AU2018264606B2 - Natural gas liquefaction apparatus - Google Patents
Natural gas liquefaction apparatus Download PDFInfo
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- AU2018264606B2 AU2018264606B2 AU2018264606A AU2018264606A AU2018264606B2 AU 2018264606 B2 AU2018264606 B2 AU 2018264606B2 AU 2018264606 A AU2018264606 A AU 2018264606A AU 2018264606 A AU2018264606 A AU 2018264606A AU 2018264606 B2 AU2018264606 B2 AU 2018264606B2
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- refrigerant
- heat exchanger
- flow
- cryogenic heat
- natural gas
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 239000003345 natural gas Substances 0.000 title claims abstract description 59
- 239000003507 refrigerant Substances 0.000 claims abstract description 344
- 230000006835 compression Effects 0.000 claims description 73
- 238000007906 compression Methods 0.000 claims description 73
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- 239000003949 liquefied natural gas Substances 0.000 claims description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 238000000034 method Methods 0.000 description 29
- 239000002131 composite material Substances 0.000 description 27
- 238000001816 cooling Methods 0.000 description 15
- 239000012530 fluid Substances 0.000 description 12
- 101000841267 Homo sapiens Long chain 3-hydroxyacyl-CoA dehydrogenase Proteins 0.000 description 3
- 102100029107 Long chain 3-hydroxyacyl-CoA dehydrogenase Human genes 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- JJYKJUXBWFATTE-UHFFFAOYSA-N mosher's acid Chemical compound COC(C(O)=O)(C(F)(F)F)C1=CC=CC=C1 JJYKJUXBWFATTE-UHFFFAOYSA-N 0.000 description 3
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 2
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000001151 other effect Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0082—Methane
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0205—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a dual level SCR refrigeration cascade
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0294—Multiple compressor casings/strings in parallel, e.g. split arrangement
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A natural gas liquefaction apparatus according to the present invention comprises: a cryogenic heat exchanger in which a natural gas is liquefied into LNG by exchanging heat with a first and a second refrigerant while the natural gas passes through the cryogenic heat exchanger; a first refrigerant cycle which allows the first refrigerant to circulate therethrough, includes a partial flow channel passing through the cryogenic heat exchanger for heat exchange, and includes multiple divided flow channels in which the first refrigerant expands and is pre-compressed after exchanging heat in the cryogenic heat exchanger; and a second refrigerant cycle which allows the second refrigerant to circulate therethrough and includes a partial flow channel passing through the cryogenic heat exchanger.
Description
[0001] The present disclosure relates to a natural gas liquefaction apparatus, and more
particularly, to a natural gas liquefaction apparatus for liquefying natural gas through a
plurality of cycles using different refrigerants.
[0002] In general, natural gas is transported in a gas state through land or marine gas
piping, or is stored in an LNG transport ship in a state of liquefied natural gas (LNG) and
transported.
[0003] At this point, natural gas is obtained by being cooled to an ultra low
temperature and has a volume reduced to about 1/600 of that of gas-state natural gas, and is
therefore very suitable for long distance marine transportation.
[0004] In addition, conventionally used liquefaction methods for natural gas have been
performed by allowing the natural gas to pass through one or more heat exchangers so as to
be cooled.
[0005] U.S. Patent Publication No. 2014-0245780 discloses a technology using
mutually independent heat exchange cycles so that two different refrigerants circulate
therethrough.
[0006] However, the technology disclosed in the patent has a limitation in that it is
difficult to adjust process variables because cycles are each configured in series in its entirety, and the limitation greatly decreases process efficiency.
[0007] Consequently, methods and systems for addressing one or more of the above
limitations is described.
[0008] The present disclosure is devised to address or ameliorate one or more of the
abovementioned or other limitations of conventional art, and may provide improvements or
alternatives for providing a natural gas liquefaction apparatus which facilitates the
adjustment of process variables and is capable of maximizing heat exchange efficiency.
[0009] Any discussion of documents, acts, materials, devices, articles or the like
which has been included in the present specification is not to be taken as an admission that
any or all of these matters form part of the prior art base or were common general
knowledge in the field relevant to the present disclosure as it existed before the priority
date of each of the appended claims.
[0009a] Throughout this specification the word "comprise", or variations such as
"comprises" or "comprising", will be understood to imply the inclusion of a stated element,
integer or step, or group of elements, integers or steps, but not the exclusion of any other
element, integer or step, or group of elements, integers or steps.
[0009b] Some embodiments relate to a natural gas liquefaction apparatus comprising: a
cryogenic heat exchanger through which natural gas passes and is liquefied into liquefied
natural gas through heat exchange with a first refrigerant and a second refrigerant; a first
refrigerant cycle through which the first refrigerant circulates and which comprises a path
for the first refrigerant divided into a plurality of paths at the cryogenic heat exchanger;
and a second refrigerant cycle through which the second refrigerant circulates and which comprises a path for the second refrigerant passing though the cryogenic heat exchanger, wherein the first refrigerant cycle further comprises: a first refrigerant first compression part provided upstream of the cryogenic heat exchanger and configured to compress the first refrigerant to a high pressure, the first refrigerant compressed at the first refrigerant first compression part being divided into a first flow and a second flow of the first refrigerant through two respective paths at the cryogenic heat exchanger; a first refrigerant first turbo expander comprising a first refrigerant first expansion part provided downstream of the cryogenic heat exchanger and configured to expand the first flow of the first refrigerant having passed through the cryogenic heat exchanger, and a first refrigerant first pre-compression part configured to pre-compress the first refrigerant which has been expanded by the first refrigerant first expansion part and has passed through the cryogenic heat exchanger again; a first refrigerant second turbo expander, comprising a first refrigerant second expansion part provided downstream of the cryogenic heat exchanger and configured to expand the second flow of the first refrigerant having passed through the cryogenic heat exchanger, and a first refrigerant second pre-compression part configured to pre-compress the first refrigerant which has been expanded by the first refrigerant second expansion part and has passed through the cryogenic heat exchanger again; and a mixing pipe for mixing the first flow of the first refrigerant pre-compressed by the first refrigerant first pre-compression part and the second flow of the first refrigerant pre-compressed by the first refrigerant second pre-compression part, the mixed first and second flows of the first refrigerant in the mixing pipe flowing into the first refrigerant first compression part.
[0010] Some embodiments relate to a natural gas liquefaction apparatuses according to
the present disclosure, including: a cryogenic heat exchanger through which natural gas
passes through and is liquefied into LNG through heat exchange with a first refrigerant and a second refrigerant; a first refrigerant cycle through which the first refrigerant circulates, which has some paths passing through the cryogenic heat exchanger to perform heat exchange, and which has a path of the first refrigerant divided into a plurality of paths after performing heat exchange at the cryogenic heat exchanger and performs expansion and pre-compression of the first refrigerant; and a second refrigerant cycle through which the second refrigerant circulates and which has some paths passing though the cryogenic heat exchanger.
[0011] The first refrigerant cycle may include: a first refrigerant first compression part
provided upstream of the cryogenic heat exchanger and configured to compress the first
refrigerant to a high pressure; a first refrigerant first turbo expander including a first
refrigerant first expansion part provided downstream of the cryogenic heat exchanger and
configured to expand the first flow among the two divided flows of the first refrigerant
having passed through the cryogenic heat exchanger, and a first refrigerant first pre
compression part configured to pre-compress the first refrigerant which has been expanded
by the first refrigerant first expansion part and have passed through the cryogenic heat
exchanger again; and a first refrigerant second turbo expander including a first refrigerant
second expansion part provided downstream of the cryogenic heat exchanger and
configured to expand the second flow among the two divided flows of the first refrigerant
having passed through the cryogenic heat exchanger, and a first refrigerant second pre
compression part configured to pre-compress the first refrigerant which has been expanded
by the first refrigerant second expansion part and have passed through the cryogenic heat
exchanger again.
[0012] In addition, the first refrigerant cycle may include: a first refrigerant first
compression part provided upstream of the cryogenic heat exchanger and configured to compress the first refrigerant to a high pressure; a first refrigerant first turbo expander including a first refrigerant first expansion part provided downstream of the cryogenic heat exchanger and configured to expand the first flow among the three divided flows of the first refrigerant having passed through the cryogenic heat exchanger, and a first refrigerant first pre-compression part configured to pre-compress the first refrigerant which has been expanded by the first refrigerant first expansion part and has passed through the cryogenic heat exchanger again; a first refrigerant second turbo expander including a first refrigerant second expansion part provided downstream of the cryogenic heat exchanger and configured to expand the second flow among the three divided flows of the first refrigerant having passed through the cryogenic heat exchanger, and a first refrigerant second pre compression part configured to pre-compress the first refrigerant which has been expanded by the first refrigerant second expansion part and has passed through the cryogenic heat exchanger again; and a first refrigerant third turbo expander including a first refrigerant third expansion part provided downstream of the cryogenic heat exchanger and configured to expand the third flow among the three divided flows of the first refrigerant having passed through the cryogenic heat exchanger, and a first refrigerant third pre-compression part configured to pre-compress the first refrigerant which has been expanded by the first refrigerant third expansion part and has passed through the cryogenic heat exchanger again.
[0013] In addition, the first refrigerant first compression part may be provided in
plurality.
[0014] In addition, the second refrigerant cycle may include a second refrigerant
compression part provided upstream of the cryogenic heat exchanger and configured to
compress the second refrigerant to a high pressure; and a second refrigerant turbo expander
including a second refrigerant expansion part provided downstream of the cryogenic heat exchanger and configured to expand the second refrigerant having passed through the cryogenic heat exchanger, and a second refrigerant pre-compression part configured to pre compress the second refrigerant which has been expanded by the second refrigerant expansion part and has passed through the cryogenic heat exchanger again.
[0015] The natural gas liquefaction apparatus of the present disclosure for addressing
the abovementioned limitation has the following effects.
[0016] First, there is a merit in that a portion of the first refrigerant cycle divides the
flow of the first refrigerant so that expansion and pre-compression for each flow of the first
refrigerant may be separately performed, and thus process variables are easily adjusted.
[0017] Secondly, there is a merit in that due to excellent heat exchange efficiency, the
yield can be increased and energy may be saved.
[0018] Thirdly, there is a merit in that the flow rate of the second refrigerant can be
reduced compared to that in conventional arts.
6a
[0019] Effects to be obtained by the present embodiments are not limited to the
aforesaid, but other effects not described herein will be clearly understood by those skilled
in the art from descriptions below.
[0020] FIG.1 is a view illustrating the configuration of a natural gas liquefaction
apparatus according to some embodiments.
[0021] FIG. 2 is a graph illustrating a composite curve of a conventional natural gas
liquefaction apparatus.
[0022] FIG 3 is a view illustrating a composite curve of a natural gas liquefaction
apparatus according to some embodiments.
[0023] FIG 4 is a view illustrating the configuration of a natural gas liquefaction
apparatus according to a further embodiment.
[0024] Hereinafter, the embodiments may specifically be achieved will be described
with reference to the accompanying drawings. In describing the embodiments, like
names and reference symbols are used for the same elements, and the additional
description thereon will not be provided.
[0025] FIG1 is a view illustrating the configuration of a natural gas liquefaction
apparatus according to some embodiments.
[0026] As illustrated in FIG1, a natural gas liquefaction apparatus according some
embodiments includes an ultra low temperature heat exchange 10, a first refrigerant cycle
100, and a second refrigerant cycle 200.
6b
[0027] The cryogenic heat exchanger 10 allows natural gas passing therethrough to be
liquefied into LNG by the heat exchange with the first refrigerant circulating in first
refrigerant cycle 100 and the second refrigerant cycle 200 circulating in the second
refrigerant cycle 200.
[0028] At this point, in case of the present embodiment, methane serves as the first
refrigerant and nitrogen serves as the second refrigerant. However, embodiments are not
limited to the present embodiment, other refrigerants may of course be used as the first and
second refrigerants.
[0029] In addition, as described above, the first refrigerant circulates through the first
refrigerant cycle 100, some paths of which perform heat exchange via the cryogenic heat
exchanger 10.
[0030] At this point, after performing the heat exchange at the cryogenic heat
exchanger 10, the path of the first refrigerant cycle 100 is divided into a plurality of paths
so that expansion and pre-compression of the first refrigerant may be performed. That is,
the first refrigerant cycle 100 has a parallel structure because the path of the first refrigerant is divided after passing through the cryogenic heat exchanger 10.
[0031] In particular, in the present embodiment, the first refrigerant cycle 100 includes
a first refrigerant compression part 110, a first turbo expander 120, and a second turbo
expander 130.
[0032] The first refrigerant first compression part 110 is provided upstream of the
cryogenic heat exchanger 10 in the entire first refrigerant cycle 100, and compresses the
first refrigerant to a high pressure (for example, about 50-60 barg). In case of the present
embodiment, the first refrigerant first compression part 110 is provided as a plurality of
compression parts 111 and 112.
[0033] In addition, the first turbo expander 120 includes a first refrigerant first
expansion part 121 and a first refrigerant first pre-compression part 122.
[0034] The first refrigerant first expansion part 121 is provided downstream of the
cryogenic heat exchanger 10 in the entire first refrigerant cycle 100, and expands a first
flow which is a portion of the two divided flows of the first refrigerant after passing
through the cryogenic heat exchanger 10.
[0035] By means of the first expansion part 121, the first flow of the first refrigerant
may be expanded to, for example, about 10-12 barg. The expanded first flow of the first
refrigerant may be cooled to, for example, about -55°C to about -75°C. The expanded and
cooled first flow of the first refrigerant by the first refrigerant first expansion part 121
circulates to the cryogenic heat exchanger 10 side to perform heat exchange.
[0036] The first flow of the first refrigerant flowing into the cryogenic heat exchanger
from the first refrigerant first expansion part 121 may be configured to pass through a
warm heat exchange region 16 (upstream region of inner region of the heat exchanger 10
with respect to the flow of natural gas) inside the cryogenic heat exchanger 10.
[0037] The first refrigerant first pre-compression part 122 is also provided
downstream of the cryogenic heat exchanger 10 in the entire first refrigerant cycle 100.
The first refrigerant first pre-compression part 122 and the first refrigerant first expansion
part 121 may operate linked with each other.
[0038] The first refrigerant first pre-compression part 122 pre-compresses, for
example to about 20-25 barg, the first flow of the first refrigerant, which have been
expanded by the first refrigerant first expansion part 121 and have passed through the
cryogenic heat exchanger 10 again, and then supplies the first flow to the first refrigerant
first compression part 110 described above.
[0039] In addition, the second turbo expander 130 includes a first refrigerant second
expansion part 131 and a first refrigerant second pre-compression part 132.
[0040] The first refrigerant second expansion part 131 is provided downstream of the
cryogenic heat exchanger 10 in the entire first refrigerant cycle 100, and expands a second
flow which is a portion of the two divided flows of the first refrigerant after passing
through the cryogenic heat exchanger 10.
[0041] The first refrigerant first expansion part 121 and the first refrigerant second
expansion part 131 are configured to sequentially receive the first flow and the second flow,
which flow into the cryogenic heat exchanger 10 via the same refrigerant line from the first
refrigerant first compression part 110 and which are heat-exchanged inside the cryogenic
heat exchanger 10.
[0042] By means of the second expansion part 131, the second flow of the first
refrigerant may be expanded to, for example, about 15-20 barg. The expanded second
flow of the first refrigerant may be cooled to, for example, about -90°C to about -115°C.
The second flow of the first refrigerant expanded and cooled by the first refrigerant first expansion part 131 circulates to the cryogenic heat exchanger 10 side to perform heat exchange.
[0043] The second flow of the first refrigerant flowing into the cryogenic heat
exchanger 10 from the first refrigerant second expansion part 131 may be configured to
sequentially pass through an intermediate heat exchange region 14 (midstream region of
the inner region of the heat exchanger 10 with respect to the flow of natural gas) and a
warm heat exchange region 16 inside the cryogenic heat exchanger 10.
[0044] The first refrigerant second pre-compression part 132 is also provided
downstream of the cryogenic heat exchanger 10 in the entire first refrigerant cycle 100.
The first refrigerant second pre-compression part 132 and the first refrigerant second
expansion part 131 may operate linked with each other.
[0045] The first refrigerant second pre-compression part 132 pre-compresses, for
example to about 20-25 barg, the second flow of the first refrigerant, which have been
expanded by the first refrigerant second expansion part 131 and have passed through the
cryogenic heat exchanger 10 again, and then supplies the second flow to the first
refrigerant first compression part 110 described above.
[0046] The first flow of the first refrigerant pre-compressed by the first refrigerant first
pre-compression part 122 and the second flow of the first refrigerant second pre
compression part 132 may be mixed in a mixing pipe and transferred to the first refrigerant
first compression part 110.
[0047] In the embodiment, the pressure of the first refrigerant discharged from the first
refrigerant first pre-compression part 122 and the pressure of the first refrigerant
discharged from the first refrigerant second pre-compression part 132 may be mixed at the
same pressure, and then the mixed flow is allowed to flow into the first refrigerant first compression part 110. Thus, the compression efficiency of the first refrigerant may be enhanced.
[0048] As described above, in the present embodiment, the first refrigerant
compressed at the first refrigerant first compression part 110 is divided into two flows and
circulate through mutually different paths, and thus, there is a merit in that not only process
variables may easily be adjusted, but also the heat exchange efficiency is very excellent.
[0049] In addition, in the present embodiment, the first turbo expander 120 and the
second turbo expander 130 cools the first refrigerant to mutually different temperatures,
and the flow rate is configured such that about 25-45% is divided to the side of relatively
high process temperature and about 55-75% is divided to the side of relatively low
temperature.
[0050] As such, the first refrigerant with divided flows are introduced into the
cryogenic heat exchanger 10 and a pre-cooling (from about -55 °C to -75°C, to about 30°C
to 45C) and a partial liquefaction (from about -90 °C to -115°C, to about 30°C to 45°C)
may be separated and efficiently performed.
[0051] For example, the first turbo expander 120 may adjust the temperature
difference between the first refrigerant and a fluid in a warm region corresponding to -65
°C to -30°C with the first flow rate of the first refrigerant to adjust the process of the pre
cooling.
[0052] The second turbo expander 130 may adjust the temperature difference between
the first refrigerant and a fluid in an intermediate region corresponding to -110 °C to -65°C
with the second flow rate of the first refrigerant to adjust the process of the liquefaction
(partial liquefaction).
[0053] Meanwhile, as described above, the second refrigerant circulates through the second refrigerant cycle 200, some paths of which perform heat exchange via the cryogenic heat exchanger 10.
[0054] In the present embodiment, the second refrigeration cycle 200 includes a
second refrigerant compression part 210 and the second refrigerant turbo expander 220.
[0055] The second refrigerant compression part 210 is provided upstream of the
cryogenic heat exchanger 10 in the entire second refrigerant cycle 200, and compresses the
second refrigerant to a high pressure (for example, about 50-60 barg).
[0056] In addition, the second refrigerant turbo expander 220 includes a second
refrigerant expansion part 221 and a second refrigerant pre-compression part 222.
[0057] The second refrigerant expansion part 221 is provided downstream of the
cryogenic heat exchanger 10 in the entire second refrigerant cycle 200, is in charge of a
remaining liquefaction process (from about -165 °C to -150°C, to about 30°C to 45°C), and
expands the second refrigerant having passed through the cryogenic heat exchanger 10.
[0058] The second refrigerant may be expanded to about 12-18 barg by the second
refrigerant expansion part 221. The flow of the expanded second refrigerant may be
cooled to about -150 °C to -165°C. The flow of the second refrigerant expanded and
cooled by the second refrigerant expansion part 221 circulates to the cryogenic heat
exchanger 10 side to perform heat exchange. Here, the second refrigerant is in charge of
a process of a cold loop (from -165 °C to -150°C, to 30 °C to 45°C including an ultra cold
section (-165°C to -110°C) in which heat exchange may not be performed with the first
refrigerant.
[0059] The flow of the second refrigerant flowing into the cryogenic heat exchanger
from the second refrigerant expansion part 221 may be configured to sequentially pass
through, in the cryogenic heat exchanger 10, a cold heat exchange region 12 (downstream region inside the heat exchanger 10 with respect to the flow of natural gas), an intermediate heat exchange region 14 (midstream region of the inner region of the heat exchanger 10 with respect to the flow of natural gas) and a warm heat exchange region 16.
[0060] The second refrigerant pre-compression part 222 is also provided downstream
of the cryogenic heat exchanger 10 in the entire second refrigerant cycle 200, and pre
compresses the second refrigerant, having passed through the cryogenic heat exchanger 10
again, to about 15-20 barg, for example.
[0061] The entirety of the pre-cooling, liquefaction, and subcooling which are
liquefaction process of a fluid may be adjusted by the first turbo expander 120, the second
turbo expander 130 and the second refrigerant turbo expander 220.
[0062] As described above, the present embodiment has an additional merit in that the
flow rate of the second refrigerant of the second refrigerant cycle 200 may be reduced
compared to that in the conventional art through an efficient process of the first refrigerant
cycle 100.
[0063] FIG. 2 is a graph illustrating a composite curve of a related natural gas
liquefaction apparatus, and FIG 3 is a view illustrating a composite curve of a natural gas
liquefaction apparatus according to some embodiments. Here, x-axes of the graphs
illustrated in FIGS. 2 and 3 indicate heat flow transferred in a heat exchanger through the
heat amount of each of the turbo expanders and the compression parts, and y-axes indicates
temperatures.
[0064] In addition, the hot composite of natural gas located on the upper side is
depicted in a solid line and the cold composite of the refrigerant located on the lower side
is depicted in a dotted line.
[0065] First, examining the composite curve illustrated in the graph of FIG. 2, it may be confirmed that the temperature difference between the hot composite as natural gas and the cold composite as the refrigerant is large in a range of about -40°C to about -100°C, and thus, it may be found that the area formed between the hot composite and the cold composite is larger than that of the cold region.
[0066] This is because the first refrigerant cycle and the second refrigerant cycle are
entirely formed in series and has only one adjustable inflection point and thus there is a
limit in optimizing a system.
[0067] Conversely, examining the composite curve illustrated in the graph of FIG 3, it
may be confirmed that the temperature difference between the hot composite as natural gas
and the cold composite as the refrigerant is large in a range of about -40°C to about -100°C,
and thus, the area formed between the hot composite and the cold composite may be
minimized.
[0068] This is because the first refrigerant cycle is formed, unlike that in the
conventional art, in series as a pre-cooling section (30 °C to about -65°C) and a partial
liquefaction (30°C to about -110°C), and a plurality of adjustable inflection points are
present.
[0069] A natural gas liquefaction apparatus of the present embodiments has a first
refrigerant cycle composed of a warm loop and an intermediate loop, and a second
refrigerant cycle composed of a cold loop. In FIG 1, the warm loop is illustrated in
dotted lines, the intermediate loop is illustrated in alternate long and short dash lines, and
the cold loop is illustrated in alternate long and two short dash lines.
[0070] Each loop is operated in various temperature ranges considering the composite
curve. For example, the intermediate loop through which the first refrigerant circulates is
cooled to about -90°C to -115°C and may be operated until reaching about 25°C to 45°C, the warm loop through which the first refrigerant circulates is cooled to about -55°C to
°C and may be operated until reaching about 25°C to 45°C, and the cold loop through
which the first refrigerant circulates is cooled to about -150°C to -165°C and may be
operated until reaching about 25°C to 45°C.
[0071] Changes in the amounts or ratios of the first refrigerant and the second
refrigerant which circulate through respective loops may substantially affect the composite
curve. More specifically, a change in the second flow rate of the first refrigerant circulating
through the intermediate loop may substantially affect a liquefaction region between about
-115°Cto-90°C. In addition, a change in the first flow rate circulating through the warm
loop may mainly have influence at about -90°C or higher.
[0072] As such, according to the natural gas liquefaction apparatus of the present
disclosure, by adjusting the first and second flow rates of the first refrigerant and the flow
rate of the second refrigerant, and adjusting the temperatures of the respective loops, the
difference between the composite curves of the fluid (natural gas) and the refrigerants may
effectively be reduced in the temperature sections mainly dealt with the respective loops.
[0073] In addition, the efficiency of a liquefaction process of a fluid may be improved
by reducing the energy consumed for liquefying the fluid by enhancing the compression
efficiency of the refrigerant and effectively cooling the fluid with a simple process.
[0074] The log mean temperature differences (LMTDs) illustrated in FIGS. 2 and 3
are log mean temperature differences between the hot composite of natural gas and the
cold composite of the refrigerant. The LMTD, with which the entire heat exchange process
inside a heat exchange is analyzed by a mean temperature, is a value representing the
temperature difference between the natural gas and the refrigerant. When ALT is the
difference between the inlet side temperature of natural gas and the outlet side temperature of a refrigerant in a heat exchanger, and AT2 is the difference between the outlet side temperature of the natural gas and the inlet side temperature of the refrigerant in a heat exchanger, the LMTD may be calculated as the value of [(AT1-A T2)/{(lnAT1)
(lnAT2)}].
[0075] Referring to FIGS. 2 and 3, when comparing the LMTDs of the composite
curves of actual two processes, it may be found that the difference between the hot
composite of the natural gas and the cold composite of the refrigerant is about 4.309°C and
is smaller in the present embodiment than about 4.685°C in a conventional device, and this
means that the cooling efficiency becomes better.
[0076] In addition, in the present embodiment, unlike in conventional arts, since a
cooling process of at least -110°C is efficiently performed in the first refrigerant cycle, the
flow rate of the second refrigerant required in the second refrigerant cycle is reduced, and
thus, unlike the conventional arts, there is a merit in that sufficient pressurization may be
performed only with a single second refrigerant compression part and the number of
apparatuses may also be reduced.
[0077] In FIGS. 2 and 3, the portions depicted by shadow represent a portion of the
pre-cooling process of natural gas and liquefaction/partial liquefaction process.
Comparing with FIG. 2, according to some embodiments, it may be confirmed that the
difference between the composite curve of the natural gas and the composite curve of the
refrigerant in the pre-cooling process is reduced in the liquefaction/partial liquefaction
processes (portions depicted by shadow in FIG. 3).
[0078] This is because the first refrigerant cycle is formed in parallel as the pre
cooling section (about 30°C to -65°C) and the partial liquefaction section (about 30°C to
110C), so that the pre-cooling section (about 30°C to -65°C) may be adjusted by the first flow rate of the first refrigerant, and the partial liquefaction section (about 30°C to -110°C) may be adjusted by the second flow rate of the first refrigerant, and a plurality of adjustable inflection points are present in the pre-cooling section (about 30°C to -65°C) and the partial liquefaction section (about 30°C to -110°C), and the pre-cooling and partial liquefaction processes may be separated and efficiently performed.
[0079] That is, according to some embodiments, the heat exchange (subcooling
process) between the natural gas and the refrigerant in the ultra cold section (about -165°C
to -110°C) may be adjusted by the second refrigerant cycle in which the second refrigerant
circulates through the cold loop, the heat exchange (liquefaction/partial liquefaction
process) between the natural gas and the refrigerant in the intermediate section (about
110C to -65°C) may be adjusted by the first refrigerant cycle in which the second flow of
the first refrigerant circulates through the intermediate loop, and the heat exchange (pre
cooling process) between the natural gas and the refrigerant in the warm section (about
°C to -30°C) may be adjusted by the first refrigerant cycle in which the first flow of the
first refrigerant circulates through the warm loop
[0080] Thus, according to some embodiments, the first flow rate of the first refrigerant
circulating through the warm loop, the second flow rate of the first refrigerant circulating
through the intermediate loop, and the flow rate of the second refrigerant circulating
through the cold loop are each adjusted, so that the temperature differences between the
fluid and the refrigerants for each loop is adjusted, and the distance between the composite
curves of the fluid (natural gas) and the refrigerants may effectively reduced in the
temperature section mainly dealt with by each loop.
[0081] In addition, the pressure of the first refrigerant discharged from the first
refrigerant first pre-compression part 122 and the pressure of the first refrigerant discharged from the first refrigerant second pre-compression part 132 may be mixed at the same pressure, and then the mixed flow is allowed to flow into the first refrigerant first compression part 110. Thus, the compression efficiency of the refrigerant may be enhanced. That is, according to some embodiments, the efficiency of a liquefaction process of a fluid may be improved by reducing the energy consumed for liquefying the fluid by enhancing the compression efficiency of the refrigerant and effectively cooling the fluid with a simple process.
[0082] In Table 1 provided below, the yields and energy efficiencies of the natural gas
liquefaction apparatuses according to a conventional art and the present embodiment are
compared.
[0083] [Table 1]
Conventional art Present embodiment
Compressor Duty [MW] 40.0 40.0
LNG Production [MTPA] 1.005 1.183
Efficiency [kW/(ton/day)] 14.42 12.23
[0084] Examining Table 1 above, the production was performed on the basis of
available capacity of about 40.0 MW, and it may be confirmed that the present
embodiment may increase the yield as much as about 17.8% from about 1.005 MTPA to
1.183 MTPA in the conventional art.
[0085] In addition, it may be confirmed that energy is reduced to about 12.23 kW from
about 14.42 kW of energy consumed for LNG production of about 1 ton/day, and thus
about 17.8 % of energy may be saved.
[0086] FIG. 4 is a view illustrating the configuration of a natural gas liquefaction
apparatus according to further embodiments.
[0087] In the embodiments illustrated in FIG 4, the entirety of components is
configured in the same manner as the previously described embodiments. However, the
present embodiments are different from the previously described embodiments in that the
flow of a first refrigerant having passed through a cryogenic heat exchanger 10 is divided
into three flows in the first refrigerant cycle 100.
[0088] Accordingly, in the present embodiments, a first flow among the three divided
flows of the first refrigerant is supplied to a first refrigerant first turbo expander 120 side,
and the second flow among the three divided flows of the first refrigerant is supplied to a
first refrigerant second turbo expander 130 side.
[0089] In addition, in the present embodiments, a first refrigerant third turbo expander
140 is further provided, and a third flow among the three divided flows of the first
refrigerant is supplied to the first refrigerant third turbo expander 140 side.
[0090] In addition, the first refrigerant third turbo expander 140 may include: a first
refrigerant third expansion part 141 which expands the third flow among the three divided
flows of the first refrigerant; and a first refrigerant third pre-compression part 142 which
pre-compresses the first refrigerant which has been expanded by the first refrigerant third
expansion part 141 and has passed through again the cryogenic heat exchanger 10.
[0091] As such, it may be found that in the present embodiments, the flow of the first
refrigerant may be divided into a plurality of paths more than two divided paths.
[0092] So far, preferable embodiments of the present disclosure have been described,
and it would be obvious to those skilled in the art that the present invention may be
implemented in other specific forms without departing from the spirit and scope of the
invention aside from the abovementioned embodiments. Therefore, embodiments
described above should not be construed as limitative but illustrative, and thus, the present disclosure is not limited to the above description, and may also be modified within the scope of claims and equivalent scope thereto.
Claims (6)
1. A natural gas liquefaction apparatus comprising:
a cryogenic heat exchanger through which natural gas passes and is liquefied into
liquefied natural gas through heat exchange with a first refrigerant and a second
refrigerant;
a first refrigerant cycle through which the first refrigerant circulates and which
comprises a path for the first refrigerant divided into a plurality of paths at the cryogenic
heat exchanger; and
a second refrigerant cycle through which the second refrigerant circulates and
which comprises a path for the second refrigerant passing though the cryogenic heat
exchanger,
wherein the first refrigerant cycle further comprises:
a first refrigerant first compression part provided upstream of the cryogenic heat
exchanger and configured to compress the first refrigerant to a high pressure, the first
refrigerant compressed at the first refrigerant first compression part being divided into a
first flow and a second flow of the first refrigerant through two respective paths at the
cryogenic heat exchanger;
a first refrigerant first turbo expander comprising a first refrigerant first expansion
part provided downstream of the cryogenic heat exchanger and configured to expand the
first flow of the first refrigerant having passed through the cryogenic heat exchanger, and
a first refrigerant first pre-compression part configured to pre-compress the first
refrigerant which has been expanded by the first refrigerant first expansion part and has
passed through the cryogenic heat exchanger again; a first refrigerant second turbo expander, comprising a first refrigerant second expansion part provided downstream of the cryogenic heat exchanger and configured to expand the second flow of the first refrigerant having passed through the cryogenic heat exchanger, and a first refrigerant second pre-compression part configured to pre-compress the first refrigerant which has been expanded by the first refrigerant second expansion part and has passed through the cryogenic heat exchanger again; and a mixing pipe for mixing the first flow of the first refrigerant pre-compressed by the first refrigerant first pre-compression part and the second flow of the first refrigerant pre-compressed by the first refrigerant second pre-compression part, the mixed first and second flows of the first refrigerant in the mixing pipe flowing into the first refrigerant first compression part.
2. The natural gas liquefaction apparatus of claim 1, wherein the first refrigerant first
expansion part expands the first flow of the first refrigerant to a first temperature and the
first refrigerant second expansion part expands the second flow of the first refrigerant to a
second temperature which is lower than the first temperature, and wherein the flow rate of
the first flow of the first refrigerant is lower than the flow rate of the second flow of the
first refrigerant.
3. The natural gas liquefaction apparatus of claim 1, wherein the first refrigerant
compressed at the first refrigerant first compression part is divided into the first flow, the
second flow and a third flow of the first refrigerant through three respective paths at the
cryogenic heat exchanger, and wherein the first refrigerant cycle further comprises: a first refrigerant third turbo expander comprising a first refrigerant third expansion part provided downstream of the cryogenic heat exchanger and configured to expand the third flow of the first refrigerant having passed through the cryogenic heat exchanger, and a first refrigerant third pre-compression part configured to pre-compress the first refrigerant which has been expanded by the first refrigerant third expansion part and has passed through the cryogenic heat exchanger again, and wherein the first flow of the first refrigerant pre-compressed by the first refrigerant first pre-compression part, the second flow of the first refrigerant pre-compressed by the first refrigerant second pre-compression part, and the third flow of the first refrigerant pre compressed by the first refrigerant third pre-compression part are mixed in the mixing pipe and flow into the first refrigerant first compression part.
4. The natural gas liquefaction apparatus of claim 2 or claim 3, wherein the first
refrigerant first compression part is provided as a plurality of compression parts.
5. The natural gas liquefaction apparatus of any one of claims 1 to 4, wherein the
second refrigerant cycle further comprises:
a second refrigerant compression part provided upstream of the cryogenic heat
exchanger and configured to compress the second refrigerant to a high pressure; and
a second refrigerant turbo expander comprising a second refrigerant expansion part
provided downstream of the cryogenic heat exchanger and configured to expand the
second refrigerant having passed through the cryogenic heat exchanger, and a second
refrigerant pre-compression part configured to pre-compress the second refrigerant which
has been expanded by the second refrigerant expansion part and has passed through the cryogenic heat exchanger again.
6. The natural gas liquefaction apparatus of claims 1 to 5, wherein the first refrigerant
comprises methane, and the second refrigerant comprise nitrogen.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR10-2017-0059322 | 2017-05-12 | ||
| KR20170059322 | 2017-05-12 | ||
| KR1020170178604A KR102039618B1 (en) | 2017-05-12 | 2017-12-22 | Natural Gas Liquefaction Apparatus |
| KR10-2017-0178604 | 2017-12-22 | ||
| PCT/KR2018/000701 WO2018207994A1 (en) | 2017-05-12 | 2018-01-16 | Natural gas liquefaction apparatus |
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| Publication Number | Publication Date |
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| AU2018264606A1 AU2018264606A1 (en) | 2019-12-12 |
| AU2018264606B2 true AU2018264606B2 (en) | 2021-05-27 |
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| AU2018264606A Active AU2018264606B2 (en) | 2017-05-12 | 2018-01-16 | Natural gas liquefaction apparatus |
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| US (1) | US20230266059A1 (en) |
| EP (1) | EP3637029A4 (en) |
| AU (1) | AU2018264606B2 (en) |
| WO (1) | WO2018207994A1 (en) |
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| WO2020204218A1 (en) * | 2019-04-01 | 2020-10-08 | 삼성중공업 주식회사 | Cooling system |
| US20230115492A1 (en) * | 2021-10-13 | 2023-04-13 | Henry Edward Howard | System and method to produce liquefied natural gas |
| US20230129424A1 (en) * | 2021-10-21 | 2023-04-27 | Henry Edward Howard | System and method to produce liquefied natural gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100786135B1 (en) * | 2001-03-06 | 2007-12-21 | 에이비비 루머스 글러벌 인코포레이티드 | Lng production using dual independent expander refrigeration cycles |
| KR20140093952A (en) * | 2011-10-21 | 2014-07-29 | 싱글 뷰이 무어링스 인크. | Multi nitrogen expansion process for lng production |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1549893A1 (en) * | 2002-09-30 | 2005-07-06 | BP Corporation North America Inc. | Modular lng process |
| US7581411B2 (en) * | 2006-05-08 | 2009-09-01 | Amcs Corporation | Equipment and process for liquefaction of LNG boiloff gas |
| FR2938903B1 (en) * | 2008-11-25 | 2013-02-08 | Technip France | PROCESS FOR PRODUCING A LIQUEFIED NATURAL GAS CURRENT SUB-COOLED FROM A NATURAL GAS CHARGE CURRENT AND ASSOCIATED INSTALLATION |
| GB2479940B (en) * | 2010-04-30 | 2012-09-05 | Costain Oil Gas & Process Ltd | Process and apparatus for the liquefaction of natural gas |
| US20140352353A1 (en) * | 2013-05-28 | 2014-12-04 | Robert S. Wissolik | Natural Gas Liquefaction System for Producing LNG and Merchant Gas Products |
-
2018
- 2018-01-16 AU AU2018264606A patent/AU2018264606B2/en active Active
- 2018-01-16 WO PCT/KR2018/000701 patent/WO2018207994A1/en active Application Filing
- 2018-01-16 EP EP18799240.9A patent/EP3637029A4/en active Pending
- 2018-01-16 US US16/612,863 patent/US20230266059A1/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100786135B1 (en) * | 2001-03-06 | 2007-12-21 | 에이비비 루머스 글러벌 인코포레이티드 | Lng production using dual independent expander refrigeration cycles |
| KR20140093952A (en) * | 2011-10-21 | 2014-07-29 | 싱글 뷰이 무어링스 인크. | Multi nitrogen expansion process for lng production |
Also Published As
| Publication number | Publication date |
|---|---|
| US20230266059A1 (en) | 2023-08-24 |
| EP3637029A4 (en) | 2021-01-06 |
| AU2018264606A1 (en) | 2019-12-12 |
| WO2018207994A1 (en) | 2018-11-15 |
| EP3637029A1 (en) | 2020-04-15 |
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