
premixing the gas mixture with the cycle media and by means of a
compressor bringing it to an elevated pressure and subjecting it to
a fractional condensation where the cycle media and the more
difficulty boiling mixture constituents are precipitated as liquid
fractions in separators. The liquid fraction of the first separator
is divided into two partial streams. The first stream, which forms
the first partial cycle, after expansion to an average pressure
gives off coolness from cycle gas and gas mixture to be liquefied
to the mixture streaming to the first separator and again conducts
back to the compressor. The second stream is deep-cooled, expanded
to about atmospheric pressure and admixed to the last cycle medium
streaming back to the compressor. Furthermore, it is proceeded with
the compressor of the subsequent separator accordingly, the
expansion of the first partial streams occurring at average
pressure until finally the liquid precipitating in the last
separator after cooling of itself and expanding to about
atmospheric pressure, gives off coolness to the gas mixture to be
liquefied and to the other separated cycle media and is again
conducted to the compressor.
Inventors: |
Streich; Martin
(Niedereschbach, DT) |
Assignee: |
Messer Griescheim GmbH
(Frankfurt am Main, DT)
|
Family
ID: |
5676819 |
Appl.
No.: |
04/786,595 |
Filed: |
December 24, 1968 |
Current U.S.
Class: |
62/612 |
Current CPC
Class: |
F25J
1/0045 (20130101); F25J 1/004 (20130101); F25J
1/0202 (20130101); F25J 3/0209 (20130101); F25J
3/0257 (20130101); F25J 3/0233 (20130101); F25J
1/0022 (20130101); F25J 2250/20 (20130101); F25J
2270/88 (20130101); F25J 2200/02 (20130101); F25J
2200/70 (20130101); F25J 2205/04 (20130101) |
Current International
Class: |
F25J
1/00 (20060101); F25J 3/02 (20060101); F25j
003/00 (); F25j 003/02 (); F25j 003/06 () |
Field of
Search: |
;62/23,24,27,28,29,40 |
References Cited
[Referenced By]
U.S. Patent Documents
Other References
Kleemenko, "One Flow Cascade Cycle," in Progress In Refrigeration
Science and Technology Vol I Pergamon Press, New York 1960 pps
34--39.
|
Primary Examiner: Yudkoff; Norman
Assistant Examiner: Purcell; Arthur F.
Claims
I claim:
1. A process for the liquefaction of hydrocarbon gas mixtures by
means of at least two open refrigeration cycles of media,
consisting of heavy components of the gas to be liquefied and
having different boiling ranges wherein the gas mixture is premixed
with the cycle media and brought to an elevated pressure by a
compressor, and is subjected to a fractional condensation, the
cycle gas and the high-boiling constituents being separated into
liquid fractions in a plurality of separators, the improvement
being dividing the liquid fraction of the first separator into a
fist and a second partial streams, the first stream forming one of
the refrigeration cycles, after being discharged from the first
separator the first stream being expanded to an intermediate
pressure which is a pressure greater than atmospheric and less than
that of the compressor, outlet after expansion the first stream
being utilized for cooling the mixture fed into the first
separator, and the first stream being fed back to the compressor;
the second stream from the first separator being deep-cooled and
expanded to about atmospheric pressure, the second stream then
being admixed with one of the other of the refrigeration cycles and
fed back to the compressor; and the condensates in the following
separators are subdivided into first and second portions in the
manner of the first separator, the respective first and second
streams of the following separators are processed in the same
manner as the first and second streams of the first separator until
finally the liquid of the last separator is cooled against itself
and expanded to about atmospheric pressure and is utilized for
cooling the gas to be liquefied and the other separated cycle gas
media and then is mixed with the second partial streams to form the
other of the circulation cycles which is fed back to the
compressor.
2. A process according to claim 1 wherein each first partial stream
is greater than its second partial stream.
3. A process according to claim 2, characterized in that from at
least one of the first partial streams formed from the liquid
fractions, a partial amount is branched off, deep-cooled, expanded,
and again admixed to the liquefied gas mixture.
4. A process according to claim 3, characterized in that the gas
mixture to be liquefied is natural gas and the cycle media consist
preponderantly of high-boiling hydrocarbons.
5. A process according to claim 4, whereby nitrogen is to be
removed from the natural gas, characterized in that the gaseous
fraction drawn off from the last separator after further cooling
and partial liquefaction is subjected to a predecomposition in an
additional separator for the purpose of nitrogen separation, and
before further cooling is expanded in the nitrogen column.
6. A process according to claim 5, characterized in that only two
refrigeration cycles are used with two appropriate separators.
7. A process according to claim 1, characterized in that the gas
mixture to be liquefied is natural gas and the cycle media consist
preponderantly of high-boiling hydrocarbons.
Description
BACKGROUND OF INVENTION
This invention relates to a liquefaction process for gas mixtures
by means of fractional condensation where the cycles are open and
the cycle media consist of constituents of the gas mixture to be
liquefied.
Liquefaction processes according to this principle are known.
French Pat. 1,302, 989, for example teaches a process wherein the
cycle media obtained by fractional condensation from natural gas to
be liquefied expanded to a common average pressure are mixed,
recompressed to the pressure of the natural gas streaming in to the
equipment, and are again admixed thereto. It is characteristic of
this process that the individual cycle media are expanded to the
common average pressure. The process requires an extensive
distribution of the heat exchanger. Consequently, there results a
complicated connection.
SUMMARY OF INVENTION
The object of the invention is to provide a liquefaction process of
the above type which in a simple connection is particularly
suitable even for small liquefaction capacities.
A process has now been found for the liquefaction of gas mixtures
by at least two open partial cycles with different boiling ranges
where the gas mixture which previously was mixed with the cycle
media and by means of which a compressor was brought to elevated
pressure, was subjected to a fractional condensation, where the
cycle media and the more difficulty boiling mixture constituents
precipitate as liquid fractions in separators. According to the
invention, the liquid fraction s of the first separator are
distributed into two partial streams of which the first, forming
the first partial cycle, after expansion to an average pressure,
gives off coolness from the cycle gas and gas mixture to be
liquefied to the mixture streaming to the first separator and again
conducts back to the compressor, the second one is deep-cooled,
expanded to about atmospheric pressure and is admixed to the last
cycle medium streaming back to the compressor. Furthermore, it is
proceeded correspondingly with the compressor of the following
separator, the expansion of the first partial streams occurring at
average pressure until finally the liquid precipitating in the last
separator, after cooling against itself and expansion to about
atmospheric pressure, cools the gas mixture to be liquefied and the
other separated cycle media and is again conducted to the
compressor.
The inventive process needs, independent of pressure, under which
the gas mixture is available, only one compressor. It also allows
with respect to small liquefaction capacities the introduction of
turbocompressors in a suitable work range. In this connection, the
connection is simple and the number of heat exchangers is small.
Further advantages can be seen from the embodiment of the
invention.
THE DRAWINGS
The invention is now explained in more detail by way of an example.
The example illustrated in the drawing shows the liquefaction of
natural gas according to the inventive process, where besides the
actual natural gas liquefaction there also occurs a nitrogen
separation.
DETAILED DESCRIPTION
From pipeline 1 is branched off a partial stream 2 of the natural
gas under pressure. It is this gas which is to be liquefied and
freed of nitrogen. In the purification equipment 3 the natural gas
is first prepurified and through conduit 4 reaches the
turbocompressor 5 wherein it is compressed to about 25--35 absolute
pressure together with the cycle gas fractions. In the
afterconnected water cooler 6 a part of the compressed mixture is
already liquefied through conduit 7 the mixture reaches heat
exchanger 8 where it is further liquefied and through conduit 9 it
reaches separator 10. In separator 10 there is the first
decomposition into a liquid and a gaseous fraction. The liquid
fraction contains above all the heavy hydrocarbons of ethyl hydride
which is drawn off through conduit 11 from separator 10 and
distributed into three partial streams. The largest stream is
expanded in valve 12 and vaporized under 5--10 absolute pressure in
heat exchanger 8. The cold from the largest stream cools the second
cycle and the natural gas to be liquefied. By way of conduit 13 it
returns in gas form into turbocompressor 5.
A second, smaller partial stream is conducted through conduit 14
into heat exhanger 16 where it is deep-cooled, subsequently
expanded in valve 15 and admixed to the low-pressure cycle
fraction. The third partial stream is very small and also flows
through conduit 14 into heat exchanger 16, where it then branches
off from the second partial stream and through conduit 17 reaches
in sequence into heat exchangers 18, 19, and 20 where it is deep-
cooled and finally admixed to the liquefied natural gas.
The top gas in separator 10 consists of nitrogen and light
hydrocarbons which flows through conduit 27 into heat exchanger 16
and from there into the second separator 21. In heat exchangers 16
it is cooled to the extent that in the subsequent phase separation
in the second separator 21 the gaseous fraction has about the same
composition as the fraction to be processed. The condensate
precipitating in the second separator 21 forms the cooling medium
of the second cycle. It is drawn off by way of conduit 22,
deep-cooled in heat exchangers 18 and 19, and expanded in valve 23
to about atmospheric pressure. Then it gives off the deep cold in
the heat exchangers 18 and 19 to the natural gas to be liquefied
and reaches then by way of heat exchangers 16 and 8 into
turbocompressor 5. Before heat exchanger 19 there is still admixed
to it the vaporization gas coming over conduit 24.
After the cycle fractions are separated, the top gas of the second
separator 21 again forms the natural gas to be liquefied. The top
gas can be liquefied in heat exchangers 18 and 19. However, if a
separation of the nitrogen is desired-- as assumed in this
example-- a predecomposition is required. For this purpose the top
gas is conducted through conduit 25 into heat exchanger 18 where it
is partially liquefied. Then the top gas reaches a third separator
26 where it is decomposed into a liquid fraction poor in nitrogen
and into a gaseous fraction rich in nitrogen, both of which are
expanded into the nitrogen column 30 through conduits 28 and 29 and
valves 31 and 32 after further cooling in heat exchanger 19. In the
nitrogen column occurs the decomposition into extensive
nitrogen-free natural gas in the column absorption layer and
nitrogen in the column top. The natural gas drawn off by way of
conduit 33 contains very little heavy hydrocarbons. These are
therefore, as described above, admixed to it through conduit 17
over expansion valve 35 from the condensate of the first separator
10. The nitrogen is drawn off at the top of column 30 through
conduit 34 and conducted through the the nitrogen deep cooler 36.
Its residual coolness is given off in sequence in heat exchangers
20, 19, 18, 16 and 8 and reaches with surrounding pressure and
temperature the plot limit.
The above example shows that the inventive liquefaction process
gets by with few subdivision of the heat exchanger; the connection
is therefore simple. Despite this, good efficiency is achieved.
Furthermore, only a compressor is necessary. Since it also
compresses the cycle fractions, even with small liquefaction
outputs turbocompressors can be set in without their having to be
operated in a disadvantageous work range.
The gas circulating in the cycles is formed from the natural gas
components automatically in the correct composition, so that no
special precautions for the starting and running ready-position of
the cycle gas are necessary.
The process can be expanded by one or more cycles. The cycle media
would then be expanded to pressures which are situated between the
pressure of conduit 13 and the atmospheric pressure. This
broadening decreases the energy requirement and is recommended for
liquefaction of gas mixtures with relatively many heavy
hydrocarbons.
* * * * *