TWI746977B - Gas liquefaction method and gas liquefaction device - Google Patents
Gas liquefaction method and gas liquefaction device Download PDFInfo
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- TWI746977B TWI746977B TW108116444A TW108116444A TWI746977B TW I746977 B TWI746977 B TW I746977B TW 108116444 A TW108116444 A TW 108116444A TW 108116444 A TW108116444 A TW 108116444A TW I746977 B TWI746977 B TW I746977B
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- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 454
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 163
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 94
- 239000007788 liquid Substances 0.000 claims abstract description 68
- 239000003345 natural gas Substances 0.000 claims abstract description 47
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 238000001816 cooling Methods 0.000 claims description 64
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 43
- 230000006835 compression Effects 0.000 claims description 35
- 238000007906 compression Methods 0.000 claims description 35
- 230000008016 vaporization Effects 0.000 claims description 35
- 229910052757 nitrogen Inorganic materials 0.000 claims description 21
- 239000012071 phase Substances 0.000 claims description 11
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 7
- 238000004781 supercooling Methods 0.000 claims description 6
- 229910052786 argon Inorganic materials 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 230000006837 decompression Effects 0.000 claims description 4
- 238000009795 derivation Methods 0.000 claims description 2
- 238000009834 vaporization Methods 0.000 description 34
- 238000010586 diagram Methods 0.000 description 10
- 238000002309 gasification Methods 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
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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
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/0015—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
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. air
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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
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/0017—Oxygen
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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
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/002—Argon
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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
- F25J1/003—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
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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
- F25J1/003—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"
- F25J1/0045—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 vaporising a liquid return stream
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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
- F25J1/0221—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 the cold stored in an external cryogenic component in an open refrigeration loop
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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
- F25J1/0221—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 the cold stored in an external cryogenic component in an open refrigeration loop
- F25J1/0224—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 the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration loop
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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.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
Abstract
Description
本發明係關於一種氣體液化裝置及氣體液化方法，尤其關於一種於利用液化天然氣之汽化熱之氮氣液化裝置，高效率地獲得液態氮之氣體液化裝置及氣體液化方法。The present invention relates to a gas liquefaction device and a gas liquefaction method, in particular to a nitrogen liquefaction device using the vaporization heat of liquefied natural gas, and a gas liquefaction device and a gas liquefaction method for efficiently obtaining liquid nitrogen.
天然氣（natural gas，NG）由於輸送或儲藏之便利性等，而作為液化天然氣（liquefied natural gas，LNG）來儲藏，將其氣化後，主要用作火力發電用途或城鎮氣體燃料用途。因此，開發出有效利用氣化時所獲得之LNG之汽化熱的技術。Natural gas (NG) is stored as liquefied natural gas (LNG) due to the convenience of transportation or storage. After gasification, it is mainly used for thermal power generation or urban gas fuel use. Therefore, a technology to effectively utilize the heat of vaporization of LNG obtained during gasification has been developed.
作為利用LNG之汽化熱而將氮氣等進行液化之設備，通常使用如下製程：將氮氣以壓縮機進行壓縮，接著利用熱交換器而使其與LNG進行熱交換，使LNG升溫氣化，並且將氮氣液化。 例如專利文獻1揭示有如下方法：利用使LNG蒸發時所吸收之汽化熱，將由壓縮機所壓縮之高壓氮氣於熱交換器冷卻，接著利用減壓閥使其減壓，藉此獲得液態氮。 [現有技術文獻] [專利文獻]As equipment for liquefying nitrogen and the like using the heat of vaporization of LNG, the following process is usually used: the nitrogen is compressed by a compressor, and then heat exchanged with the LNG by a heat exchanger, the LNG is heated up and vaporized, and the Nitrogen is liquefied. For example, Patent Document 1 discloses a method of using vaporization heat absorbed when LNG is evaporated, cooling high-pressure nitrogen compressed by a compressor in a heat exchanger, and then using a pressure reducing valve to depressurize, thereby obtaining liquid nitrogen. [Prior Art Literature] [Patent Literature]
[專利文獻1]日本特開平2005-164150號公報[Patent Document 1] Japanese Patent Laid-Open No. 2005-164150
[發明所欲解決之問題][The problem to be solved by the invention]
如專利文獻1所揭示之氮氣之液化方法，將氮氣液化之液化能力仰賴於對熱交換器供給之LNG之溫度。即，供給至熱交換器之LNG溫度愈低，配置於熱交換器之後段的減壓閥之液化量愈多。相反，若LNG溫度愈高，則液化量減少。 液化量減少，意指於減壓閥將氮氣減壓時所產生之氮氣量增加。由於減壓時所產生之氮氣為低壓，故而需要再次壓縮而再循環使用，或有必要釋放，因此於LNG溫度高之情形時，氮氣之液化的效率較差。As disclosed in Patent Document 1, the liquefaction ability of the nitrogen liquefaction depends on the temperature of the LNG supplied to the heat exchanger. That is, the lower the temperature of the LNG supplied to the heat exchanger, the greater the liquefaction amount of the pressure reducing valve arranged at the rear stage of the heat exchanger. Conversely, if the LNG temperature is higher, the amount of liquefaction decreases. The decrease in the amount of liquefaction means that the amount of nitrogen generated when the pressure reducing valve reduces the pressure of the nitrogen increases. Since the nitrogen generated during decompression is at a low pressure, it needs to be compressed again for recycling, or it is necessary to release. Therefore, when the temperature of LNG is high, the efficiency of nitrogen liquefaction is poor.
另一方面，近年來伴隨著天然氣渦輪機之效率化，而有所使用之天然氣之壓力升高之傾向。因此，以更高之壓力使LNG蒸發之必要性增加。 為了獲得較高的天然氣壓力，通常使儲存於儲槽之LNG以泵升壓後使其蒸發。但是，若將LNG以泵升壓，則藉由來自泵之熱輸入，LNG溫度上升。因此，使LNG升壓至較高之壓力，會提高LNG溫度。其結果為，存在利用LNG之汽化熱的氮氣之液化效率下降之問題。On the other hand, in recent years, along with the efficiency of natural gas turbines, the pressure of natural gas used has tended to increase. Therefore, the necessity of evaporating LNG at a higher pressure has increased. In order to obtain a higher natural gas pressure, the LNG stored in the storage tank is usually pumped up to evaporate. However, if the LNG is boosted by a pump, the temperature of the LNG rises due to the heat input from the pump. Therefore, increasing the pressure of LNG to a higher pressure will increase the temperature of LNG. As a result, there is a problem that the liquefaction efficiency of nitrogen using the heat of vaporization of LNG decreases.
鑒於上述實情，本發明目的為提供一種於利用液化天然氣之汽化熱而將饋入氣體高效率地液化之裝置，可供給高壓力之天然氣之氣體液化裝置及使用該裝置之氣體液化方法。 [解決問題之手段]In view of the foregoing facts, the object of the present invention is to provide a device for efficiently liquefying the feed gas by using the heat of vaporization of liquefied natural gas, a gas liquefaction device capable of supplying high-pressure natural gas, and a gas liquefaction method using the device. [Means to Solve the Problem]
（發明1） 本發明之氣體液化方法包括： 第一升壓步驟，將液化天然氣升壓至第一壓力； 第二升壓步驟，將於上述第一升壓步驟升壓之液化天然氣導入主熱交換器後，升壓至高於上述第一壓力之第二壓力； 第一天然氣導出步驟，將於上述第二升壓步驟升壓之液化天然氣之至少一部分經由上述主熱交換器，作為天然氣而從上述主熱交換器導出； 饋入氣體壓縮步驟，將饋入氣體壓縮； 饋入氣體冷卻步驟，將於上述饋入氣體壓縮步驟壓縮之饋入氣體冷卻至第一溫度； 氣液分離步驟，將於上述饋入氣體冷卻步驟冷卻之饋入氣體減壓、冷卻後進行氣液分離；以及 液化饋入氣體導出步驟，將上述氣液分離步驟所獲得之液化饋入氣體以液體狀態導出；並且 上述饋入氣體冷卻步驟係於上述主熱交換器，藉由於上述第一升壓步驟升壓之液化天然氣以及於上述第二升壓步驟升壓之上述液化天然氣，與上述饋入氣體之間的熱交換，而將上述饋入氣體進行冷卻。(Invention 1) The gas liquefaction method of the present invention includes: The first boosting step, boosting the liquefied natural gas to the first pressure; In the second pressure increasing step, after the LNG boosted in the first pressure increasing step is introduced into the main heat exchanger, the pressure is increased to a second pressure higher than the first pressure; In the first natural gas deriving step, at least a part of the liquefied natural gas that will be boosted in the second boosting step is exported from the main heat exchanger as natural gas via the main heat exchanger; The feeding gas compression step, compressing the feeding gas; The feeding gas cooling step is to cool the feeding gas compressed in the feeding gas compression step to the first temperature; In the gas-liquid separation step, the gas-liquid separation is performed after decompression and cooling of the feed gas cooled in the above-mentioned feed gas cooling step; and The liquefaction feed gas deriving step is to derive the liquefied feed gas obtained in the above gas-liquid separation step in a liquid state; and The feeding gas cooling step is in the main heat exchanger, and the LNG boosted by the first boosting step and the LNG boosted in the second boosting step are separated from the feeding gas. Heat exchange, while cooling the above-mentioned feed gas.
依據上述方法，首先，於第一升壓步驟升壓至第一壓力之液化天然氣導入至主熱交換器之冷端，與饋入氣體進行熱交換。藉由該熱交換而升溫至既定溫度之液化天然氣從主熱交換器之中間部導出，於第二升壓步驟升壓至第二壓力，進一步升溫。升溫之液化天然氣再次返送至主熱交換器，藉由與饋入氣體之熱交換而吸收之汽化熱，從而氣化。According to the above method, first, the liquefied natural gas boosted to the first pressure in the first boosting step is introduced to the cold end of the main heat exchanger to exchange heat with the feed gas. The liquefied natural gas heated to a predetermined temperature by the heat exchange is led out from the middle part of the main heat exchanger, and is boosted to a second pressure in the second pressure boosting step, and the temperature is further increased. The heated liquefied natural gas is returned to the main heat exchanger again, and is vaporized by the heat of vaporization absorbed by the heat exchange with the feed gas.
藉由如上所述，設為將使液化天然氣升壓之步驟設為2階段之構成，則於必須供給高壓力（例如80 barA以上）之天然氣之情形時，可將導入至主熱交換器之冷端的液化天然氣之壓力抑制為較低。藉由降低於第一升壓步驟升壓之壓力（第一壓力），則與升壓之壓力較高之情形相比較，第一升壓步驟之液化天然氣之溫度上升減少。因此，主熱交換器可實施溫度較低之液化天然氣與饋入氣體之熱交換，饋入氣體之液化效率上升。As described above, the step of increasing the pressure of the liquefied natural gas is set to a two-stage configuration. When it is necessary to supply natural gas at a high pressure (for example, 80 barA or more), it can be introduced into the main heat exchanger. The pressure of the LNG at the cold end is suppressed to a lower level. By reducing the pressure boosted in the first boosting step (the first pressure), the temperature rise of the liquefied natural gas in the first boosting step is reduced compared with the case where the boosting pressure is higher. Therefore, the main heat exchanger can perform heat exchange between the lower temperature liquefied natural gas and the feed gas, and the liquefaction efficiency of the feed gas increases.
若於主熱交換器進行低溫之液化天然氣與饋入氣體之熱交換，吸收某種程度之液化天然氣之汽化熱後，於第二升壓步驟升壓至第二壓力，則可使該液化天然氣氣化而獲得較高壓力之氣體狀態之天然氣。If the heat exchange between low-temperature liquefied natural gas and the feed gas is carried out in the main heat exchanger, after absorbing a certain degree of vaporization heat of the liquefied natural gas, the pressure is increased to the second pressure in the second step-up step, the liquefied natural gas can be made It is gasified to obtain natural gas in a gas state of higher pressure.
進一步地，關於在第二升壓步驟溫度上升之液化天然氣，藉由返送至主熱交換器而使其汽化熱進一步被吸收，而可將液化天然氣之汽化熱用於饋入氣體之冷卻。如此一來，由於將比較低之壓力（第一壓力）下之液化天然氣之汽化熱、與比較高之壓力（第二壓力）下之液化天然氣之汽化熱分別用於饋入氣體之冷卻，故而可稱為熱效率高之饋入氣體之液化方法。Furthermore, regarding the LNG whose temperature rises in the second boosting step, the heat of vaporization is further absorbed by returning to the main heat exchanger, and the heat of vaporization of the LNG can be used for cooling the feed gas. In this way, since the heat of vaporization of liquefied natural gas at a relatively low pressure (first pressure) and the heat of vaporization of liquefied natural gas at a relatively high pressure (second pressure) are respectively used for cooling of the feed gas, It can be called a liquefaction method of feeding gas with high thermal efficiency.
（發明2） 本發明之氣體液化方法可進一步包含饋入氣體再循環步驟，使於氣液分離步驟進行氣液分離而獲得之氣體狀態之饋入氣體，與供給至上述饋入氣體壓縮步驟之饋入氣體匯流。(Invention 2) The gas liquefaction method of the present invention may further include a feeding gas recirculation step, so that the feeding gas in the gas state obtained by the gas-liquid separation step in the gas-liquid separation step merges with the feeding gas supplied to the above-mentioned feeding gas compression step .
於主熱交換器冷卻，且減壓冷卻之饋入氣體成為氣液混合狀態，被液化之液化饋入氣體作為製品而導出。 另一方面，未經液化且經冷卻之氣體狀態之饋入氣體係作為用以供給至再次壓縮步驟、及繼其之後之饋入氣體冷卻步驟之再循環饋入氣體而匯流於饋入氣體。 藉由將如上所述未液化之部分之饋入氣體進行再循環，可避免饋入氣體之損耗。It is cooled in the main heat exchanger and the feed gas cooled under reduced pressure becomes a gas-liquid mixed state, and the liquefied liquefied feed gas is led out as a product. On the other hand, the feed gas system in a gas state that has not been liquefied and is cooled is used as the recirculated feed gas to be fed to the recompression step and the subsequent feed gas cooling step and merges with the feed gas. By recycling the part of the feed gas that has not been liquefied as described above, the loss of the feed gas can be avoided.
氣體狀態之饋入氣體從氣液分離器導出後導入至主熱交換器，將其汽化熱釋放出後供給至饋入氣體壓縮步驟亦可。從氣液分離器導出之氣體狀態之饋入氣體為冷卻之狀態，因此藉由將該汽化熱用於饋入氣體冷卻步驟之饋入氣體之冷卻，可進一步提高饋入氣體之液化效率。The feed gas in the gas state is exported from the gas-liquid separator and then introduced into the main heat exchanger, and the heat of vaporization is released and then supplied to the feed gas compression step. The feed gas in the gas state derived from the gas-liquid separator is in a cooled state, so by using the vaporization heat for the cooling of the feed gas in the gas cooling step, the liquefaction efficiency of the feed gas can be further improved.
（發明3） 上述本發明之氣體液化方法進一步包含將饋入氣體冷卻至高於第一溫度之第二溫度之預冷步驟，且 於上述預冷步驟經冷卻之饋入氣體可於壓縮後供給至饋入氣體冷卻步驟。(Invention 3) The above-mentioned gas liquefaction method of the present invention further includes a pre-cooling step of cooling the feed gas to a second temperature higher than the first temperature, and The feed gas cooled in the above-mentioned pre-cooling step can be supplied to the feed gas cooling step after being compressed.
由於可將液化天然氣之汽化熱用於在饋入氣體壓縮步驟壓縮前之饋入氣體之預冷，故而饋入氣體於經由上述主熱交換器之預冷步驟冷卻至第二溫度後，供給至饋入氣體壓縮步驟亦可。其原因在於，藉由將饋入氣體於更低溫下進行壓縮，可削減壓縮時消耗之動力。Since the heat of vaporization of liquefied natural gas can be used for the pre-cooling of the feed gas before compression in the feed gas compression step, the feed gas is fed to the second temperature after being cooled to the second temperature through the pre-cooling step of the main heat exchanger. It is also possible to feed the gas compression step. The reason is that by compressing the feed gas at a lower temperature, the power consumed during compression can be reduced.
（發明4） 上述本發明之氣體液化方法進一步包含中間冷卻步驟，其將於饋入氣體壓縮步驟壓縮之饋入氣體冷卻至高於第一溫度之第三溫度，且於上述中間冷卻步驟經冷卻之饋入氣體可進一步壓縮後供給至上述饋入氣體冷卻步驟。(Invention 4) The gas liquefaction method of the present invention further includes an intermediate cooling step, which cools the feed gas compressed in the feed gas compression step to a third temperature higher than the first temperature, and the feed gas cooled in the intermediate cooling step can be After being further compressed, it is supplied to the above-mentioned feeding gas cooling step.
將饋入氣體壓縮步驟分割為複數個壓縮階段，將其中間之饋入氣體，利用液化天然氣之汽化熱而於上述主熱交換器來冷卻亦可。於氣體壓縮步驟，氣體溫度藉由絕熱壓縮而上升，壓縮比愈大，熱效率愈下降。因此於壓縮步驟，可藉由應用中間冷卻而改善熱效率。The feed gas compression step is divided into a plurality of compression stages, and the feed gas in the middle can be cooled in the above-mentioned main heat exchanger using the vaporization heat of liquefied natural gas. In the gas compression step, the gas temperature is increased by adiabatic compression. The larger the compression ratio, the lower the thermal efficiency. Therefore, in the compression step, the thermal efficiency can be improved by applying intermediate cooling.
（發明5） 本發明之氣體液化方法亦可進一步包含 第二天然氣導出步驟，其使於第二升壓步驟升壓之液化天然氣的未導入主熱交換器之部分於蒸發器氣化，作為天然氣而從蒸發器導出。(Invention 5) The gas liquefaction method of the present invention may further include The second natural gas exporting step is to vaporize the portion of the liquefied natural gas boosted in the second boosting step that is not introduced into the main heat exchanger in an evaporator, and is exported from the evaporator as natural gas.
於第二升壓步驟升壓之液化天然氣可將將其總量導入主熱交換器，使其升溫、氣化，但將其一部分不導入主熱交換器，而導入與主熱交換器獨立配置之蒸發器亦可。導入蒸發器之液化天然氣於蒸發器氣化，作為氣體狀態之天然氣而供給至天然氣之消耗地。The liquefied natural gas that is boosted in the second boosting step can be introduced into the main heat exchanger to heat up and vaporize, but part of it is not introduced into the main heat exchanger, but is independent of the main heat exchanger. The evaporator is also available. The liquefied natural gas introduced into the evaporator is vaporized in the evaporator and supplied to the natural gas consumption site as natural gas in a gas state.
若將於第二升壓步驟升壓之液化天然氣之總量導入主熱交換器，則存在如下情形：於主熱交換器藉由與饋入氣體之熱交換而獲得液化天然氣之熱量對其總量之蒸發而言不充分。如此，從蒸發器導出之天然氣之總量不成為氣體狀態，而成為氣液混合狀態，或者即便為氣體狀態，亦產生由溫度過低所引起之不良。 因此，將於主熱交換器無法蒸發之部分之液化天然氣導入蒸發器，使其於蒸發器氣化。藉此，可使於第二升壓步驟升壓之液化天然氣之總量蒸發。If the total amount of liquefied natural gas boosted in the second boosting step is introduced into the main heat exchanger, there is a situation where the main heat exchanger obtains the heat of the liquefied natural gas through heat exchange with the feed gas. The amount is insufficient for evaporation. In this way, the total amount of natural gas derived from the evaporator does not become a gas state, but becomes a gas-liquid mixed state, or even if it is a gas state, defects caused by too low temperature occur. Therefore, the part of the liquefied natural gas that cannot be evaporated in the main heat exchanger is introduced into the evaporator and vaporized in the evaporator. Thereby, the total amount of LNG boosted in the second boosting step can be evaporated.
於蒸發器，液化天然氣進行氣化時吸收汽化熱，將該汽化熱用於例如饋入氣體壓縮步驟所使用之壓縮機之冷卻，藉此可進一步提高熱效率。In the evaporator, the LNG absorbs the heat of vaporization when it is gasified, and the heat of vaporization is used, for example, to feed into the cooling of the compressor used in the gas compression step, thereby further improving the thermal efficiency.
（發明6） 上述本發明之氣體液化方法可進一步包含過冷卻步驟，其用以將於液化饋入氣體導出步驟所導出之液體狀態之液化饋入氣體進一步冷卻。(Invention 6) The above-mentioned gas liquefaction method of the present invention may further include a supercooling step for further cooling the liquefied feed gas in the liquid state derived from the liquefied feed gas export step.
於液化饋入氣體導出步驟導出之液體狀態之液化饋入氣體可直接儲藏於液化饋入氣體之儲槽，但亦可經由過冷卻步驟而進一步冷卻後加以儲藏。 於液化饋入氣體導出步驟作為液體狀態而導出之液化饋入氣體之溫度，常常為比較接近饋入氣體之液化點之溫度。但是，若於該溫度下儲藏，則有於儲藏時產生大量蒸發氣體，液體狀態下之儲藏效率下降之情形。因此，若經由本發明所涉及之過冷卻步驟而將液體狀態之液化饋入氣體進一步冷卻，則使蒸發氣體減少，可抑制由於液化饋入氣體進行氣化而引起之饋入氣體之損耗。The liquefied feed gas in the liquid state derived in the liquefied feed gas deriving step can be directly stored in the storage tank of the liquefied feed gas, but it can also be stored after being further cooled through the supercooling step. The temperature of the liquefied feed gas derived as a liquid in the liquefied feed gas derivation step is usually a temperature relatively close to the liquefaction point of the feed gas. However, if it is stored at this temperature, a large amount of vaporized gas may be generated during storage, and the storage efficiency in the liquid state may decrease. Therefore, if the liquefied feed gas in the liquid state is further cooled through the supercooling step involved in the present invention, the boil-off gas is reduced, and the loss of the feed gas caused by the vaporization of the liquefied feed gas can be suppressed.
（發明7） 上述本發明，饋入氣體若為藉由壓縮，利用液化天然氣進行冷卻而液化之氣體即可，例如可為氮氣、氬氣、或氧氣。(Invention 7) In the present invention described above, if the feed gas is compressed and liquefied by using liquefied natural gas, for example, it can be nitrogen, argon, or oxygen.
（發明8） 本發明之氣體液化裝置具備： 將饋入氣體壓縮之第一壓縮機，將饋入氣體導入第一壓縮機之饋入氣體管線，及將經壓縮之饋入氣體導入主熱交換器之壓縮饋入氣體管線； 將藉由上述第一壓縮機而壓縮之饋入氣體進行冷卻之主熱交換器； 將從上述主熱交換器之冷端導出之饋入氣體進行減壓、冷卻之第一減壓閥，及將從上述第一減壓閥導出之饋入氣體進行氣液分離之氣液分離器； 將從上述氣液分離器之液相端導出液體狀態之液化饋入氣體之液化饋入氣體導出管線； 使液化天然氣升壓至第一壓力之第一泵； 使液化天然氣升壓至高於第一壓力之第二壓力之第二泵； 第一液化天然氣管線，其將從上述第一泵導出之液化天然氣導入至上述主熱交換器之冷端； 第二液化天然氣管線，其將經由上述第一液化天然氣管線而導入上述主熱交換器之液化天然氣，於低於液化天然氣之臨界溫度之溫度下從上述主熱交換器之中間部導出，導入上述第二泵； 第三液化天然氣管線，其將從上述第二泵導出之液化天然氣之至少一部分導入至上述主熱交換器之中間部；以及 第一天然氣管線，其將經由上述第三液化天然氣管線而導入上述主熱交換器之液化天然氣，從上述主熱交換器之溫端導出。(Invention 8) The gas liquefaction device of the present invention has: The first compressor that compresses the feed gas, the feed gas into the feed gas line of the first compressor, and the compressed feed gas into the compressed feed gas line of the main heat exchanger; The main heat exchanger for cooling the feed gas compressed by the above-mentioned first compressor; The first pressure reducing valve that decompresses and cools the feed gas derived from the cold end of the above-mentioned main heat exchanger, and the gas-liquid separator that conducts gas-liquid separation of the feed gas derived from the first pressure reducing valve ； From the liquid phase end of the above-mentioned gas-liquid separator, the liquefied feed gas in the liquid state is derived from the liquefied feed gas outlet line; The first pump that boosts the liquefied natural gas to the first pressure; A second pump that boosts the pressure of liquefied natural gas to a second pressure higher than the first pressure; The first liquefied natural gas pipeline, which leads the liquefied natural gas derived from the first pump to the cold end of the main heat exchanger; The second liquefied natural gas pipeline, which will lead the liquefied natural gas introduced into the main heat exchanger via the first liquefied natural gas pipeline from the middle part of the main heat exchanger at a temperature lower than the critical temperature of the liquefied natural gas, and lead into the above Second pump The third LNG pipeline, which introduces at least a part of the LNG derived from the second pump to the middle part of the main heat exchanger; and The first natural gas pipeline, which will lead the LNG into the main heat exchanger through the third LNG pipeline, and lead out from the warm end of the main heat exchanger.
饋入氣體於第一壓縮機壓縮後，於主熱交換器冷卻，進一步地於第一減壓閥進行減壓、冷卻，藉此，至少其一部分液化。After the feed gas is compressed in the first compressor, it is cooled in the main heat exchanger, and further reduced and cooled in the first pressure reducing valve, whereby at least a part of it is liquefied.
於主熱交換器，進行饋入氣體、與液化天然氣之熱交換，藉由液化天然氣之汽化熱而將饋入氣體冷卻。液化天然氣係利用第一泵而升壓至既定壓力（設為第一壓力），導入至主熱交換器之冷端，藉由與饋入氣體之熱交換而吸收汽化熱。然後，液化天然氣從主熱交換器之中間部導出，導入第二泵，藉由該第二泵而升壓至第二壓力。第二壓力高於第一壓力，藉由從第一壓力升壓至第二壓力，則液化天然氣之溫度上升。溫度上升之液化天然氣再次導入主熱交換器，進一步地藉由與饋入氣體之熱交換而吸收汽化熱，進行氣化，從主熱交換器之溫端導出。In the main heat exchanger, the feed gas is exchanged with the LNG, and the feed gas is cooled by the heat of vaporization of the LNG. The liquefied natural gas is boosted to a predetermined pressure (set as the first pressure) by the first pump, and is introduced to the cold end of the main heat exchanger to absorb the heat of vaporization by heat exchange with the feed gas. Then, the liquefied natural gas is led out from the middle part of the main heat exchanger, introduced into the second pump, and the pressure is increased to the second pressure by the second pump. The second pressure is higher than the first pressure, and by increasing the pressure from the first pressure to the second pressure, the temperature of the liquefied natural gas rises. The liquefied natural gas whose temperature has risen is introduced into the main heat exchanger again, and further absorbs the heat of vaporization by heat exchange with the feed gas, undergoes gasification, and is discharged from the warm end of the main heat exchanger.
由於在第一泵升壓至第一壓力，故而從第一泵導入主熱交換器時之液化天然氣之溫度（即，主熱交換器之溫端之液化天然氣之溫度）與升壓至第二壓力之情形相比較而言低。因此，藉由不使液化天然氣之壓力上升至第一壓力以上，可於主熱交換器獲得充分之汽化熱。 實施與具有第一壓力之液化天然氣之熱交換後，藉由第二泵而使液化天然氣升壓至第二壓力。藉由上升至第二壓力，可將使液化天然氣進行氣化後的氣體狀態之天然氣以高壓來供給。達到第二壓力之液化天然氣之汽化熱對於使饋入氣體液化而言不充分，但對於使液化前之氣體狀態之饋入氣體冷卻而言充分。因此，達到第二壓力之液化天然氣再次導入主熱交換器，將該汽化熱用於饋入氣體之冷卻。Since the pressure of the first pump is increased to the first pressure, the temperature of the liquefied natural gas (ie, the temperature of the liquefied natural gas at the warm end of the main heat exchanger) and the pressure increased to the second The stress situation is relatively low. Therefore, by not increasing the pressure of the liquefied natural gas above the first pressure, sufficient heat of vaporization can be obtained in the main heat exchanger. After the heat exchange with the liquefied natural gas having the first pressure is implemented, the pressure of the liquefied natural gas is increased to the second pressure by the second pump. By increasing to the second pressure, the natural gas in the gas state after gasifying the LNG can be supplied at a high pressure. The heat of vaporization of the liquefied natural gas reaching the second pressure is not sufficient for liquefying the feed gas, but is sufficient for cooling the feed gas in the gas state before liquefaction. Therefore, the liquefied natural gas reaching the second pressure is introduced into the main heat exchanger again, and the heat of vaporization is used for the cooling of the feed gas.
如以上所述於主熱交換器冷卻之饋入氣體從主熱交換器之冷端導入第一減壓閥，進行減壓、冷卻。此處，成為氣液混合狀態之饋入氣體利用氣液分離器而分離為氣相及液相，從液相端部分導出液體狀態之液化饋入氣體。As described above, the feed gas cooled in the main heat exchanger is introduced from the cold end of the main heat exchanger to the first pressure reducing valve for pressure reduction and cooling. Here, the feed gas in a gas-liquid mixed state is separated into a gas phase and a liquid phase by a gas-liquid separator, and the liquefied feed gas in a liquid state is derived from the liquid phase end portion.
（發明9） 上述發明之氣體液化裝置亦可進一步包含再循環饋入氣體管線，其從氣液分離器之氣相端導出氣體狀態之饋入氣體，使其匯流於上述第一壓縮機之前段。(Invention 9) The gas liquefaction device of the above-mentioned invention may further include a recirculation feed-in gas line, which leads the feed-in gas in a gaseous state from the gas-phase end of the gas-liquid separator to converge at the front stage of the first compressor.
分離為氣液分離器之氣相的氣體狀態之饋入氣體可直接釋放至外部，但作為與導入第一壓縮機之前段之饋入氣體匯流之再循環饋入氣體亦可。其原因在於，藉由向如上所述將未經液化之部分之饋入氣體再次液化之步驟進行再循環，而避免饋入氣體之損耗。The feed gas in the gas state separated into the gas phase of the gas-liquid separator can be directly released to the outside, but it can also be used as a recirculation feed gas that merges with the feed gas introduced into the first stage of the compressor. The reason is to avoid the loss of the fed gas by recirculating the step of re-liquefying the feeding gas of the part that has not been liquefied as described above.
（發明10） 再循環饋入氣體管線亦可設為經過上述主熱交換器。(Invention 10) The recirculation feed gas line can also be set to pass through the above-mentioned main heat exchanger.
再循環饋入氣體由於經過主熱交換器及第一減壓閥而冷卻，故而可使其再次經過主熱交換器，而將其汽化熱用於饋入氣體之冷卻。藉由設為此種構成，未經液化之部分之饋入氣體之汽化熱亦有效利用，可提高氣體液化裝置整體之熱效率。The recirculated feed gas is cooled by passing through the main heat exchanger and the first pressure reducing valve, so it can pass through the main heat exchanger again, and its vaporization heat is used for the cooling of the feed gas. With this configuration, the heat of vaporization of the fed gas in the part that has not been liquefied is also effectively used, and the overall thermal efficiency of the gas liquefaction device can be improved.
（發明11） 上述發明之氣體液化裝置，饋入氣體管線設為經過上述主熱交換器亦可。(Invention 11) In the gas liquefaction device of the above invention, the feed gas line may be set to pass through the main heat exchanger.
藉由將饋入氣體於第一壓縮機壓縮前加以冷卻，可削減饋入氣體壓縮所消耗之動力。By cooling the feed gas before compression by the first compressor, the power consumed by the feed gas compression can be reduced.
（發明12） 上述發明之氣體液化裝置，進一步具備：第二壓縮機，其將經壓縮之饋入氣體進一步壓縮；饋入氣體中間冷卻管線，其經過上述主熱交換器將壓縮之上述饋入氣體導入至上述第二壓縮機；以及升壓饋入氣體管線，其將由上述第二壓縮機所壓縮之饋入氣體導入上述主熱交換器。(Invention 12) The gas liquefaction device of the above invention further includes: a second compressor that further compresses the compressed feed gas; and a feed gas intermediate cooling line that introduces the compressed feed gas through the main heat exchanger to the A second compressor; and a boosted feed gas line, which introduces the feed gas compressed by the second compressor into the main heat exchanger.
藉由第一壓縮機而壓縮之饋入氣體被導入主熱交換器。然後，於主熱交換器內冷卻至第三溫度後再從主熱交換器之中間部導出。此處，利用第二壓縮機而進一步壓縮，再次導入主熱交換器。可藉由該等而削減饋入氣體之壓縮所消耗之動力。The feed gas compressed by the first compressor is introduced into the main heat exchanger. Then, it is cooled to the third temperature in the main heat exchanger and then discharged from the middle part of the main heat exchanger. Here, it is further compressed by the second compressor and introduced into the main heat exchanger again. The power consumed by the compression of the fed gas can be reduced by these.
（發明13） 上述發明之氣體液化裝置，進一步具備：蒸發器，其使於第二泵升壓之液化天然氣的未導入上述主熱交換器之部分之液化天然氣進行氣化；以及 第二天然氣管線，其從上述蒸發器導出氣體狀態之天然氣亦可。(Invention 13) The gas liquefaction device of the above-mentioned invention further includes: an evaporator that vaporizes the portion of the liquefied natural gas boosted by the second pump that is not introduced into the main heat exchanger; and The second natural gas pipeline can also export natural gas in a gas state from the above-mentioned evaporator.
雖可將於第二泵升壓之液化天然氣之總量導入主熱交換器，但若多於饋入氣體之冷卻所需之汽化熱之量的汽化熱導入主熱交換器，則液化天然氣之氣化不充分。於此種情形時，於主熱交換器未經氣化之部分之液化天然氣可不導入主熱交換器，而是導入與主熱交換器獨立設置之蒸發器。藉由設為此種構成，可將於第二泵升壓之液化天然氣之總量進行氣化，而導出氣體狀態之天然氣。Although the total amount of liquefied natural gas boosted by the second pump can be introduced into the main heat exchanger, if more than the amount of vaporization heat required for cooling of the fed gas is introduced into the main heat exchanger, the liquefied natural gas Insufficient gasification. In this case, the unvaporized portion of the LNG in the main heat exchanger may not be introduced into the main heat exchanger, but into an evaporator installed independently of the main heat exchanger. With this configuration, the total amount of liquefied natural gas boosted by the second pump can be gasified, and natural gas in a gaseous state can be derived.
（發明14） 上述發明之氣體液化裝置，進一步具備：過冷卻器，其用以將從液化饋入氣體導出管線導出之液化饋入氣體進行冷卻； 將從上述過冷卻器導出之液化饋入氣體之一部分進行減壓冷卻之第二減壓閥、及將從上述第二減壓閥導出之饋入氣體作為低壓再循環饋入氣體而導入至上述過冷卻器之冷端的第一低壓再循環氣體管線； 第二低壓再循環氣體管線，其將從上述過冷卻器之溫端導出之低壓再循環饋入氣體導入至上述主熱交換器之冷端； 第三壓縮機，其將上述低壓再循環饋入氣體壓縮而使其匯流於上述第一壓縮機之前段；以及 第三低壓再循環氣體管線，其將經由上述第二低壓饋入氣體管線而從上述主熱交換器之溫端導出之低壓再循環饋入氣體，於第三壓縮機壓縮而使其匯流於上述第一壓縮機之前段。(Invention 14) The gas liquefaction device of the above invention further includes: a subcooler for cooling the liquefied feed gas derived from the liquefied feed gas outlet line; A second pressure reducing valve for decompressing and cooling a part of the liquefied feed gas derived from the above-mentioned subcooler, and the feed gas derived from the second pressure reducing valve as low-pressure recirculation feed gas and introducing it to the above The first low-pressure recirculation gas line at the cold end of the subcooler; The second low-pressure recirculation gas pipeline, which introduces the low-pressure recirculation feed gas derived from the warm end of the above-mentioned subcooler to the cold end of the above-mentioned main heat exchanger; A third compressor, which compresses the low-pressure recirculation feed gas and makes it converge in the front stage of the first compressor; and The third low-pressure recirculation gas line, which combines the low-pressure recirculation feed gas derived from the warm end of the main heat exchanger through the second low-pressure feed gas line, and compresses it in a third compressor to converge to the above Before the first compressor.
利用過冷卻器，可將由氣液分離器分離為液相側之液體狀態之液化饋入氣體進一步冷卻。使液化饋入氣體之溫度下降，可減少儲藏時之饋入氣體之氣化（即，蒸發氣體之產生），減少液化饋入氣體之儲藏時之損耗。Using the subcooler, the liquefied feed gas separated into the liquid state on the liquid side by the gas-liquid separator can be further cooled. Lowering the temperature of the liquefied feed gas can reduce the vaporization of the feed gas (ie, the generation of boil-off gas) during storage, and reduce the loss of the liquefied feed gas during storage.
（發明15） 進一步具備低壓饋入氣體管線，其於上述第三壓縮機導入壓力低於饋入氣體之低壓饋入氣體。(Invention 15) It is further provided with a low-pressure feed gas pipeline, which introduces a low-pressure feed gas whose pressure is lower than the feed gas into the third compressor.
於從外部供給之饋入氣體之供給壓力低之情形時，可利用第三壓縮機進行壓縮。When the supply pressure of the feed gas supplied from the outside is low, the third compressor can be used for compression.
（發明16） 上述發明，饋入氣體只要係藉由壓縮且利用液化天然氣進行冷卻而液化之氣體即可，例如可為氮氣、氬氣、或氧氣。(Invention 16) In the above invention, the feed gas only needs to be a gas that is liquefied by being compressed and cooled with liquefied natural gas. For example, it may be nitrogen, argon, or oxygen.
以下對本發明之若干實施方式進行說明。以下所說明之實施方式係對本發明之一例加以說明者。本發明不受以下實施方式之任何限定，亦包含於不變更本發明之主旨之範圍內實施的各種變形形態。此外，並非以下所說明之構成之全部為本發明之必需構成。Several embodiments of the present invention will be described below. The embodiments described below are illustrative of an example of the present invention. The present invention is not limited to the following embodiments at all, and is also included in various modified forms implemented within the scope of not changing the gist of the present invention. In addition, not all of the constitutions described below are essential constitutions of the present invention.
（實施方式1）
參照圖1，對實施方式1之氣體液化裝置100及使用其之氣體液化方法進行說明。(Embodiment 1)
1, the
本發明之氣體液化裝置100具備：第一壓縮機1，其將饋入氣體壓縮；饋入氣體管線29，其將饋入氣體導入第一壓縮機1；主熱交換器2，其將由上述第一壓縮機1所壓縮之饋入氣體進行冷卻；壓縮饋入氣體管線30，其將由上述第一壓縮機1所壓縮之饋入氣體導入上述主熱交換器2；第一減壓閥3，其將從上述主熱交換器2之冷端導出之饋入氣體進行減壓・冷卻；氣液分離器4，其將從上述第一減壓閥3導出之饋入氣體進行氣液分離；液化饋入氣體導出管線21，其從上述氣液分離器4之液相端導出液體狀態之液化饋入氣體；第一泵11，其使液化天然氣升壓至第一壓力；第二泵12，其使液化天然氣升壓至高於第一壓力之第二壓力；第一液化天然氣管線22，其將從上述第一泵11導出之液化天然氣導入至上述主熱交換器2之冷端；第二液化天然氣管線23，其將經由上述第一液化天然氣管線22而導入上述主熱交換器2之液化天然氣，於低於液化天然氣之臨界溫度之溫度下從上述主熱交換器2之中間部導出，再導入上述第二泵12；第三液化天然氣管線24，其將從上述第二泵12導出之液化天然氣之至少一部分導入至上述主熱交換器2之中間部；以及第一天然氣管線25，其將經由上述第三液化天然氣管線24而導入上述主熱交換器2之液化天然氣，從上述主熱交換器2之溫端導出。
本實施方式，例如作為成為液化之對象的饋入氣體，將氮氣導入氣體液化裝置100之第一壓縮機11。該氣體亦可為低於常溫（25℃），例如可為0℃以上、65℃以下。The
於饋入氣體壓縮步驟，饋入氣體（例如流量為1653 Nm3
/h）藉由第一壓縮機1而壓縮至既定壓力。
第一壓縮機1係用以將供給至主熱交換器2且冷卻之饋入氣體，於主熱交換器2之前段進行壓縮之壓縮機。饋入氣體係於主熱交換器2冷卻後液化之氣體，例如可為氮氣、氬氣、或氧氣，為該等之混合氣體亦可。
於導入第一壓縮機1之饋入氣體為氮氣之情形時，第一壓縮機1導入時之氮氣之壓力例如為1 barA以上、12 barA以下。導入主熱交換器2之饋入氣體之壓力例如為40 barA以上、60 barA以下。In the feeding gas compression step, the feeding gas (for example, the flow rate is 1653 Nm 3 /h) is compressed to a predetermined pressure by the first compressor 1. The first compressor 1 is a compressor used to compress the feed gas supplied to the
饋入氣體冷卻步驟中，於饋入氣體壓縮步驟經壓縮之饋入氣體於主熱交換器2冷卻至第一溫度。
第一溫度必須為於第一減壓閥3之後段，饋入氣體之至少一部分液化之溫度，例如為-160℃以上、-130℃以下之溫度。
饋入氣體係於主熱交換器2之內部，藉由與後述液化天然氣之熱交換而冷卻。
此外，預先冷卻供給至饋入氣體壓縮步驟之饋入氣體亦可。In the feeding gas cooling step, the feeding gas compressed in the feeding gas compression step is cooled to the first temperature in the
氣液分離步驟中，將於饋入氣體冷卻步驟冷卻之饋入氣體，利用第一減壓閥3而減壓、冷卻後，利用氣液分離器4而氣液分離為氣相及液相。藉由經過減壓閥3，饋入氣體之溫度較從熱交換器2之冷端導出之時刻而言下降。其結果為，饋入氣體係以-196℃以上、-160℃以下之溫度來導入氣液分離器4。In the gas-liquid separation step, the feed gas cooled in the feed gas cooling step is decompressed and cooled by the first
液化饋入氣體導出步驟係將於氣液分離步驟分離為氣液分離器4之液相端的液化饋入氣體以液體狀態從液化饋入氣體導出管線21導出之步驟。所導出之饋入氣體係以液體狀態來儲存。The liquefied feed gas deriving step is a step of separating the liquefied feed gas from the liquid phase end of the gas-
第一升壓步驟係利用第一泵11，將儲存於儲槽之液化天然氣（例如流量為3695 Nm3
/h）升壓至第一壓力之步驟。儲槽內之液化天然氣之壓力為大氣壓以上，例如為1.013 barA以上、2 barA以下之範圍。第一壓力例如為7 barA以上、30 barA以下之範圍。The first pressure increasing step is a step of using the
升壓至第一壓力之液化天然氣導入主熱交換器2後，於第二泵12升壓至高於第一壓力之第二壓力。
為使第二泵12不產生空蝕，第一壓力係以液化天然氣之導入第二泵12時之壓力下之飽和溫度高於導入第二泵時之溫度的方式來設定。After the LNG boosted to the first pressure is introduced into the
例如，當導入第二泵12之液化天然氣之溫度為-120℃時，導入第二泵12之液化天然氣之壓力必須為-120℃下之飽和壓力即14 barA以上，第一泵11之出口壓力係以可達到該壓力以上之方式設定。
從第一泵11導出之液化天然氣經由第一液化天然氣管線22而導入至主熱交換器2之冷端，進一步地從主熱交換器2之中間部，經由第二液化天然氣管線23而導入至第二泵12。
從主熱交換器2之中間部導出至第二液化天然氣管線23之液化天然氣之溫度係低於液化天然氣之飽和溫度的溫度。For example, when the temperature of the liquefied natural gas introduced into the
儲存於儲槽之液化天然氣之溫度係於第一泵11升壓時藉由熱輸入而上升，但於其溫度上升大之情形時，主熱交換器2之饋入氣體之冷卻及液化變得不充分，存在損及液化效率之顧慮。因此，藉由第一泵11之升壓係於第二泵12入口，於不達到飽和溫度之壓力之範圍內僅可能抑制為低，較佳為抑制來自第一泵11之液化天然氣之溫度上升。導入主熱交換器2之液化天然氣溫度例如為-162℃以上、-140℃以下。The temperature of the liquefied natural gas stored in the storage tank is increased by heat input when the pressure of the
第二升壓步驟係利用第二泵12，使液化天然氣升壓至高於第一壓力之第二壓力的步驟。第二壓力係根據使用經氣化之天然氣時所必需之天然氣壓力來決定，例如，於必須將氣體狀態之天然氣以50 barA以上、120 barA以下之壓力來供給之情形時，考慮到主熱交換器2之壓力損耗等，第二壓力可設為51 barA以上、121 barA以下。The second pressure increasing step is a step of using the
第一天然氣導出步驟係將藉由第二泵12而升壓之液化天然氣之至少一部分，經由第三液化天然氣管線24而導入主熱交換器2，使其氣化，從主熱交換器2之溫端，利用第一天然氣管線25而以氣體狀態導出之步驟。所導出之氣體狀態之天然氣具有低於第二壓力之壓力（例如50 barA以上、120 barA以下），於消耗地被消耗。The first natural gas export step is to introduce at least a part of the liquefied natural gas boosted by the
饋入氣體冷卻步驟中，從主熱交換器2之溫端導入主熱交換器2之饋入氣體係於主熱交換器2之內部，進行與經過第三液化天然氣管線24之液化天然氣之熱交換。藉此經冷卻之饋入氣體進一步與經過第一液化天然氣管線22之液化天然氣進行熱交換，藉此進一步冷卻，從熱交換器2之冷端導出。
如上所述，藉由與經過第一液化天然氣管線22之充分低之溫度之液化天然氣進行熱交換，饋入氣體高效率地液化。進一步地，然後藉由利用第二泵12進行升壓，氣體狀態之天然氣可以充分之壓力來供給至消耗地。
上述實施方式1，於將高壓（95 barA）之天然氣以流量3700 Nm3
/h導出之情形時，液化天然氣藉由第一泵11而升壓至壓力20 barA，進一步地藉由第二泵12而升壓至壓力95 barA。該情形時之饋入氣體（氮氣）之液化量成為1000 Nm3
/h。
另一方面，於不將升壓之步驟如本實施方式般設為2個階段，而利用1個升壓機構，將液化天然氣以1個階段升壓，而導出具有同等壓力之天然氣之情形時，必須以1個階段將液化天然氣升壓至95 barA。於該1個階段之升壓步驟中，本實施方式為-155℃之向主熱交換器2之液化天然氣導入溫度上升至-147℃。因此，液化天然氣於主熱交換器2吸收之汽化熱減少，饋入氣體之冷卻變得不充分。其結果為，饋入氣體之液化量成為810 Nm3
/h，較實施方式1之情形而言減少。
如上所述，於將升壓步驟設為2個階段之本實施方式之方法中，與將升壓步驟設為1個階段之現有之饋入氣體液化方法比較，可以高效率來液化。In the feeding gas cooling step, the feeding gas system of the
（另一實施方式1）
於氣液分離步驟分離為氣液分離器4之氣相側的氣體狀態之饋入氣體（例如流量為371 Nm3
/h）可如圖1所示，向系統外釋放，但作為另一實施方式，如圖2所示，經由再循環饋入氣體管線26而匯流於第一壓縮機1之前段，與饋入氣體一起再次供給至饋入氣體壓縮步驟。藉由設置此種饋入氣體再循環步驟，而將氣液分離器4之氣相部之饋入氣體作為再循環饋入氣體而再次向饋入氣體壓縮步驟供給，可抑制氣體狀態之饋入氣體之損耗。(Another embodiment 1) In the gas-liquid separation step, the feed gas (for example, the flow rate is 371 Nm 3 /h) separated into the gaseous state of the gas-
（另一實施方式2）
進一步地作為另一實施方式，如圖3所示，使從氣液分離器4之氣相側導出之再循環饋入氣體（例如流量為371 Nm3
/h）經過主熱交換器2後，匯流於第一壓縮機1之前段。從氣液分離器4之氣相側導出之氣體狀態之再循環饋入氣體被冷卻，例如為-180℃以上、-160℃以下之低溫，因此使其汽化熱於主熱交換器2釋放，利用於饋入氣體之冷卻，藉此可進一步提高液化效率。
經過主熱交換器2之再循環饋入氣體可從主熱交換器2之冷端導出，亦可從主熱交換器2之中間部導出。(Another embodiment 2) As another embodiment, as shown in FIG. 3, the recycled feed gas (for example, the flow rate of 371 Nm 3 /h) derived from the gas-phase side of the gas-
（實施方式2）
參照圖4，對實施方式2之氣體液化裝置101及使用其之氣體液化方法進行說明。與上述實施方式之氣體液化裝置相同之符號之要素由於具有相同功能，故而省略其說明。(Embodiment 2)
4, the
實施方式2之氣體液化裝置101，於將饋入氣體導入第一壓縮機之前，藉由預冷步驟而實施饋入氣體之預冷。
於饋入氣體預冷步驟，饋入氣體係從主熱交換器2之溫端導入至主熱交換器2之內部，且進行冷卻。導入至主熱交換器2之溫端時的饋入氣體之溫度例如為0℃以上、65℃以下，於主熱交換器2之內部預冷至例如-110℃以上、-50℃以下後，從主熱交換器2之中間部導出。此處，使經預冷之饋入氣體導出之主熱交換器2之中間部較利用第二泵12而於主熱交換器2再導液化天然氣之點而言，位於主熱交換器2之溫端側。
從主熱交換器2之中間部導出之饋入氣體導入至第一壓縮機1，進行壓縮。In the
（實施方式3）
參照圖5，對實施方式3之氣體液化裝置102及使用其之氣體液化方法進行說明。與上述實施方式之氣體液化裝置相同之符號之要素由於具有相同功能，故而省略其說明。(Embodiment 3)
5, the
實施方式3之氣體液化裝置102中，實施饋入氣體壓縮步驟後，藉由中間冷卻步驟而實施饋入氣體之中間冷卻。
於饋入氣體壓縮步驟藉由第一壓縮機1而壓縮之饋入氣體於接下來之中間冷卻步驟，從主熱交換器2之溫端導入至主熱交換器2之內部，進行冷卻。導入至主熱交換器2之溫端時之壓縮饋入氣體之溫度例如為0℃以上、65℃以下，於主熱交換器2之內部進行中間冷卻至例如-110℃以上、-50℃以下之後，從主熱交換器2之中間部導出。此處，使經中間冷卻之饋入氣體導出的主熱交換器2之中間部較藉由第二泵12而於主熱交換器2再導入液化天然氣之點而言，位於主熱交換器2之溫端側。In the
從主熱交換器2之中間部導出之饋入氣體導入至第二壓縮機6壓縮。藉此，例如從第一壓縮機1以10 barA以上、30 barA以下之壓力導出饋入氣體之壓力，從第二壓縮機6以40 barA以上、60 barA以下之壓力導出。
從第二壓縮機6導出之饋入氣體經由升壓饋入氣體管線32，從主熱交換器2之溫端而再次導入至主熱交換器2之內部，供給至接下來之饋入氣體冷卻步驟。The feed gas derived from the middle part of the
（實施方式4）
使用圖6，對實施方式4之氣體液化裝置103及使用其之氣體液化方法進行說明。與實施方式1之氣體液化裝置相同之符號之要素由於具有相同之功能，故而省略其說明。(Embodiment 4)
Using FIG. 6, the
實施方式4之氣體液化裝置103包括第二天然氣導出步驟，其將於第二升壓步驟藉由第二泵12而升壓之液化天然氣（例如流量為3695 Nm3
/h）的未導入主熱交換器2之部分（例如流量為3277 Nm3
/h），導入蒸發器5而使其氣化，以氣體狀態從蒸發器5，且從第二天然氣管線27導出。The
從第二泵12經由第三液化天然氣管線24而導入至主熱交換器2之液化天然氣、與導入至蒸發器5之液化天然氣之流量比率可根據饋入氣體之熱量（即，饋入氣體之流量、壓力及溫度）來決定，例如可設為2：8～9：1之範圍。於饋入氣體之熱量較大之情形時，可使向主熱交換器2導入之液化天然氣之流量增加，於饋入氣體之熱量較小之情形時，可使導入至蒸發器5之液化天然氣之流量增加。藉由以上述方式進行調整，從主熱交換器經由第一天然氣管線25而導出之天然氣、以及從蒸發器5經由第二天然氣管線27而導出之天然氣均可以總量為氣化之狀態而導出。The flow rate ratio of the LNG introduced from the
（實施方式5）
參照圖7，對實施方式5之氣體液化裝置104及使用其之氣體液化方法進行說明。與上述實施方式之氣體液化裝置相同之符號之要素由於具有相同功能，故而省略其說明。(Embodiment 5)
7, the
於實施方式5之氣體液化裝置104，於液化饋入氣體導出步驟從液化饋入氣體導出管線21導出之液化饋入氣體係於過冷卻步驟進一步冷卻。
過冷卻步驟中，於氣液分離器4冷卻至例如-180℃以上、-160℃以下，分離為液相側之液化饋入氣體（例如流量為1281 Nm3
/h）係經由液化饋入氣體導出管線21而導入至過冷卻器8。此處，液化饋入氣體冷卻至例如-196℃以上、-175℃以下之溫度。於過冷卻器8之內部經冷卻之液化饋入氣體（例如流量為1281 Nm3
/h）經由過冷卻液化饋入氣體管線41而從過冷卻器8導出。所導出之液化饋入氣體之一部分（例如流量為1000 Nm3
/h）可以液體狀態輸送至消耗地，儲存於儲槽亦可。In the
從過冷卻器8經由過冷卻液化饋入氣體管線41而導出之液化饋入氣體之一部分（流量為281 Nm3
/h），藉由經由設置於從管線41上分支之第一低壓再循環饋入氣體管線42上之第二減壓閥9，而減壓冷卻。此處經減壓、冷卻之氣液混合狀態之低壓再循環饋入氣體例如於-196℃以上、-176℃以下之溫度下，從過冷卻器8之冷端側導入過冷卻器8。藉由從管線42導入過冷卻器8之低壓再循環饋入氣體、與經由液化饋入氣體導出管線21而導入過冷卻器8之液化饋入氣體進行熱交換，從而於過冷卻器8之內部吸收汽化熱。A part of the liquefied feed gas (flow rate is 281 Nm 3 /h) derived from the
吸收汽化熱後之低壓再循環饋入氣體係於例如-174℃以上、-155℃以下之溫度下，從過冷卻器8之溫端側導入至第二低壓再循環饋入氣體管線33後，從主熱交換器2之冷端側導入至主熱交換器2。藉由於主熱交換器2之內部進行與饋入氣體之熱交換，而進一步吸收汽化熱，於例如0℃以上、65℃以下之溫度下，從主熱交換器2之溫端側導出至第三低壓再循環饋入氣體管線34。所導出之低壓再循環饋入氣體藉由第三壓縮機7而壓縮後，送至第一壓縮機1之前段。於第一壓縮機1之前段，作為原料之饋入氣體、經由第三低壓再循環饋入氣體管線34之低壓再循環饋入氣體、以及經由再循環饋入氣體管線26之再循環饋入氣體於第一壓縮機1之前段匯流、混合後，供給至饋入氣體壓縮步驟。
第三壓縮機7可設為能夠將低溫液化氣體壓縮之低溫壓縮機。After absorbing the heat of vaporization, the low-pressure recirculation feed gas system is introduced from the warm end of the
作為另一實施方式，饋入氣體亦可如圖8所示，匯流於第三壓縮機7之前段。饋入氣體之導入位置可根據饋入氣體之壓力來選擇。
於所供給之饋入氣體之壓力高於氣液分離器4之氣相部之壓力之情形時，較佳為將饋入氣體於第一壓縮機1之前段導入（參照圖6）。相反，於所供給之饋入氣體之壓力低於氣液分離器4之氣相部之壓力之情形時，較佳為將饋入氣體於第三壓縮機7之前段導入（參照圖7）。
此外、饋入氣體之溫度由於藉由以壓縮機進行壓縮而上升，故而用以將其冷卻之後冷卻器設置於壓縮機之後段亦可。As another embodiment, the feed gas may also be as shown in FIG. 8 and converge before the
圖9所示之實施方式6之氣體液化裝置105，從氣液分離器4之氣相部導出之再循環饋入氣體及/或從過冷卻器8導出之低壓再循環饋入氣體從主熱交換器2之中間部導出。再循環饋入氣體係與在主熱交換器2預冷之饋入氣體一併藉由第一壓縮機1而壓縮。低壓再循環氣體藉由第三壓縮機7而壓縮。
從第三壓縮機7導出之氣體於主熱交換器2冷卻後導入第一壓縮機1亦可。
饋入氣體與從第三壓縮機7導出之低壓再循環饋入氣體匯流後，導入至第一壓縮機1亦可。In the
作為其他實施方式，如圖10所示。此處，作為原料之饋入氣體於主熱交換器2預冷後導入至第三壓縮機7亦可。於第三壓縮機7之後段，與饋入氣體及再循環饋入氣體混合後導入至第一壓縮機1亦可。
於第一壓縮機1及第三壓縮機7之各自之出口，設置後冷卻器亦可。
從主熱交換器2之中間部導出之再循環饋入氣體或者低壓再循環饋入氣體之溫度例如為-120℃以上、-50℃以下。藉由該構成，可進行低溫之氣體壓縮，藉此可削減壓縮機所消耗之動力。As another embodiment, it is shown in FIG. 10. Here, the feed gas as a raw material may be pre-cooled in the
1:第一壓縮機
2:主熱交換器
3:第一減壓閥
4:氣液分離器
5:蒸發器
6:第二壓縮機
7:第三壓縮機
8:過冷卻器
9:第二減壓閥
11:第一泵
12:第二泵
21:液化饋入氣體導出管線
22:第一液化天然氣管線
23:第二液化天然氣管線
24:第三液化天然氣管線
25:第一天然氣管線
26:再循環饋入氣體管線
27:第二天然氣管線
28:饋入氣體預冷管線
29:饋入氣體管線
30:壓縮饋入氣體管線
31:饋入氣體中間冷卻管線
32:升壓饋入氣體管線
33:第二低壓再循環饋入氣體管線
34:第三低壓再循環饋入氣體管線
41:過冷卻液化饋入氣體管線
42:第一低壓再循環饋入氣體管線
100、101、102、103、104、105:氣體液化裝置1: The first compressor
2: Main heat exchanger
3: The first pressure reducing valve
4: Gas-liquid separator
5: Evaporator
6: The second compressor
7: The third compressor
8: Subcooler
9: The second pressure reducing valve
11: The first pump
12: Second pump
21: Liquefied feed gas outlet pipeline
22: The first LNG pipeline
23: The second LNG pipeline
24: The third LNG pipeline
25: The first natural gas pipeline
26: Recirculation feed gas line
27: The second natural gas pipeline
28: Feed into the gas pre-cooling pipeline
29: Feed into the gas line
30: Compressed feed gas pipeline
31: Feed into the gas intercooling pipeline
32: Boost feed gas pipeline
33: The second low-pressure recirculation feed gas line
34: The third low-pressure recirculation feed gas line
41: Subcooled liquefaction feed gas pipeline
42: The first low-pressure recirculation
圖1係表示實施方式1之氣體液化裝置之構成例之圖。
圖2係表示實施方式1之另一實施方式1氣體液化裝置之構成例的圖。
圖3係表示實施方式1之另一實施方式2氣體液化裝置之構成例的圖。
圖4係表示實施方式2之氣體液化裝置之構成例的圖。
圖5係表示實施方式3之氣體液化裝置之構成例的圖。
圖6係表示實施方式4之氣體液化裝置之構成例的圖。
圖7係表示實施方式5之氣體液化裝置之構成例的圖。
圖8係表示實施方式6之氣體液化裝置之構成例的圖。
圖9係表示實施方式7之氣體液化裝置之構成例的圖。
圖10係表示實施方式8之氣體液化裝置之構成例的圖。Fig. 1 is a diagram showing a configuration example of a gas liquefaction apparatus according to the first embodiment.
Fig. 2 is a diagram showing a configuration example of a gas liquefaction apparatus of another embodiment 1 of the first embodiment.
Fig. 3 is a diagram showing a configuration example of a gas liquefaction apparatus according to another
1:第一壓縮機 1: The first compressor
2:主熱交換器 2: Main heat exchanger
3:第一減壓閥 3: The first pressure reducing valve
4:氣液分離器 4: Gas-liquid separator
11:第一泵 11: The first pump
12:第二泵 12: Second pump
21:液化饋入氣體導出管線 21: Liquefied feed gas outlet pipeline
22:第一液化天然氣管線 22: The first LNG pipeline
23:第二液化天然氣管線 23: The second LNG pipeline
24:第三液化天然氣管線 24: The third LNG pipeline
25:第一天然氣管線 25: The first natural gas pipeline
29:饋入氣體管線 29: Feed into the gas line
30:壓縮饋入氣體管線 30: Compressed feed gas pipeline
100:氣體液化裝置 100: Gas liquefaction device
Claims (16)
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| Application Number | Priority Date | Filing Date | Title |
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| JPJP2019-008163 | 2019-01-22 | ||
| JP2019008163 | 2019-01-22 |
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| TW202028669A TW202028669A (en) | 2020-08-01 |
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| TW108116444A TWI746977B (en) | 2019-01-22 | 2019-05-13 | Gas liquefaction method and gas liquefaction device |
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| EP (1) | EP3914869A1 (en) |
| JP (1) | JP7393607B2 (en) |
| KR (1) | KR20210115006A (en) |
| CN (1) | CN113330263B (en) |
| SG (1) | SG11202107082RA (en) |
| TW (1) | TWI746977B (en) |
| WO (1) | WO2020151991A1 (en) |
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| JP7379763B2 (en) | 2019-07-25 | 2023-11-15 | レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Gas liquefaction method and gas liquefaction device |
| CN113310281A (en) * | 2021-06-15 | 2021-08-27 | 中国科学院理化技术研究所 | Liquid air production device utilizing LNG cold energy |
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| WO2017071742A1 (en) * | 2015-10-28 | 2017-05-04 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus and method for producing liquefied gas |
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| GB2486036B (en) * | 2011-06-15 | 2012-11-07 | Anthony Dwight Maunder | Process for liquefaction of natural gas |
| KR101392894B1 (en) * | 2012-07-23 | 2014-05-12 | 대우조선해양 주식회사 | Nitrogen rejection system for natural gas |
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| JP6225049B2 (en) * | 2013-12-26 | 2017-11-01 | 千代田化工建設株式会社 | Natural gas liquefaction system and method |
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| KR101669729B1 (en) * | 2014-11-13 | 2016-10-26 | 강희자 | Air liquefaction system using lng cold energy with ejector expansion device entraining expanded vapor |
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| JP6774905B2 (en) | 2017-04-19 | 2020-10-28 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Liquefied gas supply backup system and liquefied gas reserve supply method |
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- 2020-01-14 CN CN202080009703.4A patent/CN113330263B/en active Active
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| Publication number | Publication date |
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| CN113330263A (en) | 2021-08-31 |
| TW202028669A (en) | 2020-08-01 |
| EP3914869A1 (en) | 2021-12-01 |
| WO2020151991A1 (en) | 2020-07-30 |
| JP7393607B2 (en) | 2023-12-07 |
| SG11202107082RA (en) | 2021-07-29 |
| CN113330263B (en) | 2023-08-04 |
| JP2020118441A (en) | 2020-08-06 |
| KR20210115006A (en) | 2021-09-24 |
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