WO2015098124A1 - Natural gas liquefying system and liquefying method - Google Patents
Natural gas liquefying system and liquefying method Download PDFInfo
- Publication number
- WO2015098124A1 WO2015098124A1 PCT/JP2014/006501 JP2014006501W WO2015098124A1 WO 2015098124 A1 WO2015098124 A1 WO 2015098124A1 JP 2014006501 W JP2014006501 W JP 2014006501W WO 2015098124 A1 WO2015098124 A1 WO 2015098124A1
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- Prior art keywords
- raw material
- gas
- compressor
- material gas
- liquefaction
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 348
- 239000003345 natural gas Substances 0.000 title claims abstract description 150
- 238000000034 method Methods 0.000 title claims description 75
- 239000007789 gas Substances 0.000 claims abstract description 451
- 239000002994 raw material Substances 0.000 claims abstract description 313
- 238000001816 cooling Methods 0.000 claims abstract description 50
- 238000004821 distillation Methods 0.000 claims description 102
- 239000003507 refrigerant Substances 0.000 claims description 88
- 239000007788 liquid Substances 0.000 claims description 71
- 238000000926 separation method Methods 0.000 claims description 57
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 55
- 239000001294 propane Substances 0.000 claims description 27
- 238000007906 compression Methods 0.000 claims description 20
- 230000006835 compression Effects 0.000 claims description 18
- 239000007791 liquid phase Substances 0.000 claims description 17
- 239000012071 phase Substances 0.000 claims description 16
- 239000003949 liquefied natural gas Substances 0.000 claims description 15
- 238000011144 upstream manufacturing Methods 0.000 claims description 13
- 238000010248 power generation Methods 0.000 claims description 7
- 238000004804 winding Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 239000003570 air Substances 0.000 claims description 2
- 239000002826 coolant Substances 0.000 abstract description 3
- 230000007423 decrease Effects 0.000 abstract description 2
- 230000004048 modification Effects 0.000 description 105
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 12
- 239000005977 Ethylene Substances 0.000 description 12
- 229930195733 hydrocarbon Natural products 0.000 description 11
- 150000002430 hydrocarbons Chemical class 0.000 description 11
- 238000005057 refrigeration Methods 0.000 description 10
- 238000012546 transfer Methods 0.000 description 10
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 238000013459 approach Methods 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 5
- 238000009835 boiling Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 4
- 229910052753 mercury Inorganic materials 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000008646 thermal stress Effects 0.000 description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 101710187785 60S ribosomal protein L1-A Proteins 0.000 description 2
- 101710187786 60S ribosomal protein L1-B Proteins 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000003230 hygroscopic agent Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 239000003498 natural gas condensate Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
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Abstract
Description
図1は本発明の第1実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。また、後に示す表1は、第1実施形態に係る天然ガスの液化システムでの液化処理に関連するシミュレーション結果(表2~表12についても同様)である。表1には、第1実施形態に係る液化システム1において液化処理される天然ガス(以下、原料ガスという。)の温度、圧力、流量、及び各成分のモル分率等の一例を示す。表1における( i )-(ix)欄は、図1中にそれぞれ同じ番号( i )-(ix)が付された液化システム1の各位置における数値を示している。 (First embodiment)
FIG. 1 is a configuration diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the first embodiment of the present invention. Table 1 shown below is a simulation result related to the liquefaction process in the natural gas liquefaction system according to the first embodiment (the same applies to Tables 2 to 12). Table 1 shows an example of the temperature, pressure, flow rate, molar fraction of each component, and the like of natural gas (hereinafter referred to as source gas) to be liquefied in the
図2及び図3の構成図には、それぞれ本発明の第1実施形態に対応する第1及び第2参考例として、従来の天然ガスの液化システムにおける液化処理の流れを示す。図2及び図3に示す液化システム101、201では、第1実施形態に係る液化システム1に対応する構成要素についてはそれぞれ同一の符号が付されている。また、表2及び表3には、表1と同様に、それぞれ第1及び第2の参考例としての液化システム101、201における原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例が示されている。なお、第2の参考例の液化システム201は、上述の特許文献1(米国特許第4065278号明細書)の従来技術に基づき構成されたものである。 (First and second reference examples)
2 and 3 show the flow of liquefaction processing in a conventional natural gas liquefaction system as first and second reference examples corresponding to the first embodiment of the present invention, respectively. In the
図4は本発明の第1実施形態の第1変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図4に示す液化システム1では、第1実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (First modification of the first embodiment)
FIG. 4 is a configuration diagram showing the flow of the liquefaction process in the natural gas liquefaction system according to the first modification of the first embodiment of the present invention. In addition, in the
図5、図6及び図7は、それぞれ本発明の第1実施形態の第2、第3及び第4変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図5、図6及び図7に示す液化システム1では、第1実施形態(他の変形例を含む)に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Second, third, and fourth modifications of the first embodiment)
5, 6 and 7 are configuration diagrams showing the flow of the liquefaction process in the natural gas liquefaction system according to the second, third and fourth modifications of the first embodiment of the present invention, respectively. In addition, in the
図8は、本発明の第1実施形態の第5変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図8に示す液化システム1では、第1実施形態(他の変形例を含む)に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Fifth Modification of First Embodiment)
FIG. 8: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on the 5th modification of 1st Embodiment of this invention. In addition, in the
図9は、本発明の第1実施形態の第6変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。表4には、第6変形例の液化システムにおける原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例が示されている。また、表5には、液化システムで用いられる混合冷媒系の冷凍サイクルにおける冷媒の温度、圧力、流量、及び各成分のモル分率等の一例が示されている。なお、図9に示す液化システム1では、第1実施形態(他の変形例を含む)に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Sixth Modification of First Embodiment)
FIG. 9 is a configuration diagram showing the flow of the liquefaction process in the natural gas liquefaction system according to the sixth modification of the first embodiment of the present invention. Table 4 shows an example of the temperature, pressure, flow rate, and mole fraction of each component of the raw material gas in the liquefaction system of the sixth modified example. Table 5 shows an example of the refrigerant temperature, pressure, flow rate, molar fraction of each component, and the like in the mixed refrigerant refrigeration cycle used in the liquefaction system. In addition, in the
図10は、本発明の第1実施形態の第7変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。表6には、第7変形例の液化システムにおける原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例が示されている。なお、図10に示す液化システム1では、第1実施形態(他の変形例を含む)に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Seventh Modification of First Embodiment)
FIG. 10: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on the 7th modification of 1st Embodiment of this invention. Table 6 shows an example of the temperature, pressure, flow rate, and mole fraction of each component of the raw material gas in the liquefaction system of the seventh modified example. In addition, in the
図33は、本発明の第1実施形態の第8変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図33に示す液化システム1では、第1実施形態(他の変形例を含む)に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Eighth modification of the first embodiment)
FIG. 33 is a block diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the eighth modification of the first embodiment of the present invention. In addition, in the
This eighth modification has a configuration similar to that of the fifth modification described above, but the
図11は本発明の第2実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。また、表7には、第2実施形態に係る液化システム1における原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例を示す。なお、図11に示す液化システム1では、第1実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Second Embodiment)
FIG. 11 is a block diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the second embodiment of the present invention. Table 7 shows an example of the temperature, pressure, flow rate, and mole fraction of each component in the
図12は本発明の第3実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。また、表8には、第3実施形態に係る液化システム1における原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例を示す。なお、図12に示す液化システム1では、第1及び第2実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Third embodiment)
FIG. 12: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on 3rd Embodiment of this invention. Table 8 shows an example of the temperature, pressure, flow rate, and mole fraction of each component in the
図13は本発明の第3実施形態の変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図13に示す液化システム1では、第1から第3実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Modification of the third embodiment)
FIG. 13: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on the modification of 3rd Embodiment of this invention. In addition, in the
図14は本発明の第4実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。また、表9には、第4実施形態に係る液化システム1における原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例を示す。なお、図14に示す液化システム1では、第1から第3実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Fourth embodiment)
FIG. 14: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on 4th Embodiment of this invention. Table 9 shows an example of the temperature, pressure, flow rate, and mole fraction of each component in the
図15は本発明の第5実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図15に示す液化システム1では、第1から第4実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Fifth embodiment)
FIG. 15: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on 5th Embodiment of this invention. In addition, in the
図16は本発明の第6実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図16に示す液化システム1では、第1から第5実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Sixth embodiment)
FIG. 16: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on 6th Embodiment of this invention. In addition, in the
図17は本発明の第6実施形態の変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。また、表11には、第6実施形態の変形例に係る液化システム1における原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例を示す。なお、図17に示す液化システム1では、第6実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (First Modification of Sixth Embodiment)
FIG. 17: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on the modification of 6th Embodiment of this invention. Table 11 shows an example of the temperature, pressure, flow rate, and mole fraction of each component of the raw material gas in the
図18及び図19は、それぞれ本発明の第6実施形態の第2及び第3変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図18及び図19に示す液化システム1では、第6実施形態(他の変形例を含む)に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Second and third modifications of the sixth embodiment)
18 and 19 are configuration diagrams showing the flow of liquefaction processing in a natural gas liquefaction system according to second and third modifications of the sixth embodiment of the present invention, respectively. In addition, in the
図20は、本発明の第6実施形態の第4変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。表12には、第4変形例の液化システムにおける原料ガスの温度、圧力、流量、及び各成分のモル分率等の一例が示されている。なお、図20に示す液化システム1では、第6実施形態(他の変形例を含む)に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Fourth Modification of Sixth Embodiment)
FIG. 20: is a block diagram which shows the flow of the liquefaction process in the liquefaction system of the natural gas which concerns on the 4th modification of 6th Embodiment of this invention. Table 12 shows an example of the temperature, pressure, flow rate, and mole fraction of each component of the raw material gas in the liquefaction system of the fourth modified example. In addition, in the
図21は本発明の第7実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図21に示す液化システム1では、第1から第6実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Seventh embodiment)
FIG. 21 is a configuration diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the seventh embodiment of the present invention. In addition, in the
図22は本発明の第8実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図22に示す液化システム1では、第1から第7実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Eighth embodiment)
FIG. 22 is a configuration diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the eighth embodiment of the present invention. In addition, in the
図23及び図24は、それぞれ本発明の第8実施形態の第1及び第2変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図23及び図24に示す液化システム1では、第8実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (First and second modifications of the eighth embodiment)
FIGS. 23 and 24 are configuration diagrams showing the flow of liquefaction processing in the natural gas liquefaction system according to the first and second modifications of the eighth embodiment of the present invention, respectively. In addition, in the
図25は本発明の第9実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図25に示す液化システム1では、第1から第8実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Ninth embodiment)
FIG. 25 is a configuration diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the ninth embodiment of the present invention. In addition, in the
図26は本発明の第9実施形態の変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図26に示す液化システム1では、第9実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Modification of the ninth embodiment)
FIG. 26 is a block diagram showing the flow of liquefaction processing in a natural gas liquefaction system according to a modification of the ninth embodiment of the present invention. In addition, in the
図27は本発明の第10実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図27に示す液化システム1では、第1から第9実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (10th Embodiment)
FIG. 27 is a configuration diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the tenth embodiment of the present invention. In addition, in the
図28及び図29は、それぞれ本発明の第10実施形態の第1及び第2変形例に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図28及び図29に示す液化システム1では、第10実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (First and second modifications of the tenth embodiment)
FIGS. 28 and 29 are configuration diagrams showing the flow of liquefaction processing in the natural gas liquefaction system according to the first and second modifications of the tenth embodiment of the present invention, respectively. In addition, in the
図30は本発明の第11実施形態に係る天然ガスの液化システムにおける液化処理の流れを示す構成図である。なお、図30に示す液化システム1では、第1から第10実施形態に係る液化システム1と同様の構成要素についてはそれぞれ同一の符号を付し、以下で言及する事項を除いて詳細な説明を省略する。 (Eleventh embodiment)
FIG. 30 is a configuration diagram showing the flow of liquefaction processing in the natural gas liquefaction system according to the eleventh embodiment of the present invention. In addition, in the
図31及び図32は、それぞれ上述の各実施形態における膨張機と圧縮機との機械的接続構造の第1及び第2変形例を示す図である。 (Modification of connection structure of expander and compressor)
FIGS. 31 and 32 are views showing first and second modifications of the mechanical connection structure between the expander and the compressor in each of the above-described embodiments.
2 水分除去装置
3、3a 第1膨張機
3b 第2膨張機
4、4a 第1圧縮機
4b 第3圧縮機
5 シャフト
10、11、12 第1冷却器
15 蒸留装置
21 液化装置
23 第1気液分離槽
33 膨張弁
41 冷媒セパレータ
44 膨張弁
45 スプレーヘッダ
54 膨張弁
55 スプレーヘッダ
69 熱交換器
71 第4圧縮機
72 第4冷却器
75 第2圧縮機
81 モータ(第1モータ)
82 コントローラ
83 圧力計
84 モータ(第2モータ)
85 第2冷却器
86 第3冷却器
87 発電装置
89 膨張弁
91 セパレータ
92 膨張弁
96 ギヤ
97 ギヤ
98 ギヤ
Z1 暖温領域
Z2 中間領域
Z3 冷温領域 DESCRIPTION OF
82
85 Second cooler 86 Third cooler 87
Claims (22)
- 天然ガスを冷却して液化天然ガスを生成する天然ガスの液化システムであって、
加圧状態で得られた天然ガスを原料ガスとして膨張させることによって動力を発生させる第1膨張機と、
前記第1膨張機における膨張によって減圧された前記原料ガスを冷却する第1冷却器と、
前記第1冷却器によって冷却された前記原料ガスを蒸留することにより、前記原料ガス中の重質分を低減または除去する蒸留装置と、
前記第1膨張機において発生した動力を利用することにより、前記蒸留装置において前記重質分が低減または除去された前記原料ガスを圧縮する第1圧縮機と、
前記第1圧縮機によって圧縮された前記原料ガスを冷媒との熱交換によって液化する液化装置と
を備えたことを特徴とする天然ガスの液化システム。 A natural gas liquefaction system that cools natural gas to produce liquefied natural gas,
A first expander that generates power by expanding natural gas obtained in a pressurized state as a raw material gas;
A first cooler for cooling the source gas decompressed by expansion in the first expander;
A distillation apparatus for reducing or removing heavy components in the raw material gas by distilling the raw material gas cooled by the first cooler;
A first compressor that compresses the raw material gas from which the heavy component has been reduced or removed in the distillation apparatus by utilizing power generated in the first expander;
A natural gas liquefaction system comprising: a liquefaction device that liquefies the raw material gas compressed by the first compressor by heat exchange with a refrigerant. - 前記第1圧縮機と前記液化装置との間に配置され、前記第1圧縮機によって圧縮された前記原料ガスを冷却する第2冷却器を更に備えたことを特徴とする請求項1に記載の天然ガスの液化システム。 2. The apparatus according to claim 1, further comprising a second cooler disposed between the first compressor and the liquefaction device and configured to cool the raw material gas compressed by the first compressor. Natural gas liquefaction system.
- 前記液化装置は、スプール巻き型熱交換器からなり、
前記第1圧縮機から送出された前記原料ガスは、前記スプール巻き型熱交換器に対し、当該スプール巻き型熱交換器内の高温側に位置する暖温領域に導入されることを特徴とする請求項1または請求項2に記載の天然ガスの液化システム。 The liquefaction device comprises a spool-winding heat exchanger,
The raw material gas delivered from the first compressor is introduced into a warm temperature region located on a high temperature side in the spool-winding heat exchanger with respect to the spool-winding heat exchanger. The natural gas liquefaction system according to claim 1 or 2. - 前記第1圧縮機と前記液化装置との間に配置され、前記第1圧縮機から送出された前記原料ガスを昇圧する第2圧縮機を更に備えたことを特徴とする請求項1に記載の天然ガスの液化システム。 2. The apparatus according to claim 1, further comprising a second compressor that is disposed between the first compressor and the liquefaction device and pressurizes the source gas sent from the first compressor. Natural gas liquefaction system.
- 外部からの電力によって駆動され、前記液化装置に導入される前記原料ガスの圧力値に基づき駆動制御される第1モータを更に備え、
前記第2圧縮機は、前記第1モータによって駆動されることを特徴とする請求項4に記載の天然ガスの液化システム。 A first motor that is driven by electric power from the outside and that is driven and controlled based on the pressure value of the source gas introduced into the liquefaction device;
5. The natural gas liquefaction system according to claim 4, wherein the second compressor is driven by the first motor. - 前記第2圧縮機と前記液化装置との間に配置され、前記原料ガスを冷却する第2冷却器を更に備えたことを特徴とする請求項4に記載の天然ガスの液化システム。 The natural gas liquefaction system according to claim 4, further comprising a second cooler disposed between the second compressor and the liquefaction device for cooling the raw material gas.
- 前記第1膨張機において発生した動力を電力に変換する発電装置と、
前記第1圧縮機を駆動する第2モータと
を更に備え、
前記第2モータは、前記発電装置からの電力を利用して駆動されることを特徴とする請求項1に記載の天然ガスの液化システム。 A power generation device that converts power generated in the first expander into electric power;
A second motor for driving the first compressor;
2. The natural gas liquefaction system according to claim 1, wherein the second motor is driven using electric power from the power generation device. - 前記第1膨張機と前記第1圧縮機とを機械的に連結し、外部からの電力供給を受ける第2モータを更に備え、
前記第1圧縮機は、前記第1膨張機において発生した動力と、前記第2モータの動力とを利用することにより、前記原料ガスを圧縮することを特徴とする請求項1に記載の天然ガスの液化システム。 A second motor that mechanically connects the first expander and the first compressor and receives an external power supply;
The natural gas according to claim 1, wherein the first compressor compresses the raw material gas by using power generated in the first expander and power of the second motor. Liquefaction system. - 前記第1圧縮機には、前記蒸留装置において前記重質分が低減または除去された前記原料ガスが直接導入され、
前記第1圧縮機において圧縮された前記原料ガスが前記液化装置を介して導入される第1気液分離槽を備え、
前記第1気液分離槽において分離された前記原料ガスの気相成分は、前記液化装置に再び導入される一方、前記原料ガスの液相成分は、前記蒸留装置に環流されることを特徴とする請求項1に記載の天然ガスの液化システム。 The first compressor is directly introduced with the raw material gas from which the heavy component has been reduced or removed in the distillation apparatus,
A first gas-liquid separation tank into which the source gas compressed in the first compressor is introduced via the liquefaction device;
The gas phase component of the source gas separated in the first gas-liquid separation tank is reintroduced into the liquefaction device, while the liquid phase component of the source gas is circulated to the distillation device. The natural gas liquefaction system according to claim 1. - 前記第1圧縮機と前記第1気液分離槽との間に配置され、前記原料ガスを冷却する第2冷却器を更に備えたことを特徴とする請求項9に記載の天然ガスの液化システム。 The natural gas liquefaction system according to claim 9, further comprising a second cooler disposed between the first compressor and the first gas-liquid separation tank to cool the raw material gas. .
- 前記第1膨張機と前記蒸留装置との間に配置され、前記原料ガスを膨張させることによって動力を発生させる第2膨張機と、
前記蒸留装置と前記第1圧縮機との間に配置され、第2膨張機において発生した動力を利用することにより、前記蒸留装置によって蒸留された前記原料ガスを圧縮する第3圧縮機と
を更に備えたことを特徴とする請求項1に記載の天然ガスの液化システム。 A second expander that is disposed between the first expander and the distillation device and generates power by expanding the source gas;
A third compressor that is disposed between the distillation apparatus and the first compressor and that compresses the raw material gas distilled by the distillation apparatus by using power generated in the second expander; The natural gas liquefaction system according to claim 1, further comprising: - 前記第1膨張機と並列に配置され、前記原料ガスを膨張させることによって動力を発生させる第2膨張機と、
前記蒸留装置と前記第1圧縮機との間に配置され、第2膨張機において発生した動力を利用することにより、前記蒸留装置によって蒸留された前記原料ガスを圧縮する第3圧縮機と
を更に備えたことを特徴とする請求項1に記載の天然ガスの液化システム。 A second expander that is arranged in parallel with the first expander and generates power by expanding the source gas;
A third compressor that is disposed between the distillation apparatus and the first compressor and that compresses the raw material gas distilled by the distillation apparatus by using power generated in the second expander; The natural gas liquefaction system according to claim 1, further comprising: - 前記液化装置は、プレートフィン型熱交換器であることを特徴とする請求項1に記載の天然ガスの液化システム。 The natural gas liquefaction system according to claim 1, wherein the liquefaction device is a plate fin type heat exchanger.
- 前記第1圧縮機で圧縮された前記原料ガスの圧力は、5,171kPaAよりも高いことを特徴とする請求項1に記載の天然ガスの液化システム。 The natural gas liquefaction system according to claim 1, wherein the pressure of the raw material gas compressed by the first compressor is higher than 5,171 kPaA.
- 前記第2圧縮機で圧縮された前記原料ガスの圧力は、5,171kPaAよりも高いことを特徴とする請求項4または請求項5に記載の天然ガスの液化システム。 The natural gas liquefaction system according to claim 4 or 5, wherein the pressure of the raw material gas compressed by the second compressor is higher than 5,171 kPaA.
- 前記蒸留装置に導入される前記原料ガスと、前記蒸留装置からの塔頂留出物との熱交換を行う熱交換器を更に備えたことを特徴とする請求項1から請求項8のいずれかに記載の天然ガスの液化システム。 The heat exchanger which heat-exchanges the said raw material gas introduce | transduced into the said distillation apparatus, and the tower top distillate from the said distillation apparatus was further provided. The natural gas liquefaction system described in 1.
- 前記蒸留装置からの塔頂留出物が導入される第1気液分離槽と、
前記蒸留装置と前記第1気液分離槽との間に配置され、前記蒸留装置からの前記塔頂留出物を冷却する第3冷却器とを更に備えたことを特徴とする請求項1から請求項8のいずれかに記載の天然ガスの液化システム。 A first gas-liquid separation tank into which the top distillate from the distillation apparatus is introduced;
The apparatus further comprises a third cooler disposed between the distillation apparatus and the first gas-liquid separation tank and configured to cool the top distillate from the distillation apparatus. The natural gas liquefaction system according to claim 8. - 前記第1圧縮機に導入される前記原料ガスと、前記第1圧縮機において圧縮された後の前記原料ガスとの熱交換を行う第2熱交換器を更に備えたことを特徴とする請求項1から請求項8のいずれかに記載の天然ガスの液化システム。 The apparatus further comprises a second heat exchanger that performs heat exchange between the raw material gas introduced into the first compressor and the raw material gas after being compressed in the first compressor. The natural gas liquefaction system according to any one of claims 1 to 8.
- 前記第1圧縮機において圧縮された後の前記原料ガスを、前記第2熱交換器の上流側において、水、空気、及びプロパン冷媒のいずれかによって冷却する第5冷却器を更に備えたことを特徴とする請求項18に記載の天然ガスの液化システム。 The apparatus further comprises a fifth cooler that cools the raw material gas after being compressed in the first compressor with water, air, or propane refrigerant on the upstream side of the second heat exchanger. The natural gas liquefaction system according to claim 18, wherein the liquefaction system is natural.
- 前記第1圧縮機において圧縮された後の前記原料ガスと、前記蒸留装置からの塔頂留出物との熱交換を行う第3熱交換器を更に備えたことを特徴とする請求項18に記載の天然ガスの液化システム。 19. The apparatus according to claim 18, further comprising a third heat exchanger that exchanges heat between the raw material gas compressed in the first compressor and a column top distillate from the distillation apparatus. The natural gas liquefaction system described.
- 天然ガスを冷却して液化天然ガスを生成する天然ガスの液化システムであって、
加圧状態で得られた天然ガスを原料ガスとして膨張させることによって動力を発生させる第1膨張機と、
前記第1膨張機における膨張によって減圧された前記原料ガスを蒸留することにより、前記原料ガス中の重質分を低減または除去する蒸留装置と、
前記第1膨張機において発生した動力を利用することにより、前記蒸留装置において前記重質分が低減または除去された前記原料ガスを圧縮する第1圧縮機と、
前記第1圧縮機によって圧縮された前記原料ガスを冷媒との熱交換によって液化する液化装置と
を備えたことを特徴とする天然ガスの液化システム。 A natural gas liquefaction system that cools natural gas to produce liquefied natural gas,
A first expander that generates power by expanding natural gas obtained in a pressurized state as a raw material gas;
A distillation apparatus for reducing or removing heavy components in the raw material gas by distilling the raw material gas decompressed by the expansion in the first expander;
A first compressor that compresses the raw material gas from which the heavy component has been reduced or removed in the distillation apparatus by utilizing power generated in the first expander;
A natural gas liquefaction system comprising: a liquefaction device that liquefies the raw material gas compressed by the first compressor by heat exchange with a refrigerant. - 天然ガスを冷却して液化天然ガスを生成する天然ガスの液化方法であって、
加圧状態で得られた天然ガスを原料ガスとして膨張させることによって動力を発生させる第1膨張工程と、
前記第1膨張工程における膨張によって減圧された前記原料ガスを冷却する第1冷却工程と、
前記第1冷却工程によって冷却された前記原料ガスを蒸留することにより、前記原料ガス中の重質分を低減または除去する蒸留工程と、
前記第1膨張工程において発生した動力を利用することにより、前記蒸留工程において前記重質分が低減または除去された前記原料ガスを圧縮する第1圧縮工程と、
前記第1圧縮工程によって圧縮された前記原料ガスを冷媒との熱交換によって液化する液化工程と
を備えたことを特徴とする天然ガスの液化方法。 A natural gas liquefaction method for cooling natural gas to produce liquefied natural gas,
A first expansion step for generating power by expanding natural gas obtained under pressure as a raw material gas;
A first cooling step for cooling the source gas decompressed by the expansion in the first expansion step;
A distillation step of reducing or removing heavy components in the raw material gas by distilling the raw material gas cooled in the first cooling step;
A first compression step of compressing the raw material gas from which the heavy component has been reduced or removed in the distillation step by utilizing the power generated in the first expansion step;
A natural gas liquefaction method comprising: a liquefaction step of liquefying the raw material gas compressed in the first compression step by heat exchange with a refrigerant.
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KR1020167030036A KR101894076B1 (en) | 2013-12-26 | 2014-12-26 | Natural gas liquefying system and liquefying method |
EP16201992.1A EP3168558B1 (en) | 2013-12-26 | 2014-12-26 | System and method for liquefaction of natural gas |
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2016
- 2016-06-24 SA SA516371407A patent/SA516371407B1/en unknown
- 2016-06-24 SA SA516380183A patent/SA516380183B1/en unknown
- 2016-10-14 US US15/293,485 patent/US20170030633A1/en not_active Abandoned
- 2016-10-24 AU AU2016250325A patent/AU2016250325B2/en active Active
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Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2017013329A1 (en) * | 2015-07-23 | 2017-01-26 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for purifying a gas rich in hydrocarbons |
FR3039080A1 (en) * | 2015-07-23 | 2017-01-27 | Air Liquide | METHOD OF PURIFYING HYDROCARBON-RICH GAS |
US11060037B2 (en) | 2015-07-23 | 2021-07-13 | L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Method for purifying a gas rich in hydrocarbons |
AU2016296356B2 (en) * | 2015-07-23 | 2021-08-12 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for purifying a gas rich in hydrocarbons |
EP3252408A1 (en) * | 2016-06-02 | 2017-12-06 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for purifying natural gas and for liquefying carbon dioxide |
FR3052241A1 (en) * | 2016-06-02 | 2017-12-08 | L'air Liquide Sa Pour L'etude Et L'exploitation Des Procedes Georges Claude | PROCESS FOR PURIFYING NATURAL GAS AND LIQUEFACTING CARBON DIOXIDE |
US10415879B2 (en) | 2016-06-02 | 2019-09-17 | L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Process for purifying natural gas and liquefying carbon dioxide |
CN107642949A (en) * | 2016-07-21 | 2018-01-30 | 气体产品与化学公司 | Liquefaction lean gas removes heavy hydrocarbon system |
CN107642949B (en) * | 2016-07-21 | 2020-03-06 | 气体产品与化学公司 | System for removing heavy hydrocarbon from liquefied lean gas |
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