JP5325284B2 - 炭化水素流の液化方法及び装置 - Google Patents
炭化水素流の液化方法及び装置 Download PDFInfo
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- JP5325284B2 JP5325284B2 JP2011503419A JP2011503419A JP5325284B2 JP 5325284 B2 JP5325284 B2 JP 5325284B2 JP 2011503419 A JP2011503419 A JP 2011503419A JP 2011503419 A JP2011503419 A JP 2011503419A JP 5325284 B2 JP5325284 B2 JP 5325284B2
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- methane
- refrigerant
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- liquefied
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- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 118
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 117
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 101
- 238000000034 method Methods 0.000 title claims abstract description 68
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 242
- 238000011084 recovery Methods 0.000 claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 239000003507 refrigerant Substances 0.000 claims description 171
- 239000007789 gas Substances 0.000 claims description 51
- 238000001816 cooling Methods 0.000 claims description 45
- 239000003345 natural gas Substances 0.000 claims description 22
- 230000008569 process Effects 0.000 claims description 19
- 239000003949 liquefied natural gas Substances 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 239000000284 extract Substances 0.000 claims 1
- 230000008859 change Effects 0.000 abstract description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 20
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 239000001294 propane Substances 0.000 description 10
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 9
- 230000006835 compression Effects 0.000 description 9
- 238000007906 compression Methods 0.000 description 9
- 230000001276 controlling effect Effects 0.000 description 8
- 239000001273 butane Substances 0.000 description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- 239000000446 fuel Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910001868 water Inorganic materials 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 4
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- GJVFBWCTGUSGDD-UHFFFAOYSA-L pentamethonium bromide Chemical compound [Br-].[Br-].C[N+](C)(C)CCCCC[N+](C)(C)C GJVFBWCTGUSGDD-UHFFFAOYSA-L 0.000 description 3
- 150000003464 sulfur compounds Chemical class 0.000 description 3
- -1 H 2 O Chemical class 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000004781 supercooling Methods 0.000 description 2
- 238000011282 treatment Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- MWRWFPQBGSZWNV-UHFFFAOYSA-N Dinitrosopentamethylenetetramine Chemical compound C1N2CN(N=O)CN1CN(N=O)C2 MWRWFPQBGSZWNV-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229940112112 capex Drugs 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- FEBLZLNTKCEFIT-VSXGLTOVSA-N fluocinolone acetonide Chemical compound C1([C@@H](F)C2)=CC(=O)C=C[C@]1(C)[C@]1(F)[C@@H]2[C@@H]2C[C@H]3OC(C)(C)O[C@@]3(C(=O)CO)[C@@]2(C)C[C@@H]1O FEBLZLNTKCEFIT-VSXGLTOVSA-N 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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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
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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Description
米国特許第4,541,852号には、LNGを過冷却し、減圧し、更にフラッシング(flashing)(瞬間蒸発)してガス相天然ガスを回収することにより、閉鎖サイクル冷媒から圧縮力を再分配する天然ガスの液化、過冷却システムが記載されている。次いで、ガス相天然ガスは再圧縮され、システムの原料に再循環される。
(a)NGL回収システム、1つ以上の主冷媒圧縮器を備えた主冷媒回路、及び1つ以上の第一冷媒圧縮器を備えた第一冷媒回路、並びに減圧用デバイス及びこれに続く気液分離器を少なくとも有する液化システムを用意する工程、
(b)炭化水素原料流を前記NGL回収システムに通して該炭化水素原料流からメタンに富む塔頂流を生成する工程、
(c)前記メタンに富む塔頂流を第一圧縮器に通してメタン圧縮流を得る工程、
(d)前記メタン圧縮流を前記第一冷媒回路において第一冷媒で冷却し、引続き該メタン圧縮流を前記主冷媒回路において主冷媒で液化して、第一液化流を得る工程、
(e)前記第一液化流の圧力を低下させて、混合相流を得る工程、
(f)前記混合相流を最終気液分離器に通して最終ガス流及び液化炭化水素製品流を得る工程、
(g)前記最終ガス流の少なくとも一再循環画分を、前記第一冷媒回路における第一冷媒での前記冷却工程の少なくとも一部の上流の前記メタンに富む塔頂流又は前記メタン圧縮流に供給する工程、
(h)前記第一液化流の温度Txを調節して前記最終気液分離器からの最終ガス流の量を変化させると共に、工程(g)に供給される最終ガス流の再循環画分の量を制御することにより、前記1つ以上の主冷媒圧縮器及び前記1つ以上の第一冷媒圧縮器の負荷動力を最大負荷に最大化する工程、
を少なくとも含む炭化水素流の液化方法を提供する。
炭化水素原料流からC2+流を抽出して、少なくとも、メタンに富む塔頂流及びC2+に富む塔底流を得るためのNGL回収システム;
前記メタンに富む塔頂流からメタン圧縮流を得るための少なくとも第一の圧縮器、
前記メタン圧縮流を冷却して冷却メタン圧縮流を得るための第一冷却段(stage)、及び引続き該冷却メタン圧縮流を液化して第一液化流を得るための主冷却段であって、該第一冷却段は1つ以上の第一冷媒圧縮器を備えた第一冷媒回路を有し、前記主冷却段階は1つ以上の主冷媒圧縮器を備えた主冷媒回路を有する、該第一及び主冷却段;
前記第一液化流の圧力を低下させて混合相流を得るための減圧用デバイス;
前記混合相流を最終ガス流及び液化炭化水素製品流に分離するための最終気液分離器;
前記最終ガス流の少なくとも一再循環画分を、前記メタンに富む塔頂流に供給するための再循環画分ライン;及び
前記第一液化流の温度Txを調節して前記最終気液分離器からの最終ガス流の量を変化させると共に、前記再循環画分ライン中の最終圧縮流の再循環画分の量を制御することにより、前記1つ以上の主冷媒圧縮器及び前記1つ以上の第一冷媒圧縮器の負荷動力を最大負荷で最大化するために配列された制御システム;
を少なくとも有する炭化水素流の液化装置を提供する。
本発明の実施態様及び実施例を単なる例示により添付の非限定的図面を参照して説明する。
炭化水素原料流10からC2+流を抽出して、少なくとも、メタンに富む塔頂流20及びC2+に富む塔底流30を得るためのNGL回収システム12;
前記メタン圧縮流40を液化して第一液化流50を得るための主冷却段42;
前記第一液化流50の圧力を低下させて混合相流60を得るための減圧用デバイス52;
前記最終ガス流70を圧縮して最終圧縮流90を得るための1つ以上の最終圧縮器72;及び
前記最終圧縮塔頂流90の少なくとも一再循環画分を前記メタンに富む塔頂流20に供給するために、前記最終圧縮流90を前記メタンに富む塔頂流20と接続させる再循環画分ライン90b;
を有する。
炭化水素原料流10を用意する工程;
前記炭化水素原料流10をNGL回収システム12に通して炭化水素原料流10を少なくとも、メタンに富む塔頂流20及びC2+に富む塔底流30に分離する工程;
前記メタン圧縮流40を液化して第一液化流50を得る工程;
前記第一液化流50の圧力を低下させて、混合相流60を得る工程;
前記最終ガス流70を1つ以上の最終圧縮器72に通して最終圧縮流90を得る工程;及び
前記最終圧縮流72の少なくとも一再循環画分90bを、前記メタンに富む塔頂流20に供給する工程;
を含む。
供給源によっては炭化水素流は、H2O、N2、CO2、Hg、H2S及びその他の硫黄化合物等の1種以上の非炭化水素を含有してもよい。
或いは及び/又は更に、NGL回収システム12は、炭化水素原料を膨張させてNGL回収塔14用の混合相原料流16を得るための少なくとも第一の膨張器15(図2に示す)を備えてよい。
再循環画分90bは、第一圧縮器24の上流にある配合器21によりメタンに富む塔頂流20に容易に供給できるように、メタンに富む塔頂流20と同じか同様の圧力であるのが都合良い。
図2において、炭化水素原料流10は、NGL回収システム12に通す前に、第一熱交換器110、好ましくは低圧平釜(kettle)熱交換器である第二熱交換器112、及び第三熱交換器114に通される。この方法では、炭化水素原料流10は0℃未満に低下できる。圧力は40〜80バール、好ましくは45〜80バールの範囲のいずれでもよい。
(i)前述のように炭化水素原料流10を液化する工程、
(ii)図3に示す第一液化流50の温度Txを調節して最終気液分離器62からの最終ガス流70の量を変化させる工程、及び
(iii)再循環画分としてメタンに富む流れ20に供給される最終圧縮流90の再循環画分90bの量を制御する工程、
を含む炭化水素原料流10の液化方法も提供する。
この方法ではユーザーは、ここに供給される炭化水素原料流10の液化を制御する方法に従って、所定の炭化水素原料流のためにこれら圧縮器駆動器間の動力負荷をシフトすることにより、液化方法を制御できる。
通常、抑制される駆動器は液化方法において大型駆動器である第一冷媒圧縮器駆動器D2又は主冷媒圧縮器駆動器D3である。
主冷媒回路44、1つ以上の主冷媒圧縮器45、第一冷媒回路100及び1つ以上の第一冷媒圧縮器101を含む、前述のような炭化水素原料流10の液化を制御する工程、及び
1つ以上の主冷媒圧縮器45及び第一冷媒圧縮器101を最大負荷で駆動する工程、
を少なくとも含む、液化炭化水素製品流80の生産量を最大化する方法も提供する。
液化炭化水素流は液化天然ガス流であってよい。
12 NGL回収システム
13 バルブ
14 NGL回収塔
15 第一膨張器又はNGL膨張器
16 混合相原料流
17 予備NGL分離器
18 塔底液流
19 塔頂ガス流
20 メタンに富む塔頂流
21 配合器
24 第一圧縮器
25 中間冷却器
26 第一冷却器
27 ドライブシャフト
30 C2+に富む塔底流
30 C2+に富む塔底流
31 塔頂流
32 ターボ圧縮器
40 メタン圧縮流
40a 冷却メタン圧縮流
41 バルブ
42 主冷却段又は主冷媒回路
43 中間冷却器
44 主冷媒回路
45 主圧縮器
45a 第一主冷媒圧縮器
45b 第二主冷媒圧縮器
46 加圧冷媒流
47 冷却器
48 圧縮冷媒流又は冷却加圧冷媒流
49 更に冷却された加圧冷媒流
50 第一液化流
51 膨張器
52 減圧用デバイス又はバルブ
53 流れ制御バルブ
54 主極低温熱交換器(MCHE)
55 冷媒分離器
56 軽質冷媒流
57 重質冷媒流
58a バルブ又は膨張器
58b バルブ及び/又は膨張器
60 混合相流
62 最終フラッシュ容器又は最終気液分離器
70 最終フラッシュガス又は最終ガス流
72 最終圧縮器
80 液化炭化水素製品流
90 最終圧縮(塔頂)流
90a 燃料画分
90b 最終圧縮流の再循環画分(ライン)
91 最終流れ分割器
92b 最終圧縮流の再循環画分
90b 再循環画分(ライン)
100 第一冷媒回路
101 第一冷媒圧縮器
102 冷却器
103 バルブ
104 冷却膨張冷媒流冷媒流
105a 第一高圧(HP)平釜熱交換器
105b 第一高圧(HP)平釜熱交換器
106a 中間圧(MP)平釜熱交換器
106b 中間圧(MP)平釜熱交換器
107a 低圧(LP)平釜熱交換器
107c 低圧(LP)平釜熱交換器
108 圧縮冷媒流
110 第一熱交換器
112 第二熱交換器又は低圧平釜熱交換器
114 第三熱交換器
116 第四熱交換器又は第四熱交換システム
116a 第四高圧(HP)(平釜)熱交換器
116b 第四中間圧(MP)熱交換器
116c 第四低圧(LP)熱交換器
118 第五熱交換器システム
118a 第五高圧(HP)平釜熱交換器
118b 第五高圧(HP)平釜熱交換器
118c 第五低圧(LP)平釜熱交換器
120 第一熱交換器又は第一熱交換システム
122 第一熱交換システムの破断四角形
124a 別の冷却流
200 制御システム
201 再循環バルブ
D1 第一圧縮器駆動器
D2 第一冷媒圧縮器駆動器
D3 主冷媒圧縮器駆動器
D4 最終圧縮器駆動器
Claims (19)
- (a)NGL回収システム、1つ以上の主冷媒圧縮器を備えた主冷媒回路、及び1つ以上の第一冷媒圧縮器を備えた第一冷媒回路、並びに減圧用デバイス及びこれに続く気液分離器を少なくとも有する液化システムを用意する工程、
(b)炭化水素原料流を前記NGL回収システムに通して該炭化水素原料流からメタンに富む塔頂流を生成する工程、
(c)前記メタンに富む塔頂流を第一圧縮器に通してメタン圧縮流を得る工程、
(d)前記メタン圧縮流を前記第一冷媒回路において第一冷媒で冷却し、引続き該メタン圧縮流を前記主冷媒回路において主冷媒で液化して、第一液化流を得る工程、
(e)前記第一液化流の圧力を低下させて、混合相流を得る工程、
(f)前記混合相流を最終気液分離器に通して最終ガス流及び液化炭化水素製品流を得る工程、
(g)前記最終ガス流の少なくとも一再循環画分を、前記第一冷媒回路における第一冷媒での前記冷却工程の少なくとも一部の上流の前記メタンに富む塔頂流又は前記メタン圧縮流に供給する工程、
(h)前記第一液化流の温度Txを調節して前記最終気液分離器からの最終ガス流の量を変化させると共に、工程(g)に供給される最終ガス流の再循環画分の量を制御することにより、前記1つ以上の主冷媒圧縮器及び前記1つ以上の第一冷媒圧縮器の負荷動力を最大負荷とする工程、
を少なくとも含む炭化水素流の液化方法。 - 工程(b)における前記メタンに富む塔頂流の生成工程が、前記炭化水素原料流からC2+流を抽出すると共に、C2+に富む塔底流を得る工程を含む請求項1に記載の方法。
- 前記NGL回収システムが、膨張器;NGL回収塔;及び該膨張器により駆動するため、該膨張器と機械的に連結した1つ以上のターボ圧縮器;を備えると共に、工程(b)が、前記炭化水素原料流の少なくとも1つの画分を前記膨張器に通して混合相原料流を得る工程、該混合相原料流を前記NGL回収塔に通して塔頂流を製造する工程、及び該塔頂流を前記ターボ圧縮器に通して前記メタンに富む塔頂流を精製する工程、を含む請求項1又は2に記載の方法。
- 前記NGL回収塔での圧力が、40バール未満である請求項3に記載の方法。
- 前記NGL回収塔での圧力が、35バール以下である請求項3に記載の方法。
- 前記NGL回収塔での圧力が、15〜45バールの範囲である請求項3に記載の方法。
- 前記NGL回収塔での圧力が、20〜35バールの範囲である請求項3に記載の方法。
- 前記第一冷媒回路が、前記炭化水素原料流を冷却するための1つ以上の熱交換器及び前記メタン圧縮流を冷却するための1つ以上の熱交換器を備える請求項1〜7のいずれか1項に記載の方法。
- 工程(g)の前に、前記最終ガス流を1つ以上の最終圧縮器に通して最終圧縮流を得る工程であって、該最終圧縮流から該最終圧縮流の再循環画分が引抜かれる該工程を更に含む請求項1〜8のいずれか1項に記載の方法。
- 前記最終圧縮流の再循環画分の圧力が15〜45バールの範囲である請求項1〜9のいずれか1項に記載の方法。
- 前記第一圧縮器が、第一冷媒圧縮器の少なくとも1つで共同に駆動される請求項1〜10のいずれか1項に記載の方法。
- 前記炭化水素原料流が天然ガス流であり、前記液化炭化水素製品流が液化天然ガス流である請求項1〜11のいずれか1項に記載の方法。
- 工程(h)における前記第一液化流の温度Txの調節工程、及び工程(g)に供給される最終ガス流の再循環画分の量の制御工程により、前記液化炭化水素製品流の生産量が増大する、請求項1〜12のいずれか1項に記載の方法。
- 工程(h)における前記第一液化流の温度T x の調節工程、及び工程(g)に供給される最終ガス流の再循環画分の量の制御工程により、前記液化炭化水素製品流の生産量が最大化大する、請求項1〜12のいずれか1項に記載の方法。
- 工程(h)における前記負荷動力の最大化工程が、前記第一冷媒圧縮器と前記主冷媒圧縮器との間の動力負荷をシフトする工程を含む、請求項1〜14のいずれか1項に記載の方法。
- 炭化水素原料流からC2+流を抽出して、少なくとも、メタンに富む塔頂流及びC2+に富む塔底流を得るためのNGL回収システム;
前記メタンに富む塔頂流からメタン圧縮流を得るための少なくとも第一の圧縮器、
前記メタン圧縮流を冷却して冷却メタン圧縮流を得るための第一冷却段、及び引続き該冷却メタン圧縮流を液化して第一液化流を得るための主冷却段であって、該第一冷却段は1つ以上の第一冷媒圧縮器を備えた第一冷媒回路を有し、前記主冷却段階は1つ以上の主冷媒圧縮器を備えた主冷媒回路を有する、該第一及び主冷却段;
前記第一液化流の圧力を低下させて混合相流を得るための減圧用デバイス;
前記混合相流を最終ガス流及び液化炭化水素製品流に分離するための最終気液分離器;
前記最終ガス流の少なくとも一再循環画分を、前記メタンに富む塔頂流に供給するための再循環画分ライン;及び
前記第一液化流の温度Txを調節して前記最終気液分離器からの最終ガス流の量を変化させると共に、前記再循環画分ライン中の最終圧縮流の再循環画分の量を制御することにより、前記1つ以上の主冷媒圧縮器及び前記1つ以上の第一冷媒圧縮器の負荷動力を最大負荷とするために配列された制御システム;
を少なくとも有する炭化水素流の液化装置。 - 前記NGL回収システムが、
前記炭化水素原料の少なくとも1つの画分を膨張させて混合相原料流を得るために配列された膨張器:
前記混合相原料流を受取ると共に、塔頂流を製造するためのNGL回収;及び
前記膨張器により駆動されて、前記塔頂流を受取る共に、前記メタンに富む塔頂流を生成するための、該膨張器と機械的に連結した1つ以上のターボ圧縮器;
を有する請求項16に記載の装置。 - 前記最終ガス流を圧縮して最終圧縮流を得るための1つ以上の最終圧縮器であって、前記再循環画分ラインにより前記最終圧縮流が前記メタンに富む塔頂流と接続する該最終圧縮器を更に備える請求項16又は17に記載の装置。
- 前記1つ以上の第一圧縮器のうちの少なくとも1つ及び前記第一圧縮器が機械的に連結され、共同に駆動される請求項16〜18のいずれか1項に記載の装置。
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US12/100,287 US8534094B2 (en) | 2008-04-09 | 2008-04-09 | Method and apparatus for liquefying a hydrocarbon stream |
PCT/EP2009/054125 WO2009124925A2 (en) | 2008-04-09 | 2009-04-07 | Method and apparatus for liquefying a hydrocarbon stream |
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TWI707115B (zh) * | 2015-04-10 | 2020-10-11 | 美商圖表能源與化學有限公司 | 混合製冷劑液化系統和方法 |
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