JP4713548B2 - 天然ガスの液化方法及び装置 - Google Patents
天然ガスの液化方法及び装置 Download PDFInfo
- Publication number
- JP4713548B2 JP4713548B2 JP2007189675A JP2007189675A JP4713548B2 JP 4713548 B2 JP4713548 B2 JP 4713548B2 JP 2007189675 A JP2007189675 A JP 2007189675A JP 2007189675 A JP2007189675 A JP 2007189675A JP 4713548 B2 JP4713548 B2 JP 4713548B2
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- stream
- methane
- enriched
- heat exchanger
- liquid
- Prior art date
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 372
- 239000003345 natural gas Substances 0.000 title claims description 51
- 238000000034 method Methods 0.000 title claims description 39
- 239000007788 liquid Substances 0.000 claims description 132
- 150000002430 hydrocarbons Chemical class 0.000 claims description 92
- 229930195733 hydrocarbon Natural products 0.000 claims description 91
- 238000010992 reflux Methods 0.000 claims description 80
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 62
- 239000003507 refrigerant Substances 0.000 claims description 60
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 51
- 238000004821 distillation Methods 0.000 claims description 43
- 239000000047 product Substances 0.000 claims description 41
- 238000001816 cooling Methods 0.000 claims description 37
- 239000004215 Carbon black (E152) Substances 0.000 claims description 33
- 239000001294 propane Substances 0.000 claims description 31
- 239000003949 liquefied natural gas Substances 0.000 claims description 27
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 27
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 26
- 239000001273 butane Substances 0.000 claims description 25
- 238000011084 recovery Methods 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 8
- 239000013526 supercooled liquid Substances 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- 125000004432 carbon atom Chemical group C* 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 2
- 238000007792 addition Methods 0.000 claims 1
- 238000009428 plumbing Methods 0.000 claims 1
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 14
- 239000000203 mixture Substances 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 8
- 239000002994 raw material Substances 0.000 description 8
- 239000001282 iso-butane Substances 0.000 description 7
- 238000001704 evaporation Methods 0.000 description 6
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram 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
- 238000005057 refrigeration Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 3
- 239000001307 helium Substances 0.000 description 3
- 229910052734 helium Inorganic materials 0.000 description 3
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 3
- 239000004615 ingredient Substances 0.000 description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 3
- 229910052753 mercury Inorganic materials 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910001868 water Inorganic materials 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- MEKDPHXPVMKCON-UHFFFAOYSA-N ethane;methane Chemical compound C.CC MEKDPHXPVMKCON-UHFFFAOYSA-N 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical class CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000004781 supercooling Methods 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000000411 inducer Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
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Description
(a)天然ガス原料を冷却して冷却天然ガス原料を提供するとともに、冷却天然ガス原料を第1蒸留塔へ導入すること、
(b)第1蒸留塔から、メタンを富化した塔頂蒸気流及びメタンよりも重い成分を富化した塔底流を抜き出すこと、
(c)塔頂蒸気流の少なくとも一部を冷却し凝縮させて、凝縮したメタン富化流を提供すること、
(d)塔底流を1以上の追加の蒸留塔で分離して、メタンを含む残留蒸気流、エタンを富化した液体流、プロパンを富化した液体流、ブタンを富化した液体流、及びペンタンを富化した液体流からなる群から選択される1以上の製品流を提供すること、
(e)1以上の製品流のいずれかの全て又は一部を、回収炭化水素として抜き出すこと、及び、
(f)1以上の還流を第1蒸留塔に導入すること、
を含む。
(f1)液化メタン含有の還流及び第1蒸留塔の圧力に昇圧される未回収液体炭化水素の流れ、あるいは、
(f2)液化メタン含有の還流と第1蒸留塔の圧力に昇圧される未回収液体炭化水素の流れとを含む混合流、
のいずれかを含む。
(1)塔頂蒸気流を冷却し完全に凝縮させて凝縮メタン富化流を作り、そして凝縮メタン富化流の一部を抜き出して液化メタン含有の還流を提供すること、
(2)第1塔頂蒸気流の一部を冷却し完全に凝縮させて液化メタン含有の還流を提供すること、及び、
(3)塔頂蒸気流を冷却し完全に凝縮させて凝縮メタン富化流を作り、そして凝縮メタン富化流の一部を加温して液化メタン含有の還流を提供すること、
からなる群から選択される方法により提供することが可能である。
(a)天然ガス原料を冷却して冷却天然ガス原料を提供するようにされた冷却装置、
(b)冷却天然ガス原料を分離してメタンを富化した塔頂蒸気流とメタンより重い成分を富化した塔底流とにするようにされた第1蒸留塔、
(c)塔頂蒸気流の少なくとも一部を冷却し凝縮させて凝縮メタン富化流を提供するようにされた主熱交換器、
(d)塔底流を分離して、メタンを含む残留蒸気流、エタンを富化した液体流、プロパンを富化した液体流、ブタンを富化した液体流、及びペンタンを富化した液体流からなる群から選択される1以上の製品流にするようにされた1以上の追加の蒸留塔、
(e)1以上の製品流のいずれかの全て又は一部分を回収炭化水素として抜き出すようにされた配管、
(f)(f1)液化メタン含有の還流と第1蒸留塔の圧力に昇圧される未回収液体炭化水素の流れ、又は(f2)液化メタン含有の還流と第1蒸留塔の圧力に昇圧される未回収液体炭化水素の流れを含む混合流、のいずれかを含む1以上の還流を、第1蒸留塔に導入するようにされた配管、及び、
(g)1以上の追加の蒸留塔から1以上の還流を第1蒸留塔に導入するようにされた配管まで未回収液体炭化水素を移送するようにされた配管と1台以上のポンプ、
を含む装置を包含する。
(a)天然ガス原料を冷却して冷却天然ガス原料を提供するとともに、冷却天然ガス原料を第1蒸留塔に導入すること、
(b)第1蒸留塔からメタンを富化した塔頂蒸気流とメタンよりも重い成分を富化した塔底流を抜き出すこと、
(c)塔頂蒸気流の少なくとも一部を主熱交換器で冷却し凝縮させて凝縮メタン富化流を提供すること、及び、
(d)液化メタン含有の還流を第1蒸留塔に導入し、その際、液化メタン含有の還流を、
(1)塔頂蒸気流を第1蒸気部分及び第2蒸気部分に分割し、そして第1蒸気部分を冷却し完全に凝縮させて液化メタン含有の還流を提供すること、及び、
(2)塔頂蒸気流を冷却し完全に凝縮させて凝縮メタン富化流を作り、凝縮メタン富化流を第1部分及び第2部分に分割し、第1部分を加温して加温した第1部分を提供し、そして加温した第1部分を用いて液化メタン含有の還流を提供すること、
からなる群から選択される方法により提供すること、
を含む、天然ガス液化方法に関する。
(a)天然ガス原料を冷却して冷却天然ガス原料を提供するようにされた冷却装置、
(b)冷却天然ガス原料を分離してメタンを富化した塔頂蒸気流とメタンよりも重い成分を富化した塔底流とにするようにされた第1蒸留塔、
(c)塔頂蒸気流の少なくとも一部を冷却し凝縮させて凝縮メタン富化流を提供するようにされた主熱交換器、及び、
(d)次の(1)と(2)からなる群、すなわち、
(1)塔頂蒸気流の一部を冷却し完全に凝縮させて液化メタン含有の還流を提供すること、及び、
(2)塔頂蒸気流を冷却し完全に凝縮させて凝縮メタン富化流を作り、そして凝縮メタン富化流の一部を加温して液化メタン含有の還流を提供すること、
からなる群から選択される方法により提供される液化メタン含有の還流を、第1蒸留塔に導入するようにされた配管、
を含む、天然ガス液化装置を包含する。
Claims (14)
- 天然ガス液化のための方法であって、
(i)天然ガス原料(100)を冷却(110及び114)して冷却天然ガス原料(116)を提供するとともに、前記冷却天然ガス原料を第1蒸留塔(118)に導入する工程、
(ii)前記第1蒸留塔からメタンを富化した塔頂蒸気流(120)とメタンよりも重い成分を富化した塔底流(134)を抜き出す工程、
(iii)工程(i)で天然ガス原料を冷却しながら前記塔頂蒸気流のうちの少なくとも一部分(122)を間接熱交換(114)により加温する工程、
(iv)工程(iii)の前記加温した塔頂蒸気流を巻きコイルの主熱交換器(124)で、第1の冷却した多成分液体冷媒(153)を減圧(154)することにより供給される第1の気化する冷媒との間接熱交換(123)により冷却し完全に凝縮させて完全凝縮メタン富化流(125)を提供する工程、及び、
(v)液化メタン含有の還流(126、221)を前記第1蒸留塔に導入し、その際、前記液化メタン含有の還流を、前記主熱交換器からの前記完全凝縮メタン富化流のうちの一部分(126)か、あるいは、工程(iv)の前記主熱交換器とは別の熱交換器(200)での前記第1の冷却した多成分液体冷媒のうちの一部分(252)との間接熱交換により冷却し完全に凝縮させた工程(iv)の塔頂蒸気流(120)のうちの加温していない蒸気部分(220)により提供する工程、
を含む、天然ガス液化方法。 - 前記完全凝縮メタン富化流のうちの前記一部分(126)を、前記メタン含有の還流として使用する前に、前記第1の多成分液体冷媒(152)のうちの一部分(352)との間接熱交換により加温(300)する、請求項1に記載の方法。
- (vi)前記塔底流を1以上の追加の蒸留塔(136; 501、503、505及び507)で分離して、メタンを含む残留蒸気流(509)、エタンを富化した液体流(529)、プロパンを富化した液体流(547)、ブタンを富化した液体流(565)、及びペンタンを富化した液体流(573)からなる群から選択される1以上の製品流と、未回収液体炭化水素の流れ(138)とを提供する工程、
(vii)前記1以上の製品流のいずれかの全て又は一部を、回収炭化水素として抜き出す工程、及び、
(viii)単独でかあるいは前記メタン含有の還流と一緒にして、前記第1蒸留塔の圧力に昇圧される前記未回収液体炭化水素の流れを還流(138、221)として前記第1蒸留塔に導入する工程、
を含む、請求項1又は2に記載の方法。 - 前記未回収液体炭化水素の流れ(138)が50モル%を超える3個以上の炭素原子を有する炭化水素を含有する、請求項3に記載の方法。
- 前記未回収液体炭化水素(138)のモル流量が前記液化メタン還流のモル流量の25%未満である、請求項3又は4に記載の方法。
- 工程(ii)の前記塔頂蒸気流の加温していない蒸気部分(220)を、前記第1の冷却した多成分液体冷媒(153)の一部(252)を抜き出し減圧(254)することによって提供される蒸発冷媒の流れとの間接熱交換により、前記主熱交換器(124)とは別の熱交換器(200)で冷却し完全に凝縮させることによって、前記液化メタン含有の還流を供給する、請求項1〜5のいずれか1項に記載の方法。
- 前記第1の冷却した多成分液体冷媒(153)を、前記主熱交換器(124)で飽和多成分液体冷媒(152)を冷却することにより提供するとともに、前記飽和多成分液体冷媒の一部(352)との間接熱交換による前記主熱交換器とは別の熱交換器(300)での工程(iv)の凝縮メタン富化流(125)の一部(126)の加温により、前記液化メタン含有の還流を供給する、請求項2〜5のいずれか1項に記載の方法。
- 工程(iv)の前記完全凝縮メタン富化流(125)の少なくとも一部を過冷却(128)して昇圧した液化天然ガス製品(129)を提供することを含み、該過冷却を、第2の冷却した多成分液体冷媒を減圧(158)することにより提供される第2の蒸発冷媒との間接熱交換(128)により前記主熱交換器(124)において行う、請求項1〜7のいずれか1項に記載の方法。
- 前記主熱交換器の高温バンドルを分割しない、請求項1〜8のいずれか1項に記載の方法。
- 請求項1記載の方法により天然ガスを液化するための装置であって、
(a)前記天然ガス原料を冷却して前記冷却天然ガス原料(116)を提供するようにされた冷却装置(110及び114)、
(b)前記冷却天然ガス原料を分離して前記メタンを富化した塔頂蒸気流(120)と前記メタンよりも重い成分を富化した塔底流(134)とにするようにされた第1蒸留塔(118)、
(c)前記塔頂蒸気流のうちの少なくとも一部分を前記冷却装置を通して供給して前記天然ガス原料との間接熱交換(114)により当該蒸気を加温して、加温した塔頂蒸気流(122)を供給するようにされた配管、
(d)前記加温した塔頂蒸気流を、第1の冷却した多成分液体冷媒(153)を減圧(154)することにより供給される第1の気化する冷媒との間接熱交換(123)により冷却し完全に凝縮させて、前記完全凝縮メタン富化流(125)を提供するようにされた巻きコイルの主熱交換器(124)、及び、
(e)前記主熱交換器からの前記完全凝縮メタン富化流のうちの一部分(126)か、あるいは、工程(iv)の前記主熱交換器とは別の熱交換器(200)での前記第1の冷却した多成分液体冷媒のうちの一部分(252)との間接熱交換により冷却し完全に凝縮させた工程(iv)の塔頂蒸気流(120)の加温していない蒸気部分(220)、により提供される前記液化メタン含有の還流を、前記第1蒸留塔に導入するようにされた配管(126、221)、
を含む、請求項1記載の方法による天然ガス液化装置。 - 前記主熱交換器からの前記完全凝縮メタン富化流のうちの前記一部分を、メタン含有の還流として使用する前に、前記第1の多成分液体冷媒(152)のうちの一部分(352)との間接熱交換により加温(300)するようにされている、前記主熱交換器(124)とは別の熱交換器(300)を含む、請求項10に記載の装置。
- 前記装置は、
(f)前記塔底流を分離して、メタンを含む残留蒸気流(509)、エタンを富化した液体流(529)、プロパンを富化した液体流(549)、ブタンを富化した液体流(565)、及びペンタンを富化した液体流(573)からなる群から選択される1以上の製品流と、未回収液体炭化水素の流れ(138)とにするようにされた1以上の追加の蒸留塔(136; 501、503、505及び507)、
(g)前記1以上の製品流のいずれかの全て又は一部分を回収炭化水素として抜き出すようにされた配管、及び、
(h)前記第1蒸留塔の圧力に昇圧された前記未回収液体炭化水素の流れを還流として前記第1蒸留塔に導入するようにされた配管(138、221)とポンプ、
を更に含み、そして前記方法が、
(vi)前記塔底流を1以上の追加の蒸留塔(136; 501、503、505及び507)で分離して、メタンを含む残留蒸気流(509)、エタンを富化した液体流(529)、プロパンを富化した液体流(547)、ブタンを富化した液体流(565)、及びペンタンを富化した液体流(573)からなる群から選択される1以上の製品流と、未回収液体炭化水素の流れ(138)とを提供する工程、
(vii)1以上の製品流のいずれかの全て又は一部を、回収炭化水素として抜き出す工程、及び、
(viii)単独でかあるいは前記メタン含有の還流と一緒にして、前記第1蒸留塔の圧力に昇圧される前記未回収液体炭化水素の流れを還流(138、221)として前記第1蒸留塔に導入する工程、
を更に含む、天然ガスの液化及び該天然ガスからのメタンより重い成分の回収のための、請求項10又は11に記載の装置。 - 前記第1の冷却した多成分液体冷媒(153)の一部(252)を抜き出し減圧(254)することにより供給される蒸発冷媒の流れとの間接熱交換により前記第1蒸留塔(118)からの塔頂蒸気流(220)の加温していない部分を冷却し完全に凝縮するようにされた、前記主熱交換器(124)とは別の熱交換器(200)を含む、請求項10〜12のいずれか1項に記載の装置。
- 前記主熱交換器(124)が、前記完全凝縮メタン富化流(125)を提供するため前記加温した塔頂蒸気流(122)を冷却し完全に凝縮させるようにされた第1バンドル(123)と、過冷却液体製品(129)を提供するため前記完全凝縮メタン富化流の少なくとも一部を更に冷却するようにされた第2バンドル(128)を含む、請求項10〜13のいずれか1項に記載の装置。
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KR101346172B1 (ko) * | 2011-12-19 | 2013-12-31 | 삼성중공업 주식회사 | 분별증류 장치 및 이를 이용한 분별증류 방법 |
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CN101108977B (zh) | 2012-07-18 |
AU2007203296B2 (en) | 2008-12-18 |
AU2007203296A1 (en) | 2008-02-07 |
EG25242A (en) | 2011-11-20 |
CA2593886C (en) | 2012-03-27 |
KR100891907B1 (ko) | 2009-04-06 |
US20080016910A1 (en) | 2008-01-24 |
KR20080008984A (ko) | 2008-01-24 |
EP1881283A2 (en) | 2008-01-23 |
RU2374575C2 (ru) | 2009-11-27 |
CA2593886A1 (en) | 2008-01-21 |
RU2007128005A (ru) | 2009-01-27 |
EP1881283A3 (en) | 2013-04-10 |
PE20080391A1 (es) | 2008-05-16 |
TW200806784A (en) | 2008-02-01 |
MY157897A (en) | 2016-08-15 |
NO20073829L (no) | 2008-01-22 |
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JP2008057962A (ja) | 2008-03-13 |
CN101108977A (zh) | 2008-01-23 |
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