U.S. patent number 3,735,601 [Application Number 05/160,024] was granted by the patent office on 1973-05-29 for low temperature refrigeration system.
Invention is credited to James H. Stannard, Jr..
United States Patent |
3,735,601 |
Stannard, Jr. |
May 29, 1973 |
LOW TEMPERATURE REFRIGERATION SYSTEM
Abstract
A refrigeration system in which a pressurized gas provides the
energy. The gas is expanded through an expansion engine and then
passed through a heat exchanger, wherein the refrigeration effect
resulting from its expansion is recovered. The expansion engine
operates a conventional closed loop refrigeration system which is,
in turn, cascaded through the low temperature gas discharging from
the expansion engine. Prior to being cooled by the low temperature
gas, the refrigeration cycle may also reject heat at a higher
temperature to any suitable cooling medium. The invention is
particularly suited for the liquefaction of natural gas or for low
temperature separation of gas constituents.
Inventors: |
Stannard, Jr.; James H. (San
Rafael, CA) |
Family
ID: |
22575163 |
Appl.
No.: |
05/160,024 |
Filed: |
July 16, 1971 |
Current U.S.
Class: |
62/87; 62/113;
62/175; 62/402; 62/513 |
Current CPC
Class: |
F25J
1/0052 (20130101); F25J 1/0204 (20130101); F25J
1/0281 (20130101); F25J 1/0037 (20130101); F25J
1/0097 (20130101); F25J 1/0232 (20130101); F25J
1/0208 (20130101); F25J 1/0022 (20130101); F25J
1/0085 (20130101); F25J 1/0288 (20130101); F25J
2270/06 (20130101); F25J 2210/06 (20130101); F25J
2205/60 (20130101) |
Current International
Class: |
F25J
1/00 (20060101); F25J 1/02 (20060101); F25b
009/00 () |
Field of
Search: |
;62/86,87,88,402,79,175,332,335,513,113 |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
|
|
|
|
|
|
|
249,486 |
|
Apr 1948 |
|
CH |
|
1,184,854 |
|
Mar 1970 |
|
GB |
|
913,405 |
|
Jun 1954 |
|
DT |
|
949,331 |
|
Feb 1949 |
|
FR |
|
Primary Examiner: Wye; William J.
Claims
What is claimed is:
1. A low temperature refrigeration method comprising the steps
of:
drawing off a processing stream of pressurized gas from a supply
source thereof,
expanding the stream through an expansion engine, then
passing the expanded stream through a first heat exchanger,
employing said expansion engine to drive a refrigeration system
compressor,
circulating a refrigerant in said system from said compressor
through said first heat exchanger to cool said refrigerant prior to
expansion and vaporization thereof,
conducting said refrigerant from said first heat exchanger,
expanding said refrigerant to at least partial vaporization,
then passing said refrigerant through a second heat exchanger,
drawing off a liquefaction stream of pressurized gas from a supply
source thereof, and
passing the pressurized gas successively through said first and
second heat exchangers to be cooled first by said expanded stream
and further by said expanded refrigerant.
2. The method defined by claim 1 wherein:
said liquefaction stream and said processing stream are drawn from
the same supply source.
3. The low temperature refrigeration method defined by claim 1
including the further steps of:
compressing the expanded processing stream to the level of said
supply source, and
then conducting said processing stream to said source.
4. The method of providing refrigeration defined by claim 1
wherein:
said processing stream is not cooled prior to expansion thereof
through said expansion engine.
5. The method defined by claim 1 wherein:
said refrigerant is precooled between said compressor means and
said first heat exchanger.
6. A refrigeration system comprising:
a source of pressurized gas,
a processing stream conduit connected to said source,
expansion engine means to which said processing stream conduit is
connected,
a first heat exchanger connected to the outlet of said expansion
engine means,
compressor means to which said expansion engine means are coupled
for driving said compressor means,
a closed refrigeration system including said compressor means, a
refrigerant circulated by said compressor means, and an expansion
means,
refrigerant conductor means circulating said refrigerant through
said first heat exchanger for cooling the liquid refrigerant prior
to said expansion means,
a liquefaction stream conduit connected to said source and
successively to said first and second heat exchangers.
7. The system defined by claim 6 including:
auxiliary heat sink means, and
conduit means connecting the outlet of said compressor means to
said heat sink means for initial cooling of said refrigerant.
Description
BACKGROUND OF THE INVENTION
This invention relates to a low temperature refrigeration method
and apparatus particularly adapted for liquefying natural gas or
the like.
There are a number of known processes for the production of very
low temperature (cryogenic) refrigeration. Most of such processes
rely upon the application of externally applied mechanical work to
drive conventional refrigeration equipment which may be cascaded
from one refrigeration cycle to the next to provide the very low
temperature which may be required to liquefy natural gas or to
accomplish other cryogenic tasks.
Several expansion cycles have been utilized for the lique-faction
of gases which utilize the potential energy of the feed gas as the
source of liquefaction refrigeration. While such expansion cycles
have been used successfully for the liquefaction of both
atmospheric gases, i.e., Helium, Nitrogen and Oxygen, and natural
gas, as well as the low temperature separation of natural gas
constituents, they have not fully utilized the potential energy
available in the expansion of a high pressure stream of gas.
In the natural gas industry, it is often necessary to expand large
volumes of natural gas from a high pressure to a low pressure to
enable its use. Several commercial installations have been
constructed to utilize the refrigeration available from this
expansion for the purpose of liquefying or separating the natural
gas constituents. However, such expander-cycle plants have had
limited application because of the relatively small amount of
refrigeration that they are capable of producing.
OBJECTS OF THE INVENTION
It is an object of this invention to provide an improved method and
apparatus which is commercially advantageous for the economic
production of large quantities of cryogenic refrigeration.
It is a further object of this invention to provide a highly
efficient method of liquefying natural gas, or the like.
It is a further object of this invention to provide a low
temperature refrigeration, utilizing a pressurized gas to drive a
refrigeration system which contributes to the cooling and
lique-faction of gas, and a means for the rejection of heat from
the liquefaction cycle.
It is still a further object of this invention to provide a low
temperature refrigeration system utilizing the refrigeration effect
produced by expanding a pressurized gas through an expansion
engine, which, in turn, drives a system producing additional
refrigeration, which may be cascaded from the already low
temperature produced by the expansion engine.
It is a further object of this invention to provide a system for
liquefying natural gas or the like wherein a portion of the gas is
expanded through an expansion engine, which, in turn, drives a
closed loop refrigeration cycle. Both the refrigeration effect
produced by the expanded gas and the refrigeration cycle are
employed to cool a liquefaction stream of the natural gas.
Other objects and advantages of this invention will become apparent
from the description to follow, particularly when read in
conjunction with the accompanying drawing.
BRIEF SUMMARY OF THE INVENTION
In the low temperature refrigeration system of this invention, a
source of gas under pressure is expanded through one or more
expansion engines, such as expansion turbines, wherein the
temperature of the gas is greatly reduced. The mechanical work of
the expansion engine is used to drive a closed loop refrigeration
cycle. After compression, the refrigerant is cooled initially to a
suitable heat sink, such as a cooling tower, and is further cooled
by passing it through a heat exchanger wherein the low temperature
expanded gas from the expansion engine is the cooling medium. After
expansion, the refrigerant is passed through a second heat
exchanger wherein it withdraws heat from another medium.
Where the refrigeration system of this invention is employed for
the liquefaction of natural gas or the like, the gas to be
liquefied is drawn from a pressurized source, and may be tapped
from the same supply of energy gas for the expansion engine. In any
event, the gas is passed through the two heat exchangers, whereby
it is cooled first by the expanded gas and then by the at least
partially vaporized refrigerant. In the meantime, the expanded
energy gas may be conducted from the system for commercial use, as
in a distribution system, or it may be compressed and recycled.
THE DRAWINGS
FIG. 1 is a schematic flow diagram of a gas liquefaction system
embodying features of this invention; and
FIG. 2 is a partial schematic flow diagram of another embodiment of
this invention.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
The Embodiment of FIG. 1
In the flow diagram of FIG. 1, a pressurized supply of gas is
provided at pipeline 10 from any suitable source (not shown). The
gas, for example, may comprise natural gas supplied directly from a
gas well or from a gas transmission pipeline. In any event, a
stream of the gas is drawn off at 12 as the energy source for the
refrigeration system of this invention.
After removal of water and other contaminents if required, for
example, with an adsorber 14, the gas is conducted through line 16
along a processing or expander stream E wherein it is employed to
provide the mechanical work necessary to operate a closed
refrigeration cycle R which is the principal component of this
refrigerating system. Specifically, the processing stream P is
conducted through conduit 16 to one or more turbines 18, 20 and 22
(T.sub.1, T.sub.2 and T.sub.3), three being shown for purposes of
illustration. The expander or processing stream E expands in the
expansion turbines 18, 20 and 22 to produce mechanical work, and
exhausts therefrom at E.sub.1 at a greatly reduced pressure and at
a substantially lower temperature. Because the gas conducted to the
turbines 18, 20 and 22 is at the relatively high temperature of the
pipeline gas 10, there is a concomitant high drop in enthalpy
through the turbine, which results in a correspondingly high output
of work.
The low temperature expanded processing stream E.sub.1 from the
final turbine stage is fed through conduit 24 to and through a heat
exchanger 26 for cooling of the liquid refrigerant stream, and the
medium to be refrigerated, as will be hereinafter described. From
the heat exchanger 26, the processing gas E.sub.1, which is now at
a commercially usable pressure, may be returned through line 28 to
pipeline 10 for transmission to a distributing system (not shown).
A pressure reducing regulator 30 enables some gas to be fed from
the pipeline 10 to augment that fed from the processing system
discharge line 28.
The turbines 18, 20 and 22 are mechanically coupled to compressors
32, 34 and 36 (C.sub.1, C.sub.2 and C.sub.3) which compress and
circulate a refrigerant through heat exchangers. More particularly,
in the refrigerating system R, a refrigerant, such as fluorinated
hydrocarbon or ethylene, is pumped from the first compressor 32 and
heat exchanger 38a, to the second compressor 34 and the heat
exchanger 38b, and then through compressor 36 and heat exchanger
38c. At the heat exchangers 38a, 38b and 38c, the heat resulting
from the compression of the refrigerant is dissipated to the
surrounding air, water, or other cooling medium, depending upon the
type heat exchanger used. From the heat exchanger 38c, the
refrigerant flows through a conduit 40 to the heat exchanger 26
where it gives up heat and is condensed. The thus cooled liquid
refrigerant emerges from the heat exchanger 26 and is then passed
through an expansion or throttle valve 42 whereupon the liquid
expands and returns to a mixed liquid-vapor state at a greatly
reduced temperature. The cold fluid is then conducted through heat
exchangers 46 and 26 where the sensible heat and latent heat of
vaporization of the refrigerant are withdrawn from a medium to be
cooled. In the heat exchanger 26, the vaporized refrigerant may
also help cool the oncoming liquid refrigerant flowing
therethrough. From the heat exchanger 26, the vaporized refrigerant
is returned to the compressor 32 through a conduit 48 to complete
the refrigeration cycle.
Where the refrigeration system of this invention is employed for
liquefaction of natural gas or for low temperature separation of
its constituents, the natural gas is delivered to the heat
exchangers 26 and 46 along a liquefaction path L which includes a
conduit 50 connected to the outlet of a conventional carbon dioxide
separator 52, if required. With carbon dioxide thus removed, the
liquefaction fluid L passes sequentially through the heat
exchangers 26 and 46 with negligible pressure loss, emerging from
the heat exchanger 46 in a pressurized, but low temperature
liquefied condition.
The cold, pressurized liquefaction fluid L from the heat exchanger
46 then flows through temperature controlled expansion valve 54,
which results in further cooling of the already cold fluid by
reason of the Joule-Kelvin (Joule-Thomson) effect. After expansion
through the valve 54, liquefaction is substantially complete, and
the fluid is conducted through line 56 to an insulated storage tank
58.
The refrigeration system of this invention may be employed to
liquefy a portion of the natural gas in pipeline 10. In such event,
a portion of the gas is drawn off at 60 from the line 16 and
directed through the liquefaction path just described. Thus, the
natural gas from the same source is diverted into two streams, an
expander or processing stream E and a liquefaction stream L, one to
provide the energy and the other to receive the refrigeration
affects.
Reviewing the cooling process, the liquefaction stream L is first
cooled at heat exchanger 26 by the second cooling pass of the
refrigerant stream R and by the cooled, expanded process stream
E.sub.1 from the expansion turbines 18, 20 and 22. The net effect
might be, for example, to cool the gas from about 70.degree.F. to,
say -110.degree.F. Also cooled at heat exchanger 20 is the
refrigerant which, as described, was precooled at the heat
exchangers 38a, 38b and 38c.
At the second heat exchanger 46, the gas is further cooled by the
first cooling pass of the refrigerant stream, wherein the result
could be to reduce the temperature of the liquefaction stream
further to about -200.degree.F. which, at its relatively high
pressure is sufficient to liquefy it. Then, after expansion through
the valve 54, the stream is cooled to about -260.degree.F. and
still liquefied. It is within the capability of those skilled in
the art to utilize the liquefied stream for further cooling if
desired, as by diverting some of the stream to return through the
heat exchanger as a flash sub-cooler, or by drawing off vaporized
fluid from the tank 58 for the same purpose.
In the refrigeration system, the process gas E may enter the system
at about 1000 p.s.i. and at about 70.degree.F. and be cooled by
expansion through the turbines 18, 20 and 22 to about
-114.degree.F. Then, after passing through the heat exchanger 26,
where it absorbs heat from the liquid refrigerant in line 40 and
from the liquefaction stream L in line 50, it is reheated to about
80.degree.F. and is at a pressure suitable for a distribution
system. In the meantime, the refrigerant is delivered to the
compressors 32, 34 and 36 at about atmospheric pressure and at
about 80.degree.F. in temperature. The pressure is progressively
increased through the compressors to about, say 200 p.s.i. Of
course, the temperature is also increased at each compressor, but
after each pass through the heat exchanger, it is returned to about
90.degree.F. This greatly reduces the work load imposed on the
expanded gas at the heat exchanger 26. There, the refrigerant is
further cooled to about -100.degree.F. and liquefied. At the
expansion valve, the temperature is further reduced to about
-200.degree.F. as it enters the heat exchanger in a liquid-vapor
state.
Thus, in this system, a pressurized gas is cooled by expansion to
function as a cooling medium and the mechanical work produced
during such expansion drives a closed loop refrigeration cycle as
the principal cooling source. Optionally, the same gas may be
directed in a separate path through heat exchangers to be cooled by
the two sources just recited.
THE EMBODIMENT OF FIG. 2
In the embodiment of FIG. 2, the expanded process stream E.sub.1 in
line 28 may be passed through a compressor 62 which may be driven
by an engine or motor 64. The compressed gas is then reintroduced
to input line 12 at the pressure therein to circulate back through
the processing stream E to the first turbine 18 and then continuing
as in the embodiment of FIG. 1.
While this invention has been described in detail in conjunction
with preferred embodiments thereof, it is obvious that various
changes and modifications may suggest themselves to those skilled
in the art without departing from the spirit and scope of the
invention as defined by the appended claims.
* * * * *