CN104520660A - System and method for natural gas liquefaction - Google Patents
System and method for natural gas liquefaction Download PDFInfo
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- CN104520660A CN104520660A CN201280075097.1A CN201280075097A CN104520660A CN 104520660 A CN104520660 A CN 104520660A CN 201280075097 A CN201280075097 A CN 201280075097A CN 104520660 A CN104520660 A CN 104520660A
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- refrigeration
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- natural gas
- expander
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- 238000000034 method Methods 0.000 title claims abstract description 43
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 144
- 239000003345 natural gas Substances 0.000 title claims description 71
- 238000005057 refrigeration Methods 0.000 claims abstract description 171
- 238000004519 manufacturing process Methods 0.000 claims abstract description 44
- 239000003507 refrigerant Substances 0.000 claims abstract description 38
- 238000007906 compression Methods 0.000 claims abstract description 11
- 230000006835 compression Effects 0.000 claims abstract description 9
- 239000003949 liquefied natural gas Substances 0.000 claims description 117
- 230000008878 coupling Effects 0.000 claims description 81
- 238000010168 coupling process Methods 0.000 claims description 81
- 238000005859 coupling reaction Methods 0.000 claims description 81
- 238000001816 cooling Methods 0.000 claims description 49
- 239000007789 gas Substances 0.000 claims description 41
- 238000005096 rolling process Methods 0.000 claims description 30
- 238000011144 upstream manufacturing Methods 0.000 claims description 27
- 238000007710 freezing Methods 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 20
- 230000008014 freezing Effects 0.000 claims description 19
- 230000009467 reduction Effects 0.000 claims description 5
- 230000009969 flowable effect Effects 0.000 claims description 4
- 230000008569 process Effects 0.000 description 25
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 17
- 238000010586 diagram Methods 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 239000000203 mixture Substances 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910000906 Bronze Inorganic materials 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000010974 bronze Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003653 coastal water Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- KUNSUQLRTQLHQQ-UHFFFAOYSA-N copper tin Chemical compound [Cu].[Sn] KUNSUQLRTQLHQQ-UHFFFAOYSA-N 0.000 description 1
- 239000007799 cork Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000004172 nitrogen cycle Methods 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- 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
- F25J1/003—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
- F25J1/0052—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 vaporising a liquid refrigerant stream
-
- 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
- F25J1/02—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
-
- 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
- F25J1/0204—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 single flow SCR cycle
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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
- 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
Abstract
The present invention provides an LNG production system and method with improved refrigeration. The refrigeration is achieved by a refrigeration device comprising a plurality of refrigerant compressors (11, 13, 15, 17) configured into a series arrangement to perform multi-stage compressions of a refrigerant, a plurality of aftercoolers (12, 14, 16, 18) each of which being coupled to each of the plurality of refrigerant compressors to cool the compressed refrigerant, a plurality of turboexpanders (19, 20) coupled to the last aftercooler (18) and configured into a series configuration to perform multi-stage expansions of the compressed refrigerant, and a plurality of refrigerant heat exchange means (33, 34) coupled to both the first (11) of the plurality of refrigerant compressors and the last (20) of the plurality of turboexpanders, so that all components form a close refrigeration cycle.
Description
Technical field
The present invention is broadly directed to liquefaction Technology of Natural Gas, and particularly a kind of employing is configured to the system and method for multiple turbo-expanders for natural gas liquefaction of arranged in series.
Background technology
In order to transport natural gas in a more effective manner, importantly liquefied as being used for the liquefied natural gas (LNG) transported, this by the volume contraction 600 times of natural gas, thus can be transported to the consumer of other parts of the world.Many LNG liquefaction plant utilizes the kind of refrigeration cycle with mix refrigerant, its refrigeration be generally by use have comprise propane, propylene, ethane, ethene, methane and nitrogen or its mixture the heat exchange of cold-producing medium under closed loop or open loop form of one or more compositions realize.Owing to can the different phase of described liquefaction process of cold-producing medium evaporation latent heat utilized closely near the cooling curve of natural gas and multi-component refrigrant, therefore mixed-refrigerant cycle be effective.
For the natural gas liquefaction in coastal waters, recommend nitrogen expander cycle, because compared with the LNG technique based on mix refrigerant, it is safer and to relate to the environmental risk of cold-producing medium seepage less.In addition, nitrogen cycle does not need to store hydrocarbon coolant.
Know reverse Brayton cycle and be used to natural gas liquefaction.But the performance of LNG process is subject to be permitted multifactorial restriction, if the maximum temperature of main low temperature heat exchanger is close to limit, and the limited expansion ratio that single expansion function reaches.Usually, the expansion ratio that described decompressor can reach is larger, and the efficiency of LNG liquefaction process is higher, and refrigerant flow needed for kind of refrigeration cycle is lower.
Prior art has disclosed the gas deliquescence process based on the nitrogen expansion cycles utilizing two/tri-turbo-expanders in closed loop nitrogen kind of refrigeration cycle.Described nitrogen stream was just split into two/tri-strands of air-flows before utilizing two/tri-parallel expander, thus reached the different chilling temperature for natural gas liquefaction.The flow velocity adjusting the nitrogen stream of described shunting closely cooperates to make cooling curve, thus improves process efficiency.As shown in figure 12, a kind of natural gas liquefaction system with two decompressors of parallel organization in prior art is provided.Air inlet 101, inventiona gas treatment module 102, main low temperature heat exchanger 103, natural gas heat-exchange device 131, natural gas relief device 104, flash tank 105, LNG 106, flash gas heat-exchange device 132, flash gas compressor 107, flash gas aftercooler 108, fuel gas 109, first refrigeration compressor 111, first refrigeration aftercooler 112, second refrigeration compressor 113, second refrigeration aftercooler 114, first refrigeration secondary compressor 115, second refrigeration secondary compressor 117, 4th refrigeration aftercooler 118, first refrigeration heat-exchange device 133 and the second refrigeration heat-exchange device 134 similar to the corresponding assembly shown in Fig. 1 (hereafter describing in detail).First turbo-expander 119 and the second turbo-expander 120 are configured to parallel arranged, thus be two strands by the nitrogen flow point from described first refrigeration heat-exchange device 133, one is fed to described first turbo-expander 119, another stock enters described second turbo-expander 120, and the downstream substrates stream from two decompressors is directly back to described second refrigeration heat-exchange device 134.But the flow of the cooling substance in these processes is high.
Therefore, need in the art to develop a kind of natural gas liquefaction system and method with more high efficiency and less refrigeration flow.
Summary of the invention
An object of the present invention is to provide a kind of liquefied natural gas (LNG) production system with the refrigerating efficiency of improvement.
One aspect of the present invention provides a kind of liquefied natural gas (LNG) production system.In one embodiment, described liquefied natural gas (LNG) production system comprises main low temperature heat exchanger, natural gas liquid sub-systems, and refrigeration subsystem, this refrigeration subsystem comprises and is configured to arranged in series thus the multiple refrigeration compressors realizing cold-producing medium multi-stage compression, cool by multiple aftercoolers of the cold-producing medium compressed with each coupling of described multiple refrigeration compressor, be configured to cascaded structure with last aftercooler coupling thus realize described by the multiple turbo-expanders of the multiple expansion of cold-producing medium compressed, and with multiple refrigeration heat-exchange devices of first of described multiple refrigeration compressor and last coupling of described multiple turbo-expander, such all component forms a closed kind of refrigeration cycle, wherein, described main low temperature heat exchanger promotes the heat exchange the compressed natural gas through described natural gas liquid sub-systems and the cold-producing medium through described refrigeration subsystem, thus by the compressed natural gas of refrigerant liquefaction in natural gas liquid sub-systems in refrigeration subsystem.
In another embodiment of described liquefied natural gas (LNG) production system, described main low temperature heat exchanger is multi-flow heat exchanger.
In another embodiment of described liquefied natural gas (LNG) production system, described natural gas liquid sub-systems comprises inventiona gas treatment module, and it is applicable to being liquefied to make it for the treatment of compressed natural gas; Natural gas heat-exchange device, itself and described inventiona gas treatment module are with (fluidly/gaseously) coupling of flowable state/gaseous state and arrange in described main low temperature heat exchanger, for make through compressed natural gas and the flow of refrigerant heat-shift of convection current; And natural gas relief device, itself and described natural gas heat-exchange device are with flowable state/gaseous state coupling, for controlling the described reduction from the pressure of the liquefied natural gas of the compression of natural gas heat-exchange device, thus the temperature of low-compression liquefied natural gas, the liquefied natural gas (yieldingLNG) produced and flash gas (flash gas) is fallen further.
In another embodiment of described liquefied natural gas (LNG) production system, described natural gas relief device is Joule-Thomson (J-T) valve, two-phase decompressor or liquid expander.
In another embodiment of described liquefied natural gas (LNG) production system, described refrigeration subsystem comprises the first refrigeration compressor, to freeze aftercooler with first of described first refrigeration compressor coupling, the second refrigeration compressor freezing aftercooler coupling with described first, to freeze aftercooler with second of described second refrigeration compressor coupling, to freeze secondary compressor with the described second first of aftercooler coupling of freezing, to freeze aftercooler with the described first the 3rd of secondary compressor coupling of freezing, to freeze secondary compressor with the described 3rd second of aftercooler coupling of freezing, to freeze aftercooler with the described second the 4th of secondary compressor coupling of freezing, arrangement in main low temperature heat exchanger and with the described 4th first the freezing heat-exchange device of cold-producing medium of freezing aftercooler coupling thus cooled compressed immediately, freeze heat-exchange device coupling with the first turbo-expander of the cold-producing medium of described compression of first expanding with first, with described first turbo-expander coupling with the second turbo-expander of the cold-producing medium first expanded described in reexpanding, and arrangement freezing heat-exchange device with second of described second turbo-expander and the first refrigeration compressor coupling in main low temperature heat exchanger.In the further embodiment of described liquefied natural gas (LNG) production system, described refrigeration subsystem is included in the 3rd refrigeration heat-exchange device of arrangement in described main low temperature heat exchanger further, the wherein said 3rd refrigeration upstream entrance of heat-exchange device and a lower exit coupling of described first turbo-expander, and the described 3rd refrigeration lower exit of heat-exchange device and a upstream entrance coupling of described second refrigeration compressor; And in operation, two strands with 30/70 to 60/40 ratio are split into by the cold-producing medium after described first turbo-expander expands, one (30-60% of whole stock) is introduced in described 3rd refrigeration heat-exchange device using as the cold flow in main low temperature heat exchanger, and another stock (40-70% of whole stock) is expanded further by described second turbo-expander, be then incorporated into described second refrigeration heat-exchange device using as the most cold flow for liquefied natural gas secondary cooling (sub-cooling).In another further embodiment of described liquefied natural gas (LNG) production system, described refrigeration subsystem is included in arrangement in main low temperature heat exchanger and cooling during rolling machine between described first and second turbo-expanders further.In another embodiment of described liquefied natural gas (LNG) production system, described refrigeration subsystem comprises the cooling during rolling machine be arranged in between one and described second turbo-expander of described first turbo-expander further.In a further embodiment of described liquefied natural gas (LNG) production system, described refrigeration subsystem comprises the 3rd expansion gear and the second cooling during rolling machine further, and the two is all arranged between described second turbo-expander and the second refrigeration heat-exchange device.Described first turbo-expander can be selected to provide two bursts of flow of refrigerant of separating, and one sends back to the 4th refrigeration heat-exchange device be arranged in described main low temperature heat exchanger, and another stock delivers to the second expansion gear by described first cooling during rolling machine.Described second turbo-expander can be selected to provide two bursts of flow of refrigerant of separating, and one sends back to the 5th refrigeration heat-exchange device be arranged in described main low temperature heat exchanger, and another stock delivers to the 3rd expansion gear by described second cooling during rolling machine.
Another aspect of the present invention is to provide and a kind ofly utilizes the single-phase gaseous refrigerant in closed loop to produce the method for liquefied natural gas.In one embodiment, the method comprises the main low temperature heat exchanger being provided in and heat exchange wherein occurs, there is provided and flow through this main low temperature heat exchanger to obtain the pressurized natural gas stream of liquefaction, and provide cold energy by refrigerating plant to described main low temperature heat exchanger, wherein, described refrigerating plant comprises and is configured to arranged in series thus the multiple refrigeration compressors realizing cold-producing medium multi-stage compression, cool by multiple aftercoolers of the cold-producing medium compressed with each coupling of described multiple refrigeration compressor, be configured to cascaded structure with last aftercooler coupling thus realize described by the multiple turbo-expanders of the multiple expansion of cold-producing medium compressed, and with multiple refrigeration heat-exchange devices of first of described multiple refrigeration compressor and last coupling of multiple turbo-expander, such all component forms a closed kind of refrigeration cycle.
Object of the present invention and beneficial effect become apparent by detailed description of the preferred embodiment in conjunction with the following drawings.
Accompanying drawing explanation
Describe according to the preferred embodiment of the present invention now with reference to accompanying drawing, wherein identical Reference numeral represents identical element.
Fig. 1 is the schematic diagram of display according to the liquefied natural gas (LNG) production system of an embodiment of the invention;
Fig. 2 is the schematic diagram of display liquefied natural gas (LNG) production system according to another implementation of the invention;
Fig. 3 shows the heat flow-temperature curve of the liquefied natural gas (LNG) production system shown in Fig. 2;
Fig. 4 is the schematic diagram of display liquefied natural gas (LNG) production system according to another implementation of the invention;
Fig. 5 shows the heat flow-temperature curve of the liquefied natural gas (LNG) production system shown in Fig. 4;
Fig. 6 is the schematic diagram of display liquefied natural gas (LNG) production system according to another implementation of the invention;
Fig. 7 shows the heat flow-temperature curve of the liquefied natural gas (LNG) production system shown in Fig. 6;
Fig. 8 is the schematic diagram of display liquefied natural gas (LNG) production system according to another implementation of the invention;
Fig. 9 is the schematic diagram of display liquefied natural gas (LNG) production system according to another implementation of the invention;
Figure 10 is the schematic diagram of display liquefied natural gas (LNG) production system according to another implementation of the invention;
Figure 11 is the schematic diagram of display liquefied natural gas (LNG) production system according to another implementation of the invention;
Figure 12 is the schematic diagram showing exemplary liquefied natural gas (LNG) production system of the prior art.
Detailed description of the invention
Detailed description by referring to following particular implementation of the present invention more easily can understand the present invention.
In this application, quoting publication part, disclosed in these publications, content is incorporated in the application by reference completely at this, thus more fully describes the situation of the application's association area.
The invention provides and a kind ofly utilize kind of refrigeration cycle based on decompressor to make the system and method for natural gas liquefaction in a simple and efficient manner.This system and method uses the turbo-expander of arranged in series, compared with known prior art processes, has simple and flexible, low refrigeration traffic demand, low thermal expansion demand to each decompressor, and the advantage of competitive efficiency and power consumption.
Referring now to Fig. 1, which provide a kind of liquefied natural gas (LNG) production system according to an embodiment of the invention.Described liquefied natural gas (LNG) production system 100 comprises main low temperature heat exchanger 3, natural gas liquid sub-systems, and refrigeration subsystem, wherein, described main low temperature heat exchanger 3 promotes the heat exchange the natural gas through described natural gas liquid sub-systems and the cold-producing medium through described refrigeration subsystem, thus by the natural gas in the refrigerant liquefaction natural gas liquid sub-systems in refrigeration subsystem.
Described main low temperature heat exchanger 3 is multi-flow heat exchangers, and it integrates the Heat transmission of hot and cold stream, and the cooling curve optimized and combined.
As shown in fig. 1, described natural gas liquid sub-systems comprises inventiona gas treatment module 2, and it guarantees that air inlet 1 is suitable for gas deliquescence process; Natural gas heat-exchange device 31, it arranges in described main low temperature heat exchanger 3, for make through natural gas and the cold-producing medium of convection current or other air-flows (such as, flash gas stream discussed below) heat-shift; Natural gas relief device 4 (such as, Joule-Thomson (J-T) valve, two-phase decompressor or liquid expander), it is for controlling the reduction of the pressure of the cooled natural gas from described natural gas heat-exchange device 31, with the temperature reducing natural gas further, the two-phase (gas and liquid) of output flows; And flash tank 5, it is for being split into liquefied natural gas 6 and flash gas by described two phase flow.All component is by conventional pipeline/Flows state coupling: the lower exit of inventiona gas treatment module 2 described in 2/31 pipeline coupling and the upstream entrance of described natural gas heat-exchange device 31; The lower exit of natural gas heat-exchange device 31 described in 31/4 pipeline coupling and the upstream entrance of described J-T valve 4, and the lower exit of J-T valve 4 described in 4/5 pipeline coupling and the upstream entrance of described flash tank 5.Described liquefied natural gas 6 utilizes conventional equipment to store.For flash gas, described natural gas liquid sub-systems comprises flash gas heat-exchange device 32 further, and it is arranged in described main low temperature heat exchanger 3, for utilizing the natural gas that flows through described natural gas heat-exchange device 31 and regenerating cold energy; Flash gas compressor 7, it is for compressing the flash gas of cold energy regeneration; And flash gas aftercooler 8, its flash gas for cooled compressed is with output fuel gas 9.With assembly described in the pipeline of routine/Flows state/gaseous state coupling: the lower exit of flash tank 5 described in 5/32 pipeline coupling and the upstream entrance of described flash gas heat-exchange device 32; The lower exit of flash gas heat-exchange device 32 described in 32/7 pipeline coupling and the upstream entrance of described flash gas compressor 7; And 7/8 flash gas compressor 7 described in pipeline coupling lower exit and described flash gas aftercooler 8.
Air inlet 1 from external source is usual with certain pressure (being generally 20-60barg), and processes to remove CO in described inventiona gas treatment module 2
2, dehydration and the removal of mercury.Under the cryogenic temperature of liquefied natural gas, CO
2freezing of main low temperature heat exchanger can be caused with the existence of water.After gas treatment, need CO
2outflow concentration <50ppm, H
2the outflow concentration <1ppm of O.H
2s and Hg can cause aluminum bronze welding plate sheet heat exchanger (aluminum brazed plate fin heat exchanger), the i.e. corrosion of main low temperature heat exchanger 3, therefore, before liquefaction process, also need to remove Hg to <10ng/Sm in described inventiona gas treatment module 2
3, H
2s removes to <2ppm.
In the operation of described natural gas liquefaction system, through the high-pressure natural gas after gas treatment through the natural gas heat-exchange device 31 be arranged in described main low temperature heat exchanger 3, be liquefied herein.The highly pressurised liquid of being discharged by main low temperature heat exchanger 3 is through J-T valve 4 thus make Pressure Drop be low to moderate ~ 1.2 bar.The reduction of the pressure of described high-pressure spray makes temperature drop to about-161 DEG C and form two-phase flow, in described flash tank 5, be further separated into gas and liquid.Liquid is liquefied natural gas product, and is transferred to liquefied natural gas storage tanks.Flash gas is regenerated by the cold energy in described main low temperature heat exchanger 3.Described cold flash gas is being further compressed as a part for cold-producing medium and in described main low temperature heat exchanger 3, is regenerating cold energy before being used as fuel gas.
In theory, described refrigeration subsystem comprises multiplely carries out the refrigeration compressor of multi-stage compression, multiple aftercooler, multiple turbo-expander carrying out multiple expansion, and multiple refrigeration heat-exchange device, wherein all component is with cascaded structure coupling, thus forms closed kind of refrigeration cycle.Described " multiple " refer to two or more in the present invention.As shown in fig. 1, first refrigeration compressor 11, first aftercooler 12, second refrigeration compressor 13, second freeze secondary compressor 15, the 3rd refrigeration aftercooler 16, second of aftercooler 14, first that freeze that freeze freezes the first refrigeration heat-exchange device 33, first turbo-expander 19, second turbo-expander 20 of secondary compressor 17, the 4th refrigeration aftercooler 18, arrangement described main low temperature heat exchanger 3 in, and arrange described main low temperature heat exchanger 3 in second freezes heat-exchange device 34.All these assemblies pass through the conventional continuous coupling of pipeline/pipeline to form closed refrigerating ring; The second refrigeration lower exit of heat-exchange device 34 and the upstream entrance of described first refrigeration compressor 11 described in 34/11 pipeline coupling; The lower exit of the first refrigeration compressor 11 described in 11/12 pipeline coupling and the upstream entrance of described first refrigeration aftercooler 12; The first refrigeration lower exit of aftercooler 12 and the upstream entrance of described second refrigeration compressor 13 described in 12/13 pipeline coupling; The lower exit of the second refrigeration compressor 13 described in 13/14 pipeline coupling and the upstream entrance of described second refrigeration aftercooler 14; The lower exit of the second refrigeration aftercooler 14 described in 14/15 pipeline coupling and the upstream entrance of described first refrigeration secondary compressor 15; The lower exit of the first refrigeration secondary compressor 15 described in 15/16 pipeline coupling and the upstream entrance of described 3rd refrigeration aftercooler 16; The lower exit of the 3rd refrigeration aftercooler 16 described in 16/17 pipeline coupling and the upstream entrance of described second refrigeration secondary compressor 17; Described in 17/18 pipeline coupling second refrigeration secondary compressor 17 lower exit and described 4th refrigeration aftercooler 18 upstream entrance; The lower exit of the 4th refrigeration aftercooler 18 described in 18/33 pipeline coupling and the upstream entrance of described first refrigeration heat-exchange device 33; The first refrigeration lower exit of heat-exchange device 33 and the upstream entrance of described first turbo-expander 19 described in 33/19 pipeline coupling; The lower exit of the first turbo-expander 19 described in 19/20 pipeline coupling and the upstream entrance of described second turbo-expander 20; And 20,/34 second turbo-expander 20 described in pipeline coupling lower exit and the upstream entrance of described second refrigeration heat-exchange device 34.Preferred cold-producing medium is nitrogen (N
2).Described first and second refrigeration compressors 11,13 can utilize motor, internal combustion engine or combustion gas turbine to drive, and described first and second secondary compressor 15,17 utilize the described second and first turbo-expander 20,19 to drive respectively.Described aftercooler is typical air cooling machine or water chiller, and according to environmental condition by the refrigerant cools of described compression extremely, such as, the temperature of ~ 40 DEG C.
In the operation of described refrigeration subsystem, the cold-producing medium of discharging from the lower exit of described second refrigeration heat-exchange device 34 has low pressure (typically being 6 bar); First described low pressure refrigerant is compressed into ~ 50 bar by the first and second refrigeration compressors 11,13, is then compressed into 90-100 bar further by described first and second secondary compressor 15,17.The downstream of each described refrigeration compressor and secondary compressor is respectively by four aftercoolers 12,14,16, and a cooling in 18 is to reach the temperature according to environmental condition.High-pressure refrigerant from described 4th aftercooler 18 lower exit flows to the first refrigeration heat-exchange device 33 into arrangement in described main low temperature heat exchanger 3, thus be cooled to middle temperature, typically be ~-27 DEG C, then enter the first turbo-expander 19 being expanded to ~ pressure of 24 bar, then enter the second turbo-expander 20 to reach to ~ 7 bar to reduce pressure ~ the temperature of-153 DEG C.Flow of refrigerant from the cryogenic temperature of described second turbo-expander 20 lower exit enters the second refrigeration heat-exchange device 34 of arrangement in described main low temperature heat exchanger 3, and provides main cold energy with liquefied natural gas.In described main low temperature heat exchanger 3 after freezing regeneration, described flow of refrigerant flows into described first refrigeration compressor 11 again, and again circulates in closed refrigerating ring.
Referring now to Fig. 2, which provide a kind of liquefied natural gas (LNG) production system according to another implementation of the invention.In order to the feature of this embodiment outstanding, when not necessary, the description with the similar features shown in Fig. 1 will be omitted.Described refrigeration subsystem is included in the 3rd refrigeration heat-exchange device 35 of arrangement in described main low temperature heat exchanger 3 further.The upstream entrance of described 3rd refrigeration heat-exchange device 35 passes through a lower exit coupling of 19/35 pipeline and described first turbo-expander 19, and the lower exit of described 3rd refrigeration heat-exchange device 35 passes through the upstream entrance coupling of 35/13 pipeline and described second refrigeration compressor 13 simultaneously.In operation, cold-producing medium after being expanded by the first turbo-expander 19 is split into two strands with 30/70 to 60/40 ratio, one (30-60% of whole stock) is introduced in described 3rd refrigeration heat-exchange device 35 using as the cold flow in main low temperature heat exchanger 3, and another stock (40-70% of whole stock) is expanded further by described second turbo-expander 20, be then incorporated into described second refrigeration heat-exchange device 34 using the most cold flow of the secondary cooling as the liquefied natural gas for pressurizeing.Because the condensation in medium temperature needs more cold energy than the secondary cooling of natural gas at low temperatures, the shunting after described first turbo-expander 19 can distribute cold energy by the heat needed for natural gas liquefaction better.Because the temperature difference between hot and cold stream is flatly close along heat flow as shown in Figure 3, the change of this process to natural gas feed pressure therefore in Fig. 2 is flexibly.When tapped downstream after described first turbo-expander, effective/specific energy requirement in the process described in FIG improves 15-20%.
Referring now to Fig. 4, which provide a kind of liquefied natural gas (LNG) production system according to another implementation of the invention.In order to the feature of this embodiment outstanding, when not necessary, the description with the similar features shown in Fig. 1 will be omitted.Described refrigeration subsystem is included in described first and second turbo-expanders 19 further, the cooling during rolling machine 36 of arrangement between 20.The upstream entrance of described cooling during rolling machine 36 passes through the lower exit coupling of 19/36 pipeline and described first turbo-expander 19, and the upstream entrance coupling of the lower exit of described cooling during rolling machine 36 and described second turbo-expander 20.High-pressure refrigerant stream from described first turbo-expander 19 lower exit was expanded to before entering cooling during rolling machine 36 ~ pressure of 24 bar being cooled to further ~-136 DEG C, then enter the second turbo-expander 20 being decompressed to ~ temperature of 15 bar reaching ~-153 DEG C.The downstream of this second turbo-expander 20 is passed described main low temperature heat exchanger 3 at cryogenic temperatures and provides main cold energy with liquefied natural gas.After the cold energy regeneration of described main low temperature heat exchanger 3, described flow of refrigerant flows into the first refrigeration compressor 11 again, and again circulates in described closed refrigerating ring.Fig. 5 shows the cooling curve of the system described above shown in Fig. 4.When having cooling during rolling machine between described first and second decompressors, effective/specific energy requirement in the system described in FIG and process improves 8-10%.
Referring now to Fig. 6, which provide a kind of liquefied natural gas (LNG) production system according to another implementation of the invention.In order to the feature of this embodiment outstanding, when not necessary, the description with the similar features shown in Fig. 1,2 and 4 will be omitted.In described refrigeration subsystem, the cold-producing medium from described first turbo-expander 19 is split into two strands.Then described cooling during rolling machine 36 by 37/20 conduit arrangements between one and described second turbo-expander 20 from described first turbo-expander 19.In operation, described high-pressure refrigerant stream was cooled to medium temperature before entering described first turbo-expander 19, such as, and ~-32 DEG C, and being expanded to by splitting into before two strands ~ pressure of 30 bar.One cooling during rolling machine 37 again entering in described main low temperature heat exchanger 3 arrangement being cooled to further ~-111 DEG C, then enter described second turbo-expander 20 to reduce the temperature of pressure extremely ~ 10 bar reaching ~-153 DEG C.The downstream of this decompressor 20 is through main low temperature heat exchanger 3 and provide the main cold energy of low temperature thus liquefied natural gas.The stream that another strand separates from decompressor 19 downstream directly passes main low temperature heat exchanger 3 thus provides the cold energy of high temperature with liquefied natural gas.After cold energy regeneration in described main low temperature heat exchanger 3, two bursts of flow of refrigerant flow into described first and second refrigeration compressors 11,13 respectively, and again circulate in closed refrigerating ring.Refrigerant branches after described first turbo-expander more contributes to the heat flow of assignment system cryogen between warm cold temperature, thus mates better and going overheated, condensation and the natural gas in the secondary cooling stage by the heat demand being warmed to cold temperature.Compared with the process in Fig. 4, the process in Fig. 6 has the reduction of the improved efficiency of further 5-7% and the refrigerant flow of 2-5%.In Fig. 6, the cooling curve of above process as shown in Figure 7.
Referring now to Fig. 8, which provide a kind of liquefied natural gas (LNG) production system according to another implementation of the invention.In order to the feature of this embodiment outstanding, when not necessary, the description with the similar features shown in Fig. 1,2,4 and 6 will be omitted.In described refrigeration subsystem, the cold-producing medium from described second turbo-expander 20 is split into two strands.Described refrigeration subsystem be included in further described second refrigeration compressor 13 and described first refrigeration secondary compressor 15 between arrangement the 3rd refrigeration compressor 22 and the 5th refrigeration aftercooler 23, for receive from described second turbo-expander 20 the one the 5th refrigeration heat-exchange device 38, for receive from described second turbo-expander 20 another strand the 6th refrigeration heat-exchange device 39, and the described 6th and second refrigeration heat-exchange device 39, between 34 arrangement for periods of low pressure expand the 2nd J-T valve.
Referring now to Fig. 9, which provide a kind of liquefied natural gas (LNG) production system according to another implementation of the invention.In order to the feature of this embodiment outstanding, when not necessary, the description with the similar features shown in Fig. 1,2,4,6 and 8 will be omitted.Compared with Fig. 8, described refrigeration subsystem comprises the 3rd secondary compressor 26 with aftercooler 25 further, and replaces the 3rd turbo-expander 24 of described 2nd J-T valve.
Fig. 8,9,10 and 11 shows use three grades of expansion process, thus provides three strands of cold flows for the embodiment of the liquefaction supply cold energy to natural gas.Described refrigeration subsystem is included in the cooling during rolling machine arranged between one and described second turbo-expander from described first turbo-expander, and the second cooling during rolling machine arranged between one and described 3rd decompressor from described second turbo-expander.As shown in Fig. 8,9 and 11, the downstream of described second decompressor 20 can be selected to be split into two strands before being expanded by the 3rd expansion gear 21 or 24 further, and one is natural gas cooling as cold flow, and another strand is then cooled to lower temperature further.As shown in figs, the downstream of described first decompressor 19 also can be selected to be split into two strands before being expanded by the second decompressor 20 further, and one is natural gas cooling as cold flow, and another strand is then further cooled to lower temperature.Described three grades of whole pressure expansions expanded compare at about 12-15, higher than the double expansion in the process described in Fig. 4 and 6.When the expansion ratio increased, compared with the process in Fig. 6, process efficiency can improve 4-8% further, and refrigerant flow reduces 30-40%.
Process new above has the following advantages:
Compared with single decompressor, two nitrogen expansion machine allowable temperatures of series connection are close more closely, correspondingly concerning specific power consumption, have large improvement in efficiency.
Compared with single expansion process, two decompressors of cascaded structure make the expansion ratio of each decompressor minimize.Such as attempting reaching in the liquefied natural gas (LNG) production rate with 9% flash gas generation, two N of arranged in series
2be <4 to the expansion ratio of each expansion process in expansion cycles, and in single expansion process, need the expansion ratio of 9.4.In addition, end user can be made simply commercially to obtain decompressor like a cork, the particularly decompressor of low capacity and power consumption.
Two decompressors of arranged in series have the flexibility of adaptation scheme, and do not generate flash gas in liquefied natural gas (LNG) production while, in main low temperature heat exchanger, still holding temperature is close is no more than 30 DEG C, that is, the requirement of widely used ALPEMA standard.
If needed, in order to produce the liquefied natural gas of the amount containing different flash gas, by adjustment low pressure (second) decompressor flow and the expansion ratio for the cooling of liquefied natural gas, thus the cold N needed for controlling flexibly
2temperature.
Such as, in fig. 2, the flow of 19/35 reduces the inlet flow rate that can increase by the second decompressor 20, thus can increase expansion ratio to reach lower outlet temperature, and its further liquefied natural gas is to lower temperature and be reduced in the amount of the flash gas after J-T expands.
Application the present invention, such as, as shown in Figure 2, according to external condition and inlet air conditions, for typically gas source, the two N of shunting of arranged in series
2expander cycle can realize the energy efficiency of the calculating of about 0.35-0.50kWh/kg.
The performance data of liquefied natural gas process under the environment temperature of table 1. ~ 30 DEG C and the admission pressure of 40barg
When describing of the present invention with reference to detailed description of the invention, should be understood that this embodiment is exemplary, not limiting the scope of the invention.For those those of ordinary skill of association area of the present invention, alternate embodiments of the present invention will be apparent.Such alternate embodiments is believed to comprise within the scope of the present invention.Correspondingly, scope of the present invention is determined by additional claim, and is supported by above description.
Claims (19)
1. liquefied natural gas (LNG) production system, comprising:
Main low temperature heat exchanger;
Natural gas liquid sub-systems; And
Refrigeration subsystem, comprise be configured to arranged in series thus realize cold-producing medium multi-stage compression multiple refrigeration compressors, cool by multiple aftercoolers of the cold-producing medium compressed, and last aftercooler coupling be configured to cascaded structure thus realize described by the multiple turbo-expanders of cold-producing medium multiple expansion compressed with each coupling of described multiple refrigeration compressor, and with multiple refrigeration heat-exchange devices of first of described multiple refrigeration compressor and last coupling of multiple turbo-expander, thus, all component forms closed kind of refrigeration cycle;
Wherein, described main low temperature heat exchanger promotes the heat exchange the compressed natural gas through described natural gas liquid sub-systems and the cold-producing medium through described refrigeration subsystem, thus by the compressed natural gas in the refrigerant liquefaction natural gas liquid sub-systems in refrigeration subsystem.
2. liquefied natural gas (LNG) production system according to claim 1, wherein, described main low temperature heat exchanger is multi-flow heat exchanger.
3. liquefied natural gas (LNG) production system according to claim 1, wherein, described natural gas liquid sub-systems comprises:
Inventiona gas treatment module, is applicable to being liquefied to make it for the treatment of compressed natural gas;
Natural gas heat-exchange device, arranges with described inventiona gas treatment module flowable state/gaseous state coupling in described main low temperature heat exchanger, for make through compressed natural gas and the flow of refrigerant heat-shift of convection current; And
Natural gas relief device, with described natural gas heat-exchange device flowable state/gaseous state coupling, for controlling the described reduction from the pressure of the compressed natural gas of the cooling of natural gas heat-exchange device, thus low-compression liquefied natural gas, the liquefied natural gas of output and the temperature of flash gas are fallen further.
4. liquefied natural gas (LNG) production system according to claim 3, wherein, described natural gas relief device is Joule-Thomson (J-T) valve, two-phase decompressor or liquid expander.
5. liquefied natural gas (LNG) production system according to claim 1, wherein, described refrigeration subsystem comprises:
First refrigeration compressor;
To freeze aftercooler with first of described first refrigeration compressor coupling;
The second refrigeration compressor freezing aftercooler coupling with described first;
To freeze aftercooler with second of described second refrigeration compressor coupling;
To freeze secondary compressor with the described second first of aftercooler coupling of freezing;
To freeze aftercooler with the described first the 3rd of secondary compressor coupling of freezing;
To freeze secondary compressor with the described 3rd second of aftercooler coupling of freezing;
To freeze aftercooler with the described second the 4th of secondary compressor coupling of freezing;
Arrangement in main low temperature heat exchanger also to be freezed aftercooler coupling thus first of cooled compressed cold-producing medium to freeze heat-exchange device immediately with the described 4th;
Freeze heat-exchange device coupling with the first turbo-expander of the described compressed refrigerant that first expands with first;
With described first turbo-expander coupling with the second turbo-expander of the cold-producing medium first expanded described in reexpanding; And
Arrangement in main low temperature heat exchanger also to be freezed heat-exchange device with second of described second turbo-expander and the first refrigeration compressor coupling.
6. liquefied natural gas (LNG) production system according to claim 5, wherein, described refrigeration subsystem is included in the 3rd refrigeration heat-exchange device of arrangement in described main low temperature heat exchanger further, the wherein said 3rd refrigeration upstream entrance of heat-exchange device and a lower exit coupling of described first turbo-expander, and the described 3rd refrigeration lower exit of heat-exchange device and a upstream entrance coupling of described second refrigeration compressor; And in operation, two strands with 30/70 to 60/40 ratio are split into by the cold-producing medium after described first turbo-expander expands, one (30-60% of whole stock) is introduced in described 3rd refrigeration heat-exchange device using as the cold flow in main low temperature heat exchanger, and another stock (40-70% of whole stock) is expanded further by described second turbo-expander, be then incorporated into described second refrigeration heat-exchange device using as the most cold flow for liquefied natural gas secondary cooling.
7. liquefied natural gas (LNG) production system according to claim 5, wherein, described refrigeration subsystem is included in arrangement in main low temperature heat exchanger and cooling during rolling machine between described first and second turbo-expanders further.
8. liquefied natural gas (LNG) production system according to claim 6, wherein, described refrigeration subsystem is included in arrangement in main low temperature heat exchanger and cooling during rolling machine between one and described second turbo-expander from described first turbo-expander further.
9. liquefied natural gas (LNG) production system according to claim 7, wherein, described refrigeration subsystem comprises the 3rd expansion gear and the second cooling during rolling machine further, the two is all arranged between described second turbo-expander and the second refrigeration heat-exchange device, and described second turbo-expander provides one by described second cooling during rolling machine to described 3rd expansion gear.
10. liquefied natural gas (LNG) production system according to claim 7, wherein, described refrigeration subsystem comprises the 3rd expansion gear and the second cooling during rolling machine further, and the two is all arranged between described second turbo-expander and the second refrigeration heat-exchange device; And described second turbo-expander provides the flow of refrigerant of two stock streams, one sends the 5th refrigeration heat-exchange device be arranged in described main low temperature heat exchanger back to, and another stock delivers to the 3rd expansion gear by described second cooling during rolling machine.
11. liquefied natural gas (LNG) production systems according to claim 8, wherein, described refrigeration subsystem comprises the 3rd expansion gear and the second cooling during rolling machine further, and the two is all arranged between described second turbo-expander and the second refrigeration heat-exchange device; And described second turbo-expander provides the flow of refrigerant of two stock streams, one sends the 5th refrigeration heat-exchange device be arranged in described main low temperature heat exchanger back to, and another stock delivers to the 3rd expansion gear by described second cooling during rolling machine.
12. 1 kinds utilize the single-phase gaseous refrigerant in closed loop to produce the method for liquefied natural gas, comprising:
Be provided in the main low temperature heat exchanger that heat exchange wherein occurs;
There is provided and flow through this main low temperature heat exchanger to obtain the pressurized natural gas stream of liquefaction; And
Cold energy is provided to described main low temperature heat exchanger by refrigerating plant, wherein, described refrigerating plant comprises and is configured to arranged in series thus the multiple refrigeration compressors realizing cold-producing medium multi-stage compression, cool by multiple aftercoolers of the cold-producing medium compressed with each coupling of described multiple refrigeration compressor, be configured to cascaded structure with last aftercooler coupling thus realize described by the multiple turbo-expanders of cold-producing medium multiple expansion compressed, and with multiple refrigeration heat-exchange devices of first of described multiple refrigeration compressor and last coupling of multiple turbo-expander, such all component forms a closed kind of refrigeration cycle.
13. methods according to claim 12, wherein, described refrigerating plant comprises:
First refrigeration compressor;
To freeze aftercooler with first of described first refrigeration compressor coupling;
The second refrigeration compressor freezing aftercooler coupling with described first;
To freeze aftercooler with second of described second refrigeration compressor coupling;
To freeze secondary compressor with the described second first of aftercooler coupling of freezing;
To freeze aftercooler with the described first the 3rd of secondary compressor coupling of freezing;
To freeze secondary compressor with the described 3rd second of aftercooler coupling of freezing;
To freeze aftercooler with the described second the 4th of secondary compressor coupling of freezing;
Arrangement in main low temperature heat exchanger also to be freezed aftercooler coupling thus first of cooled compressed cold-producing medium to freeze heat-exchange device immediately with the described 4th;
Freeze heat-exchange device coupling with the first turbo-expander of the described compressed refrigerant that first expands with first;
With described first turbo-expander coupling with the second turbo-expander of the cold-producing medium first expanded described in reexpanding; And
Arrangement in main low temperature heat exchanger also to be freezed heat-exchange device with second of described second turbo-expander and the first refrigeration compressor coupling.
14. methods according to claim 13, wherein, described refrigerating plant is included in the 3rd refrigeration heat-exchange device of arrangement in described main low temperature heat exchanger further, the wherein said 3rd refrigeration upstream entrance of heat-exchange device and a lower exit coupling of described first turbo-expander, and the described 3rd refrigeration lower exit of heat-exchange device and a upstream entrance coupling of described second refrigeration compressor; And in operation, two strands with 30/70 to 60/40 ratio are split into by the cold-producing medium after described first turbo-expander expands, one (30-60% of whole stock) is introduced in described 3rd refrigeration heat-exchange device using as the cold flow in main low temperature heat exchanger, and another stock (40-70% of whole stock) is expanded further by described second turbo-expander, be then incorporated into described second refrigeration heat-exchange device using as the most cold flow for liquefied natural gas secondary cooling.
15. methods according to claim 13, wherein, described refrigerating plant is included in arrangement in main low temperature heat exchanger and cooling during rolling machine between described first and second turbo-expanders further.
16. methods according to claim 14, wherein, described refrigerating plant is included in arrangement in main low temperature heat exchanger and cooling during rolling machine between one and described second turbo-expander from described first turbo-expander further.
17. methods according to claim 15, wherein, described refrigerating plant comprises the 3rd expansion gear and the second cooling during rolling machine further, the two is all arranged between described second turbo-expander and the second refrigeration heat-exchange device, and described second turbo-expander provides one by described second cooling during rolling machine to described 3rd expansion gear.
18. methods according to claim 15, wherein, described refrigeration subsystem comprises the 3rd expansion gear and the second cooling during rolling machine further, and the two is all arranged between described second turbo-expander and the second refrigeration heat-exchange device; And described second turbo-expander provides the flow of refrigerant of two stock streams, one sends the 5th refrigeration heat-exchange device be arranged in described main low temperature heat exchanger back to, and another stock delivers to the 3rd expansion gear by described second cooling during rolling machine.
19. methods according to claim 16, wherein, described refrigeration subsystem comprises the 3rd expansion gear and the second cooling during rolling machine further, and the two is all arranged between described second turbo-expander and the second refrigeration heat-exchange device; And described second turbo-expander provides the flow of refrigerant of two stock streams, one sends the 5th refrigeration heat-exchange device be arranged in described main low temperature heat exchanger back to, and another stock delivers to the 3rd expansion gear by described second cooling during rolling machine.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/SG2012/000327 WO2014039008A1 (en) | 2012-09-07 | 2012-09-07 | System and method for natural gas liquefaction |
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| CN104520660B CN104520660B (en) | 2017-04-26 |
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| US (1) | US20150204603A1 (en) |
| EP (1) | EP2893275A1 (en) |
| CN (1) | CN104520660B (en) |
| BR (1) | BR112015002174A2 (en) |
| MX (1) | MX2014014750A (en) |
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| CN107762630B (en) * | 2016-08-23 | 2020-10-23 | 通用电气航空***有限责任公司 | Method for pre-cooling an environmental control system using a turbomachine and aircraft |
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| TWI712769B (en) * | 2017-11-21 | 2020-12-11 | 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 | Bog recondenser and lng supply system provided with same |
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| CN115711360A (en) * | 2022-11-15 | 2023-02-24 | 中国船舶集团有限公司第七一一研究所 | Cryogenic type boil-off gas reliquefaction system |
| CN115711360B (en) * | 2022-11-15 | 2023-12-08 | 中国船舶集团有限公司第七一一研究所 | Deep cooling type evaporation gas reliquefaction system |
Also Published As
| Publication number | Publication date |
|---|---|
| MX2014014750A (en) | 2015-04-13 |
| US20150204603A1 (en) | 2015-07-23 |
| CN104520660B (en) | 2017-04-26 |
| EP2893275A1 (en) | 2015-07-15 |
| SG11201503594SA (en) | 2015-06-29 |
| WO2014039008A1 (en) | 2014-03-13 |
| BR112015002174A2 (en) | 2017-07-04 |
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