U.S. patent number 3,729,945 [Application Number 04/880,009] was granted by the patent office on 1973-05-01 for multi-component refrigerant for the liquefaction of natural gas.
Invention is credited to David T. Linnett.
United States Patent |
3,729,945 |
Linnett |
May 1, 1973 |
MULTI-COMPONENT REFRIGERANT FOR THE LIQUEFACTION OF NATURAL GAS
Abstract
The efficiency of mixed refrigerant gas liquefaction process,
for example liquefaction of natural gas using a refrigerant
consisting of components extracted from the natural gas, may be
improved by controlling the composition, and hence the
temperature/enthalpy profiles, of the refrigerant streams in each
heat exchange stage. Coarse control is effected by adding portions
of a refrigerant mixture extracted from the previous heat exchange
stage, and fine control is effected by adding pure liquefied
gases.
Inventors: |
Linnett; David T. (Hoddesdon,
EN) |
Family
ID: |
10477652 |
Appl.
No.: |
04/880,009 |
Filed: |
November 26, 1969 |
Foreign Application Priority Data
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|
|
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Nov 29, 1968 [GB] |
|
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56,830/68 |
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Current U.S.
Class: |
62/612 |
Current CPC
Class: |
F25J
3/0209 (20130101); F25J 1/004 (20130101); F25J
1/0045 (20130101); F25J 3/0257 (20130101); F25J
1/025 (20130101); F25J 1/0249 (20130101); F25J
1/0212 (20130101); F25J 1/0055 (20130101); F25J
1/0202 (20130101); F25J 1/0022 (20130101); F25J
1/0264 (20130101); F25J 3/0233 (20130101); F25J
2200/50 (20130101); F25J 2210/06 (20130101); F25J
2245/90 (20130101); F25J 2200/74 (20130101); F25J
2205/04 (20130101); F25J 2200/02 (20130101); F25J
2220/64 (20130101) |
Current International
Class: |
F25J
1/00 (20060101); F25J 3/02 (20060101); F25J
1/02 (20060101); F25j 001/00 (); F25j 005/00 ();
F25j 003/02 () |
Field of
Search: |
;62/9,23,24,26,27,28,29,40 |
References Cited
[Referenced By]
U.S. Patent Documents
Other References
Kleemenko, One Flow Cascade Cycle; Prog. in Refrig. Science and
Tech. Pergamon Press 1960 pp. 34- 39..
|
Primary Examiner: Yudkoff; Norman
Assistant Examiner: Purcell; Arthur F.
Claims
We claim:
1. A process for the liquefaction of a natural gas feedstock
including the steps of (1) passing said feedstock through a series
of at least two heat exchange stages operating at successively
lower temperatures, (2) circulating a compressed multicomponent
refrigerant in closed circuit and in indirect heat exchange
relation with said feedstock in each of said stages, (3)
compressing and partially condensing said refrigerant to obtain
separated first liquid and first vapor phases, (4) flowing said
first liquid phase cocurrently with said feedstock in said first
heat exchange stage, (5) separating said liquid phase into first
and second portions, (6) expanding said first portion for counter
current heat exchange with said feedstock, said first vapor phase
and said first separated liquid, (7) partially condensing and
flowing said first vapor phase through said first stage and
separating said partially condensed first vapor phase into second
liquid and vapor phases, (8) combining said second portion of said
first liquid phase with said second separated liquid phase to
define a second stream for cocurrent separate flow with said
feedstock and said second separated vapor phase in said second heat
exchange stage, (9) and separating said combined second stream into
first and second portions for similar manipulation as said first
and second portions of said first liquid stream.
2. A process according to claim 1, in which at least one
substantially pure liquefied gas is introduced into at least one of
the expanded portions of liquid refrigerant prior to its
introduction into a chosen heat exchange stage, whereby the
temperature-enthalpy profile of the chosen heat exchange stage is
improved.
3. A process according to claim 2, additionally comprising taking a
bleed from at least one of said refrigerant liquid portions and
then separating the bleed to form the substantially pure liquefied
gas.
4. A process according to claim 1, in which the partial
liquefaction producing the least volatile portion of refrigerant
liquid is performed by passing the compressed circulating
refrigerant mixture through a water cooler, and the other partial
liquefactions are performed by cooling in said heat exchange
stages.
5. A process according to claim 1, in which after the successive
partial liquefactions have been performed, the remainder of the
refrigerant mixture is expanded and used to cool any heat exchange
stage through which the expanded liquid portions have not been
passed.
6. A process according to claim 1, in which vaporized liquid
natural gas is passed through at least some of the heat exchange
stages.
7. A process according to claim 1 comprising removing low boiling
point products from the feedstock by expanding the feedstock into a
column and effecting fractional distillation therein between a
boiler and a condenser.
8. A process according to claim 7 comprising heating the reboiler
by passing the feedstock through the reboiler prior to its
expansion into the column.
9. A process according to claim 7 comprising cooling said condenser
with at least part of one of the portions of expanded refrigerating
liquid to be vaporized in a lower temperature heat exchange
stage.
10. A process according to claim 9 comprising adjusting the
composition of the portion of refrigerating liquid introduced into
said condenser by adding thereto portions of one or more
substantially pure gases.
Description
FIELD OF THE INVENTION
The invention relates to a gas liquefaction process employing a
refrigerant consisting of a mixture of gases of different boiling
points.
DESCRIPTION OF THE PRIOR ART
Known processes of this type employ a single multi-component
refrigerant sometimes consisting of components extracted from the
gas undergoing liquefaction. The composition of the refrigerant is
determined so that, in a series of fractional condensation steps,
the liquid separated in each heat exchange stage matches the
refrigeration requirement of the stage immediately following. The
thermodynamic efficiency of such processes is limited by the number
of heat exchange stages economically justifiable and the limited
flexibility in the composition of any single liquid fraction. This
latter feature is due to the interdependence of all the condensed
fractions each of which is a part of a single circulating
refrigerant.
SUMMARY OF THE INVENTION
According to the present invention there is provided a process for
the refrigeration of a fluid feedstock comprising passing the fluid
feedstock through a series of heat exchange stages operating at
successively lower temperatures, cooling at least two of the heat
exchange stages with portions of expanded refrigerating liquid in
course of vaporization, each portion of refrigerating liquid
resulting from partial liquefaction of a compressed gaseous mixture
in a higher temperature heat exchange stage, and adjusting the
composition of at least one of said portions of refrigerating
liquid by addition thereto of portions of liquefied gas.
The present invention also provides a process for refrigerating a
fluid feedstock wherein said fluid feedstock is a gaseous mixture
and comprising compressing said fluid feedstock to form said
compressed gaseous mixture.
Preferably the process also comprises recompressing at least some
of the vapors produced by vaporization of said portions of
refrigerating liquid and continuously replacing at least some of
said compressed gaseous mixture with said compressed vapors.
The portions of liquefied gas may be portions of liquefied gaseous
mixtures, in which case each portion of liquefied gaseous mixture
may be obtained from the portion of refrigerating liquid to be
vaporized in a higher temperature heat exchange stage.
Alternatively the portions of liquefied gas may be portions of one
or more substantially pure liquefied gases.
Low boiling point components may be removed from the feedstock by
expanding it into a column and effecting fractional distillation
therein between a reboiler and a condenser. The reboiler may be
heated by passing the feedstock through the reboiler prior to its
expansion into the column. The condenser may be cooled by part of a
portion of expanded refrigerating liquid to be vaporized in a lower
temperature heat exchange stage. The composition of the portion of
refrigerating liquid introduced into said condenser may be adjusted
by adding thereto portions of one or more substantially pure
gases.
A bleed may be withdrawn from one or more of said portions of
refrigerating liquid to maintain the overall composition of the
compressed gaseous mixture.
The invention will be further described, by way of example, and
with reference to the accompanying drawings in which
FIGS. 1, 2 and 3 are diagrams of three different process for the
liquefaction of natural gas.
In the liquefaction process illustrated in FIG. 1 the natural gas
is cooled in a heat exchanger 4, cooled and partially condensed in
a heat exchanger 6 and separated into liquid and vapor fractions in
a separator 12. The vapor fraction withdrawn from the separator 12
is condensed by passage through a heat exchanger 8 and sub-cooled
by passage through heat exchangers 10 and 11 to a temperature such
that there is a minimum flash on expansion through an expansion
valve 18 to the storage pressure. The liquid fraction withdrawn
from the separator 12 is separated in a column system (not shown)
into its components for mixed refrigerant make-up purposes.
Refrigeration is provided by a mixed refrigerant comprising
hydrocarbons extracted from the natural gas undergoing liquefaction
and added nitrogen. The mixed refrigerant is compressed in a
compressor 15, cooled in a cooler 16 and separated in a separator
17. The vapor fraction withdrawn from the separator 17 is cooled
and partially condensed by passage through the heat exchanger 4 and
then passed to a separator 5. The vapor fraction withdrawn from the
separator 5 is cooled and partially condensed by passage through
the heat exchanger 6 and then passed to a separator 7. The vapor
fraction withdrawn from the separator 7 is cooled and partially
condensed by passage through the heat exchanger 8 and then passed
to a separator 9. The vapor fraction withdrawn from the separator 9
is condensed in the heat exchanger 10, sub-cooled in the heat
exchanger 11, expanded through an expansion vlave 20 and returned
through the heat exchangers 11, 10, 8, 6 and 4 to provide
cooling.
The liquid fraction withdrawn from the separator 9 is sub-cooled in
the heat exchanger 10, expanded through an expansion valve 21, and
vaporized in the heat exchanger 10. The liquid fraction withdrawn
from the separator 7 is sub-cooled in the heat exchanger 8,
expanded through an expansion valve 23 and vaporized in the heat
exchanger 8. The liquid fraction withdrawn from the separator 5 is
sub-cooled in the heat exchanger 6, expanded through an expansion
valve 24 and vaporized in the heat exchanger 6. The liquid fraction
withdrawn from the separator 17 is sub-cooled in the heat exchanger
4, expanded through an expansion valve 13 and vaporized in the heat
exchanger 4.
In each case the vapor fractions resulting from the vaporization of
the expanded refrigerating liquid in the heat exchangers 4, 6, 8
and 10 is returned to the compressor 15.
The overall efficiency of the basic cycle described above is, in
accordance with the invention, improved by adjusting the
compositions of the individual condensed fractions to obtain better
matching of the temperature/enthalpy profiles of the heat
exchangers.
A coarse adjustment of the temperature/enthalpy profiles in the
heat exchangers 4, 6, 8 and 10 is effected by withdrawing
controlled amounts of refrigerant by way of flow lines 26, 27 and
28 and adding them to the refrigerant in flow lines 29, 30 and 31
respectively. In each case the quantity of liquid refrigerant added
is individually controlled to provide optimum conditions in the
heat exchanger in which the liquid is ultimately vaporized. Fine
control of the temperature/enthalpy profiles in the heat exchangers
may be obtained by introducing one or more substantially pure
components preferably at a point just before the refrigerant enters
a particular heat exchanger. In this process controlled amounts of
substantially pure components are introduced via lines 32 and 33
into the refrigerant just before it enters the heat exchanger 8. It
will be appreciated that fine control of the temperature/enthalpy
profile of any heat exchanger employed in the system may be carried
out by introducing controlled amounts of substantially pure
components just before the expanded refrigerant is fed into that
particular heat exchanger.
In order to provide substantially pure components for fine control
of the expanded refrigerant fractions whilst maintaining the
overall composition of the refrigerant substantially constant, a
bleed is taken from one or more of the separated condensed liquids
via flow lines 40, 41 and 42, passed to a column separation system
(not shown) in which it is separated into the required
substantially pure components, excess quantities of these
components being returned to the refrigerant via the normal make-up
system.
In the gas liquefaction process illustrated in FIG. 2 the natural
gas feedstock is introduced by way of flow line 51 and partially
liquefied by passing it successively through heat exchanger 52 and
53. The condensate withdrawn from the heat exchanger 53 is
separated in a separator 54 and the liquid fraction withdrawn
therefrom separated in a column separation system (not shown) into
its pure components for use for mixed refrigerant make-up
purposes.
The vapor fraction withdrawn from the separator 54 is partially
liquefied in a heat exchange 55 and passed through the reboiler 56
of a degasification column 57 to provide re-boil therefor. It is
then passed through a heat exchanger 58, expanded by passage
through an expansion valve 59 and fed to the degasification column
57. In the column 57 the partially expanded mixture is separated
between the reboiler 56 and a condenser 60 to provide most of the
hydrocarbons at the bottom of the column 57 and nitrogen with some
lighter hydrocarbons at the top. The hydrocarbon liquid withdrawn
from the bottom of the column 57 is passed successively through a
series of heat exchangers 58, 61, and 62 where it is cooled in such
a way that there is a minimum flash as it is expanded through an
expansion valve 63 to the storage pressure. The nitrogen-rich vapor
fraction withdrawn from the top of the degasification column 57 is
cooled by passage through the heat exchangers 61 and 62, expanded
through an expansion valve 64 and then passed successively through
the heat exchangers 62, 61, 65, 53 and 52 to provide cooling. The
product withdrawn from the heat exchanger 52 is suitable for use as
a fuel gas.
The mixed refrigerant is compressed in a compressor 70, partially
liquefied in a cooler 71 and then passed into a separator 72. The
vapor fraction withdrawn from the separator 72 is partially
liquefied in the heat exchanger 52 and then fed into a separator
73. The liquid fraction from the separator 72 is passed through the
heat exchanger 52, expanded by passage through an expansion valve
74 and then passed by way of a refrigerant return line 68 through
the heat exchanger 52 where it vaporizes and provides cooling. The
vapor fraction discharged from the heat exchanger 52 by way of the
refrigerant return line 68 is returned to the compressor 70.
The vapor fraction withdrawn from the separator 73 is partially
liquefied in the heat exchanger 53 and then passed to a separator
59. The liquid fraction withdrawn from the separator 73 is passed
through the heat exchanger 53, expanded through an expansion valve
75 and then returned by way of a flow line 50 to the heat exchanger
53 where it vaporizes and provides cooling. The vapor fraction is
withdrawn from the heat exchanger 53 by way of a flow line 69 and
passed to the refrigerant return line 68 at a point in advance of
the heat exchanger 52.
The vapor fraction withdrawn from the separator 59 is partially
liquefied in the heat exchanger 65 and passed to a separator 76.
The liquid fraction from the separator 59 is passed through the
heat exchanger 65 after which it divides into two parts, one of
which is expanded by passage through an expansion valve 77 while
the other is expanded by passage through an expansion valve 78. The
expanded refrigerant from the valve 77 is returned by way of a
refrigerant return line 81 to the heat exchanger 65 to provide
cooling and the expanded refrigerant from the valve 78 passed
through the heat exchanger 55 where it vaporizes and provides
cooling. The vapors withdrawn from the heat exchangers 65 and 55
are fed by way of a flow line 79 into the flow line 50 where they
join the refrigerant from the expansion valve 75 prior to being fed
into the heat exchanger 53.
The vapor fraction from the separation 76 is cooled by passing it
successively through the heat exchangers 61 and 62 and then
expanded by passage through an expansion valve 80. The expanded
refrigerant is then returned through the heat exchangers 62 and 61
to join the refrigerant return line 81 at a point in advance of the
heat exchanger 65.
The liquid fraction from the separator 76 is cooled by passage
through the heat exchanger 61 after which part is expanded by
passage through an expansion valve 88 while the other part is
expanded by passage through an expansion valve 87. The expanded
refrigerant from the expansion valve 88 is fed into a refrigerant
return line 83 while the other part from the expansion valve 87 is
fed into the condenser 60 of the degasification column 57 where it
vaporizes and provides cooling. The refrigerant withdrawn from the
condenser 60 is passed through the heat exchanger 58 and fed into
the refrigerant return line 83.
The overall efficiency of the basic cycle described above is
improved by adjusting the compositions of the individual condensed
fractions to obtain better matching of the temperature/enthalpy
profiles of the heat exchangers. A coarse adjustment of the
temperature/enthalpy profiles in the heat exchangers 53, 55, 65 and
61 is effected by withdrawing controlled amounts of refrigerant by
way of flow lines 93, 94 and 95 and adding them to the refrigerant
in flow lines 91, 92 and 90 respectively. In each case the quantity
of liquid refrigerant added is individually controlled to provide
optimum conditions in the heat exchanger in which the liquid is
ultimately evaporated.
Fine control of the temperature/enthalpy profiles in the heat
exchangers may be obtained by introducing one or more substantially
pure components at a joint just before the expanded refrigerant
enters a particular heat exchanger. Controlled amounts of
substantially pure components are introduced via lines 97 and 98
into line 81 just before the refrigerant enters the heat exchanger
65. Similarly, substantially pure components are introduced by way
of lines 106 and 99 to control the temperature/enthalpy profile in
the condenser 60 and into lines 82 and 89 to control the
temperature/enthalpy profile in the heat exchanger 55. It will be
appreciated that fine control of the temperature/enthalpy profile
of any heat exchanger employed in the system may be carried out by
introducing controlled amounts of substantially pure components
just before the expanded refrigerant is fed into that particular
heat exchanger.
In order to provide the substantially pure components for fine
control of the expanded refrigerant fractions whilst maintaining
the overall composition of the refrigerant substantially constant,
a bleed is taken from one or more of the separated condensed
liquids via lines 103, 104 and 105, passed to a column separation
system in which it is separated into the required substantially
pure components, excess quantities of these components being
returned to the refrigerant via the normal make-up system.
Boil-off gas emerging from the storage tank is cold and its
refrigeration may be utilized by passing it through the heat
exchangers 65, 53 and 52.
In the gas liquefaction process illustrated in FIG. 3 the natural
gas feed stock is introduced by way of flow line 111 and is joined
by the vapor refrigerant leaving separator 153. The natural gas
refrigerant mixture is partially liquefied by passing it through
the heat exchanger 112 after which it is transferred to the
separator 113. The vapor fraction from the separator 113 is
partially liquefied by passage through the heat exchanger 114 and
then transferred to the separator 115. The liquid fraction from the
separator 113 is passed through the heat exchanger 114, expanded by
passage through an expansion valve 116 and then returned to the
heat exchanger 114 to provide cooling. The vapor fraction leaving
the heat exchanger 114 is fed into the refrigerant return line 117
at a point in advance of the heat exchanger 112.
The vapor fraction from the separator 115 is divided into two parts
one of which is partially liquefied in a heat exchanger 118 and
then passed to a separator 119 while the other is partially
liquefied by passage through a heat exchanger 120 and then passed
to the reboiler 121 of a column 122. The partially liquefied
gaseous mixture provides heat for the reboiler 121 and is then
passed through a heat exchanger 123, expanded by passage through an
expansion valve 124 and passed to the column 122 where it is
separated between the reboiler 121 and a condenser 125.
The liquid fraction from the separator 115 is passed through the
heat exchanger 118 after which it divides into two parts, one of
which is expanded by passage through an expansion valve 126 and the
other by passage through an expansion valve 127. The expanded
liquid emerging from expansion valve 126 is passed through the heat
exchanger 118 where it provides cooling and the expanded liquid
from the expansion valve 127 is fed to the heat exchanger 120 to
provide cooling. The vapor fractions leaving the heat exchangers
118 and 120 are combined and passed by way of flow line 129 into a
flow line 110 where they join the refrigerant from expansion valve
116 prior to being fed into the heat exchanger 114.
The vapor fraction from the separator 119 is fed into the column
122 by way of flow line 179 and is separated in the column 122
together with the expanded mixture entering the column 122 after
expansion through valve 124. The vapor fraction comprising nitrogen
and some lighter hydrocarbons withdrawn from the top of the column
122 is fed by way of a flow line 130 successively through the heat
exchangers 131 and 132 in which it is liquefied and subcooled,
expanded by passage through an expansion valve 133 and then
returned through the heat exchangers 132, 131, 118, 114 and 112 to
provide cooling. The expanded nitrogen rich fraction emerging from
the heat exchanger 112 may be used as a fuel gas.
The liquid hydrocarbon fraction from the bottom of the column 122
is passed successively through a series of heat exchangers 123,
131, and 132 where it is cooled in such a way that there is a
minimum flash on expansion through an expansion valve 140 to the
storage pressure.
The liquid fraction withdrawn from the separator 119 is cooled by
passage through the heat exchanger 131 and then divided into two
parts. One part is expanded by passage through an expansion valve
141 and returned through the heat exchanger 131 to provide cooling
therefor, while the other part is expanded by passage through
expansion valve 142 and then used to provide cooling for the
condenser 125 of the column 122. The vapor leaving the condenser
125 is passed through the heat exchanger 123 and first combined
with the part emerging from the heat exchanger 131 after which they
join the liquid fraction emerging from the expansion valve 126.
Vapor returning by way of flow line 117 is recompressed in a
compressor 150, partially liquefied by passage through a cooler 151
and then fed to a separator 153. The vapor product leaving the
separator 153 rejoins the gaseous mixture in the flow line 111. The
liquid product withdrawn from the separator 153 is fed through the
heat exchanger 112, expanded by passage through the expansion valve
154 and then returned through the heat exchanger 112 to provide
cooling.
The overall efficiency of the basic cycle described above is
improved by adjusting the compositions of the individual condensed
fractions to obtain better matching of the temperature/enthalpy
profiles of the heat exchangers. A coarse adjustment of the
temperature/enthalpy profiles in the heat exchangers 114, 118, 120
and 131 is effected by withdrawing controlled amounts of
refrigerant by way of flow lines 170, 171 and 172 and adding them
to the refrigerant in flow lines 161, 162 and 174 respectively. In
each case the quantity of liquid refrigerant added is individually
controlled to provide optimum conditions in the heat exchanger in
which the liquid refrigerant is ultimately evaporated.
Fine control of the temperature/enthalpy profiles in the heat
exchangers may be obtained by introducing controlled quantities of
one or more substantially pure components at a point just before
the expanded refrigerant enters a particular heat exchanger.
Controlled amounts of substantially pure components are introduced
via lines 180 and 181 just before the expanded refrigerant enters
the heat exchanger 118. Similarly, substnatially pure components
are introduced by way of lines 182 and 183 to control the
temperature/enthalpy profiles in the condenser 125 and into lines
184 and 185 to control the temperature/enthalpy profiles in the
heat exchanger 120. It will be appreciated that fine control of the
temperature/enthalpy profile of any heat exchanger employed in the
system may be carried out by introducing controlled amounts of
substantially pure components just before the refrigerant is fed
into that particular heat exchanger.
In order to provide the substantially pure components for fine
control of the expanded refrigerant fractions whilst maintaining
the overall composition of the refrigerant substantially constant,
a bleed is taken from one or more of the separated condensed
liquids via lines 190, 191 and 192, passed to a column separation
system in which it is separated into the required substantially
pure components, excess quantities of these components being
returned to the refrigerant via the normal make-up system.
Boil-off gas emerging from the storage tank is cold and its
refrigeration may be utilized by passing it through the heat
exchangers 118, 114 and 112. The invention is not restricted to the
details of the foregoing examples.
* * * * *