WO2018207994A1 - 천연가스 액화장치 - Google Patents
천연가스 액화장치 Download PDFInfo
- Publication number
- WO2018207994A1 WO2018207994A1 PCT/KR2018/000701 KR2018000701W WO2018207994A1 WO 2018207994 A1 WO2018207994 A1 WO 2018207994A1 KR 2018000701 W KR2018000701 W KR 2018000701W WO 2018207994 A1 WO2018207994 A1 WO 2018207994A1
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- WIPO (PCT)
- Prior art keywords
- refrigerant
- heat exchanger
- cryogenic heat
- flow rate
- natural gas
- Prior art date
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 106
- 239000003345 natural gas Substances 0.000 title claims abstract description 52
- 239000003507 refrigerant Substances 0.000 claims abstract description 309
- 230000006835 compression Effects 0.000 claims description 56
- 238000007906 compression Methods 0.000 claims description 56
- 238000000034 method Methods 0.000 claims description 36
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- 239000002131 composite material Substances 0.000 description 21
- 239000012530 fluid Substances 0.000 description 11
- 238000001816 cooling Methods 0.000 description 10
- 239000003949 liquefied natural gas Substances 0.000 description 8
- 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
- 230000000694 effects Effects 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
- 239000007789 gas Substances 0.000 description 2
- 239000000969 carrier Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000001151 other effect Effects 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
Images
Classifications
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
Definitions
- the present invention 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.
- Natural gas is generally transported in a gaseous state through onshore or offshore gas piping, or stored and transported in LNG carriers in the form of liquefied natural gas (LNG).
- LNG liquefied natural gas
- liquefied natural gas is obtained by cooling natural gas to cryogenic temperature, and its volume is reduced to about 1/600 than that of natural gas in gas state, so it is very suitable for long distance transportation through sea.
- the liquefaction method of the natural gas conventionally used is performed by cooling natural gas through one or more heat exchanger inside.
- the present invention has been made in order to solve the problems of the prior art described above, and has an object to provide a natural gas liquefaction apparatus that can easily control the process parameters, and maximize the heat exchange efficiency.
- Natural gas liquefaction apparatus of the present invention for achieving the above object, the cryogenic heat exchanger liquefied into LNG through heat exchange with the first refrigerant and the second refrigerant via the natural gas, the first refrigerant is circulated, A first refrigerant cycle in which a path is heat exchanged through the cryogenic heat exchanger, and after the heat exchange is performed in the cryogenic heat exchanger, dividing the path of the first refrigerant into a plurality of paths to expand and linearly compress the first refrigerant. And a second refrigerant cycle through which the second refrigerant circulates, wherein some paths pass through the cryogenic heat exchanger.
- the first refrigerant cycle is provided upstream of the cryogenic heat exchanger, and is provided at a first refrigerant first compression unit for compressing the first refrigerant at a high pressure and downstream of the cryogenic heat exchanger.
- a first refrigerant first expansion portion for expanding a first flow rate of the two-divided flow rate of the first refrigerant, and the first refrigerant expanded by the first refrigerant first expansion portion and re-passed through the cryogenic heat exchanger
- the second refrigerant flow rate is provided downstream of the first refrigerant first turbo expander and the cryogenic heat exchanger, including the first refrigerant first linear compression unit to compress, and a second flow rate of the two divided flow rates of the first refrigerant via the cryogenic heat exchanger.
- a first refrigerant comprising a first refrigerant second expansion portion to expand and a first refrigerant second linear compression portion which is expanded by the first refrigerant second expansion portion and precompresses the first refrigerant having passed through the cryogenic heat exchanger again; Second turbo It may include long-term.
- the first refrigerant cycle is provided upstream of the cryogenic heat exchanger, the first refrigerant first compression unit for compressing the first refrigerant at high pressure, downstream of the cryogenic heat exchanger, the cryogenic heat exchanger via A first refrigerant first expansion part for expanding a first flow rate among the three divided flow rates of the first refrigerant, and the first refrigerant that is expanded by the first refrigerant first expansion part to be re-passed through the cryogenic heat exchanger
- a first refrigerant first turbo expander including a first refrigerant first linear compression unit to be compressed and downstream of the cryogenic heat exchanger, and a second flow rate among the three divided flow rates of the first refrigerant via the cryogenic heat exchanger;
- a first refrigerant comprising a first refrigerant second expansion portion to expand and a first refrigerant second linear compression portion which is expanded by the first refrigerant second expansion portion and precompresses the first refrigerant having passed through the cryogenic heat exchanger
- first refrigerant compression parts may be provided.
- the second refrigerant cycle may be provided upstream of the cryogenic heat exchanger, provided in a second refrigerant compression unit for compressing the second refrigerant at a high pressure, and downstream of the cryogenic heat exchanger.
- a second refrigerant turboexpander comprising a second refrigerant expansion portion for expanding a second refrigerant and a second refrigerant linear compression portion for expanding the second refrigerant by expansion by the second refrigerant expansion portion and re-passing the cryogenic heat exchanger. It may include.
- Natural gas liquefaction apparatus of the present invention for solving the above problems has the following effects.
- FIG. 1 is a view showing the configuration of a natural gas liquefaction apparatus according to a first embodiment of the present invention
- FIG. 2 is a graph showing a composite curve of a conventional natural gas liquefaction apparatus
- FIG. 3 is a graph showing a composite curve of a natural gas liquefaction apparatus according to the first embodiment of the present invention.
- FIG. 4 is a view showing the configuration of a natural gas liquefaction apparatus according to a second embodiment of the present invention.
- FIG. 1 is a view showing the configuration of a natural gas liquefaction apparatus according to a first embodiment of the present invention.
- the natural gas liquefaction apparatus includes a cryogenic heat exchanger 10, a first refrigerant cycle 100, and a second refrigerant cycle 200.
- the cryogenic heat exchanger (10) is passed through the natural gas, LNG through the heat exchange with the first refrigerant circulating the first refrigerant cycle 100 and the second refrigerant circulating the second refrigerant cycle 200. Allow liquefaction.
- the first refrigerant is methane
- the second refrigerant is nitrogen
- the first refrigerant circulates as described above, and a portion of the first refrigerant cycle 100 performs heat exchange via the cryogenic heat exchanger 10.
- the first refrigerant cycle 100 is formed to perform expansion and linear compression of the first refrigerant by dividing a plurality of paths of the first refrigerant after performing heat exchange in the cryogenic heat exchanger 10. do. That is, after the first refrigerant cycle 100 passes through the cryogenic heat exchanger 10, the path of the first refrigerant is divided to have a parallel structure.
- the first refrigerant cycle 100 includes a first refrigerant first compression unit 110, a first turbo expander 120, and a second turbo expander 130.
- the first refrigerant first compression unit 110 is provided upstream of the cryogenic heat exchanger 10 of the entire first refrigerant cycle 100, the first refrigerant is a high pressure (for example, 50 ⁇ 60 barg) To compress.
- the first refrigerant first compression unit 110 is provided with a plurality of (111, 112).
- the first turbo expander 120 includes a first refrigerant first expansion part 121 and a first refrigerant first linear compression part 122.
- the first refrigerant first expansion part 121 is provided downstream of the cryogenic heat exchanger 10 of the entire first refrigerant cycle 100, and after passing through the cryogenic heat exchanger 10, The first flow rate, which is part of the divided flow rate, is expanded.
- the first flow rate of the first refrigerant may be expanded to 10 to 12 barg, for example.
- the first flow rate of the expanded first refrigerant may be cooled to, for example, -55 to -75 ° C.
- the first flow rate of the first refrigerant expanded and cooled by the first refrigerant first expansion part 121 circulates to the cryogenic heat exchanger 10 to perform heat exchange.
- the first flow rate of the first refrigerant flowing into the cryogenic heat exchanger 10 from the first refrigerant first expansion part 121 is the heat exchange region 16 of the cryogenic heat exchanger 10 (heat exchange based on the flow of natural gas). And an upstream region of the region within the vessel 10.
- the first refrigerant first linear compression unit 122 is likewise provided downstream of the cryogenic heat exchanger 10 of the entire first refrigerant cycle 100.
- the first refrigerant first linear compression unit 122 and the first refrigerant first expansion unit 121 may operate in conjunction with each other.
- the first refrigerant first linear compression unit 122 is expanded by the first refrigerant first expansion unit 121 to set the first flow rate of the first refrigerant after re-passing the cryogenic heat exchanger 10, for example, 20. After pre-compression to ⁇ 25 barg, the first refrigerant is supplied to the first compression unit 110 again.
- the second turbo expander 130 includes a first refrigerant second expansion unit 131 and a first refrigerant second linear compression unit 132.
- the first refrigerant second expansion portion 131 is provided downstream of the cryogenic heat exchanger 10 in the entire first refrigerant cycle 100, and passes through the cryogenic heat exchanger 10 and then of the first refrigerant.
- the second flow rate which is the remaining part of the divided flow rate, is expanded.
- the first refrigerant first expansion unit 121 and the first refrigerant second expansion unit 131 are introduced into the cryogenic heat exchanger 10 from the first refrigerant first compression unit 110 through the same refrigerant line, and thus the cryogenic heat exchange.
- the first flow rate and the second flow rate of the first refrigerant to be heat exchanged in the apparatus 10 are configured to be sequentially supplied.
- the second flow rate of the first refrigerant may be expanded to 15 to 20 barg, for example.
- the second flow rate of the expanded first refrigerant may be cooled, for example, to -90 to -115 °C.
- the second flow rate of the first refrigerant expanded and cooled by the first refrigerant second expansion part 131 is circulated to the cryogenic heat exchanger 10 to perform heat exchange.
- the second flow rate of the first refrigerant flowing into the cryogenic heat exchanger 10 from the first refrigerant second expansion portion 131 is the mid-temperature heat exchange region 14 of the cryogenic heat exchanger 10 (based on the flow of natural gas). It may be configured to sequentially pass through the middle portion of the region within the heat exchanger 10 and the hot portion heat exchange region (16).
- the first refrigerant second line compressor 132 is likewise provided downstream of the cryogenic heat exchanger 10 of the entire first refrigerant cycle 100.
- the first refrigerant second line compression unit 132 and the first refrigerant second expansion unit 131 may operate in conjunction with each other.
- the first refrigerant second linear compression part 132 is expanded by the first refrigerant second expansion part 131 and uses a second flow rate of the first refrigerant, for example, 20 which is re-passed through the cryogenic heat exchanger 10. After pre-compression to ⁇ 25 barg, the first refrigerant is supplied to the first compression unit 110 again.
- the first flow rate of the first refrigerant pre-compressed by the first refrigerant first linear compression unit 122 and the second flow rate of the first refrigerant pre-compressed by the first refrigerant second linear compression unit 132 are mixed.
- the mixture may be mixed in the tube and transferred to the first refrigerant first compression unit 110.
- the pressure of the first refrigerant discharged from the first refrigerant first linear compression unit 122 and the pressure of the first refrigerant discharged from the first refrigerant second linear compression unit 132 are equally mixed.
- the compression efficiency of the first refrigerant may be increased.
- the first refrigerant compressed by the first refrigerant first compression unit 110 is divided into two flow rates to circulate different paths connected in parallel, thereby easily adjusting process variables.
- the heat exchange efficiency is very excellent.
- the first turbo expander 120 and the second turbo expander 130 cool the first refrigerant to different temperatures, and have a relatively high process temperature of 25 to 45%.
- the flow rate was divided into 55 to 75% on the side having a low process temperature.
- the first refrigerant having the flow rate divided therein is introduced into the cryogenic heat exchanger 10 to be precooled (-55 ° C. to 75 ° C. to 30 ° C. to 45 ° C.) and partial liquefaction (30 ° C. to ⁇ 90 ° C. to ⁇ 115 ° C.). °C to 45 °C) process can be separated and carried out efficiently.
- the first turbo expander 120 adjusts a precooling process by adjusting a temperature interval between the first refrigerant and the fluid in a warm region corresponding to ⁇ 65 ° C. to 30 ° C. as the first flow rate of the first refrigerant. Can be.
- the second turbo expander 130 performs a liquefaction (part liquefaction) process by adjusting the temperature interval between the first refrigerant and the fluid in an intermediate region corresponding to -110 ° C to -65 ° C as the second flow rate of the first refrigerant. I can adjust it.
- the second refrigerant circulates as described above, and a part of the second refrigerant cycle 200 performs heat exchange via the cryogenic heat exchanger 10.
- the second refrigerant cycle 200 includes a second refrigerant compression unit 210 and a second refrigerant turbo expander 220.
- the second refrigerant compression unit 210 is provided upstream of the cryogenic heat exchanger 10 of the entire second refrigerant cycle 200, and compresses the second refrigerant to a high pressure (for example, 50 to 60 barg). do.
- the second refrigerant turbo expander 220 includes a second refrigerant expansion unit 221 and a second refrigerant linear compression unit 222.
- the second refrigerant expansion part 221 is provided downstream of the cryogenic heat exchanger 10 in the entire second refrigerant cycle 200, the remaining part of the liquefaction process (-165 °C ⁇ -150 °C 30 °C ⁇ 45 To expand the second refrigerant via the cryogenic heat exchanger (10).
- the second refrigerant may be expanded to, for example, 12 to 18 barg by the second refrigerant expansion part 221.
- the flow rate of the expanded second refrigerant may be cooled to ⁇ 150 ° C. to ⁇ 165 ° C.
- the flow rate of the second refrigerant expanded and cooled by the second refrigerant expansion unit 221 is circulated to the cryogenic heat exchanger 10 to perform heat exchange.
- the second refrigerant is in charge of a low temperature loop (-165 ° C.-150 ° C. to 30 ° C.-45 ° C.) process including a cryogenic section ( ⁇ 165 ° C. to 110 ° C.) that cannot be heat exchanged in the first refrigerant.
- the flow rate of the second refrigerant flowing into the cryogenic heat exchanger 10 from the second refrigerant expansion part 221 is the low temperature heat exchanger region 12 (the heat exchanger 10 based on the flow of natural gas) in the cryogenic heat exchanger 10. Downstream regions of the inner region), the middle temperature portion heat exchange region 14, and the high temperature portion heat exchange region 16.
- the second refrigerant precompression unit 222 is provided downstream of the cryogenic heat exchanger 10 in the entire second refrigerant cycle 200, and the second refrigerant is re-passed through the cryogenic heat exchanger 10. For example, it is precompressed to 15 to 20 barg.
- the entire liquid pre-cooling, liquefaction, and subcooling processes can be easily performed. I can adjust it.
- the present invention additionally has an advantage of reducing the flow rate of the second refrigerant of the second refrigerant cycle 200 compared to the prior art through an efficient process structure of the first refrigerant cycle 100.
- FIG. 2 is a graph showing a composite curve of a conventional natural gas liquefaction apparatus
- Figure 3 is a graph showing a composite curve of a natural gas liquefaction apparatus according to a first embodiment of the present invention.
- the x-axis of the graph shown in Figures 2 and 3 represents the heat flow (HeatFlow) of heat generated in the heat exchanger through the heat of each of the turbo expander and the compression unit
- y-axis represents the temperature.
- the temperature curve (Hot composite) of the natural gas located on the upper side is shown by the solid line
- the temperature curve (Cold composite) of the refrigerant located on the lower side is shown by the dotted line.
- the temperature difference between the hot composite, which is a natural gas, and the cold composite, which is a refrigerant is large between -40 ° C. and ⁇ 100 ° C., thus forming between the hot composite and the cold composite.
- the area is also larger than the low temperature section.
- the temperature difference between the hot composite, which is a natural gas, and the cold composite, which is a refrigerant is small between -40 ° C. and ⁇ 100 ° C., thus forming between the hot composite and the cold composite. Area is minimized.
- the first refrigerant cycle is formed in parallel to the precooling section (30 °C ⁇ -65 °C) and the partial liquefaction (30 °C ⁇ -110 °C) section unlike the conventional one, and there are a plurality of adjustable points (Inflection Point) in the section Because.
- the first refrigerant cycle consists of a warm loop and an intermediate loop
- the second refrigerant cycle consists of a cold loop.
- the warm loop is shown by the dotted line
- the intermediate loop is shown by the dashed line
- the cold loop is shown by the dashed line.
- Each loop operates over a wide range of temperatures, taking into account the temperature curve.
- the intermediate loop may be operated until the first refrigerant is circulated, and is cooled to ⁇ 90 ° C. to ⁇ 115 ° C. until the temperature reaches 25 ° C. to 45 ° C.
- the warm loop may be used to circulate the first refrigerant. It can be operated until it is cooled to -55 ⁇ -75 °C until it reaches 25 ⁇ 45 °C, the cold loop is a second refrigerant circulate, and after cooling to -150 ⁇ -165 °C 25 ⁇ It can be operated until 45 ° C.
- Changes in the amount or ratio of the first and second refrigerants circulating in each of these loops can greatly affect the temperature curve. More specifically, fluctuations in the second flow rate of the first refrigerant circulating in the intermediate loop can have a great influence on the liquefaction region between -115 ° C and -90 ° C. In addition, the fluctuation of the first flow rate of the first refrigerant circulating in the warm loop may mainly affect the above -90 ° C.
- the natural gas liquefaction apparatus of the present invention adjusts the flow rate of the first flow rate, the second flow rate and the second refrigerant of the first refrigerant circulating each loop, and adjusts the temperature of each loop, and is mainly responsible for each loop. It can effectively reduce the temperature curve interval between the fluid (natural gas) and the refrigerant in the temperature range section.
- Log Mean Temperature Difference described in FIGS. 2 and 3 is a logarithmic average temperature difference between a hot composite of natural gas and a cold composite of a refrigerant.
- LMTD is an average temperature of the entire heat exchange process inside the heat exchanger, and represents an average value representing the temperature difference between the natural gas and the refrigerant.
- LMTD is It can be calculated as a value of [( ⁇ T1- ⁇ T2) / ⁇ (ln ⁇ T1)-(ln ⁇ T2) ⁇ .
- the present embodiment efficiently performs a cooling process of ⁇ 110 ° C. or higher in the first refrigerant cycle unlike the conventional art, the flow rate of the second refrigerant required in the second refrigerant cycle is reduced, and thus, unlike the prior art, a single Only the two refrigerant compression unit can perform a sufficient pressure, there is an advantage that can reduce the number of equipment.
- FIGS. 2 and 3 represent a part of the precooling process of natural gas and a liquefaction / partial liquefaction process.
- the gap between the temperature curve of the natural gas and the temperature curve of the refrigerant is narrowed during the precooling process of the natural gas and the liquefaction / part liquefaction process (shaded in FIG. 3). You can see that.
- the first refrigerant cycle is formed in parallel with the precooling section (30 ° C.-65 ° C.) and the partial liquefaction section (30 ° C.-110 ° C.) so that the precooling section (30 ° C.-65) is provided by the first flow rate of the first refrigerant.
- the partial liquefaction section (30 ° C ⁇ -110 ° C) can be adjusted, and the partial liquefaction section (30 ° C ⁇ -110 ° C) can be adjusted by the second flow rate of the first refrigerant, the precooling section (30 ° C ⁇ -65 ° C) and the partial liquefaction section (30 This is because there are a plurality of adjustable points (Inflection Point) at °C ⁇ -110 °C), and the pre-cooling and partial liquefaction process can be separated and performed efficiently.
- adjustable points Inflection Point
- the heat exchange (supercooling process) between the natural gas and the refrigerant in the cryogenic section is a second refrigerant cycle in which the second refrigerant circulates the cold loop
- Heat exchange between the natural gas and the refrigerant (liquidification / partial liquefaction process) in the intermediate section allows the second flow rate of the first refrigerant to pass through the intermediate loop.
- the first flow rate of the first refrigerant circulating the hot loop, the second flow rate of the first refrigerant circulating the middle temperature loop and the flow rate of the second refrigerant circulating the low temperature loop are adjusted.
- the temperature interval between the fluid and the refrigerant for each loop it is possible to effectively reduce the temperature curve interval between the fluid (natural gas) and the refrigerant in the temperature range section mainly responsible for each loop.
- the compression efficiency of the refrigerant can be increased. That is, according to the embodiment of the present invention, by increasing the compression efficiency of the refrigerant in a simple process, by effectively cooling the fluid (natural gas) to reduce the energy consumed to liquefy the fluid, it is possible to improve the efficiency of the fluid liquefaction process have.
- Table 1 below is a comparison of the production efficiency and energy efficiency of the natural gas liquefaction apparatus according to the prior art and the present embodiment.
- FIG. 4 is a view showing the configuration of a natural gas liquefaction apparatus according to a second embodiment of the present invention.
- the second embodiment of the present invention shown in FIG. 4 also has the same overall components as the first embodiment. However, in the present embodiment, the flow rate of the first refrigerant via the cryogenic heat exchanger 10 is divided into three in the first refrigerant cycle 100 is different from the first embodiment described above.
- the first flow rate is supplied to the first refrigerant first turbo expander 120 and the third flow rate of the first refrigerant is divided into the first refrigerant second turbo expander 130.
- the second flow rate is supplied among the three divided flow rates.
- the first refrigerant third turbo expander 140 is further provided, and a third flow rate is supplied to the first refrigerant third turbo expander 140 at a flow rate divided by the third refrigerant.
- first refrigerant third turbo expander 140 may include a first refrigerant third expansion part 141 for expanding a third flow rate among three flow rates divided by the first refrigerant, and the first refrigerant third expansion part ( 141 may include a first refrigerant third linear compression unit 142 for pre-compressing the first refrigerant having re-passed through the cryogenic heat exchanger 10.
- the present invention can divide the flow rate of the first refrigerant into a plurality of paths more than two divisions.
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Abstract
Description
종래기술 | 본 실시예 | |
Compressor Duty [MW] | 40.0 | 40.0 |
LNG Production [MTPA] | 1.005 | 1.183 |
Efficiency [kW/(ton/day)] | 14.42 | 12.23 |
Claims (5)
- 천연가스가 경유하여 제1냉매 및 제2냉매와의 열교환을 통해 LNG로 액화되는 극저온 열교환기;상기 제1냉매가 순환하며, 일부 경로가 상기 극저온 열교환기를 경유하여 열교환을 수행하되, 상기 극저온 열교환기에서 열교환을 수행한 이후 상기 제1냉매의 경로를 복수 개로 분할하여 상기 제1냉매의 팽창 및 선압축을 수행하는 제1냉매 사이클; 및상기 제2냉매가 순환하며, 일부 경로가 상기 극저온 열교환기를 경유하는 제2냉매 사이클;을 포함하는 천연가스 액화장치.
- 제1항에 있어서,상기 제1냉매 사이클은,상기 극저온 열교환기의 상류에 구비되며, 상기 제1냉매를 고압으로 압축하는 제1냉매 제1압축부;상기 극저온 열교환기의 하류에 구비되며, 상기 극저온 열교환기를 경유한 상기 제1냉매의 2분할된 유량 중 제1유량을 팽창시키는 제1냉매 제1팽창부와, 상기 제1냉매 제1팽창부에 의해 팽창되어 상기 극저온 열교환기를 재경유한 상기 제1냉매를 선압축하는 제1냉매 제1선압축부를 포함하는 제1냉매 제1터보 확장기; 및상기 극저온 열교환기의 하류에 구비되며, 상기 극저온 열교환기를 경유한 상기 제1냉매의 2분할된 유량 중 제2유량을 팽창시키는 제1냉매 제2팽창부와, 상기 제1냉매 제2팽창부에 의해 팽창되어 상기 극저온 열교환기를 재경유한 상기 제1냉매를 선압축하는 제1냉매 제2선압축부를 포함하는 제1냉매 제2터보 확장기;를 포함하는 천연가스 액화장치.
- 제1항에 있어서,상기 제1냉매 사이클은,상기 극저온 열교환기의 상류에 구비되며, 상기 제1냉매를 고압으로 압축하는 제1냉매 제1압축부;상기 극저온 열교환기의 하류에 구비되며, 상기 극저온 열교환기를 경유한 상기 제1냉매의 3분할된 유량 중 제1유량을 팽창시키는 제1냉매 제1팽창부와, 상기 제1냉매 제1팽창부에 의해 팽창되어 상기 극저온 열교환기를 재경유한 상기 제1냉매를 선압축하는 제1냉매 제1선압축부를 포함하는 제1냉매 제1터보 확장기;상기 극저온 열교환기의 하류에 구비되며, 상기 극저온 열교환기를 경유한 상기 제1냉매의 3분할된 유량 중 제2유량을 팽창시키는 제1냉매 제2팽창부와, 상기 제1냉매 제2팽창부에 의해 팽창되어 상기 극저온 열교환기를 재경유한 상기 제1냉매를 선압축하는 제1냉매 제2선압축부를 포함하는 제1냉매 제2터보 확장기; 및상기 극저온 열교환기의 하류에 구비되며, 상기 극저온 열교환기를 경유한 상기 제1냉매의 3분할된 유량 중 제3유량을 팽창시키는 제1냉매 제3팽창부와, 상기 제1냉매 제3팽창부에 의해 팽창되어 상기 극저온 열교환기를 재경유한 상기 제1냉매를 선압축하는 제1냉매 제3선압축부를 포함하는 제1냉매 제3터보 확장기;를 포함하는 천연가스 액화장치.
- 제2항 또는 제3항에 있어서,상기 제1냉매 제1압축부는 복수 개가 구비되는 천연가스 액화장치.
- 제1항에 있어서,상기 제2냉매 사이클은,상기 극저온 열교환기의 상류에 구비되며, 상기 제2냉매를 고압으로 압축하는 제2냉매 압축부; 및상기 극저온 열교환기의 하류에 구비되며, 상기 극저온 열교환기를 경유한 상기 제2냉매를 팽창시키는 제2냉매 팽창부와, 상기 제2냉매 팽창부에 의해 팽창되어 상기 극저온 열교환기를 재경유한 상기 제2냉매를 선압축하는 제2냉매 선압축부를 포함하는 제2냉매 터보 확장기;를 포함하는 천연가스 액화장치.
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2018
- 2018-01-16 AU AU2018264606A patent/AU2018264606B2/en active Active
- 2018-01-16 WO PCT/KR2018/000701 patent/WO2018207994A1/ko active Application Filing
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KR100786135B1 (ko) * | 2001-03-06 | 2007-12-21 | 에이비비 루머스 글러벌 인코포레이티드 | 이중독립팽창기냉각사이클들을 이용하는 액화천연가스의생산방법 |
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