JP2008025986A - 空気分離プロセスにおけるlngベース液化装置の能力増強システム - Google Patents
空気分離プロセスにおけるlngベース液化装置の能力増強システム Download PDFInfo
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- JP2008025986A JP2008025986A JP2007166660A JP2007166660A JP2008025986A JP 2008025986 A JP2008025986 A JP 2008025986A JP 2007166660 A JP2007166660 A JP 2007166660A JP 2007166660 A JP2007166660 A JP 2007166660A JP 2008025986 A JP2008025986 A JP 2008025986A
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- Prior art keywords
- nitrogen
- stream
- lng
- low pressure
- liquefier
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 238000000926 separation method Methods 0.000 title claims abstract description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 304
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 146
- 238000004519 manufacturing process Methods 0.000 claims abstract description 30
- 238000004821 distillation Methods 0.000 claims abstract description 26
- 239000003949 liquefied natural gas Substances 0.000 claims description 94
- 239000007788 liquid Substances 0.000 claims description 42
- 238000000034 method Methods 0.000 claims description 40
- 238000001816 cooling Methods 0.000 claims description 23
- 238000005057 refrigeration Methods 0.000 claims description 17
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 16
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 229910052786 argon Inorganic materials 0.000 claims description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 239000002826 coolant Substances 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 230000002708 enhancing effect Effects 0.000 claims description 2
- 229910052743 krypton Inorganic materials 0.000 claims description 2
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 claims description 2
- 229910052724 xenon Inorganic materials 0.000 claims description 2
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 claims description 2
- 239000012263 liquid product Substances 0.000 abstract description 7
- 230000000153 supplemental effect Effects 0.000 abstract 2
- 230000003111 delayed effect Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 description 29
- 239000007789 gas Substances 0.000 description 13
- 239000012071 phase Substances 0.000 description 13
- 229910001873 dinitrogen Inorganic materials 0.000 description 12
- 239000003507 refrigerant Substances 0.000 description 10
- 238000010586 diagram Methods 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 230000009977 dual effect Effects 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 1
- 238000011067 equilibration Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000008450 motivation Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- 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
- 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
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
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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
- F25J2210/02—Multiple feed streams, e.g. originating from different sources
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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
- F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
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Abstract
【解決手段】本システムにおいて、低生産モードでは、LNGベース液化装置に供給される窒素が蒸留カラムシステムからの少なくとも一部の高圧力窒素のみからなり、一方高生産モードでは、補助コンプレッサーを使用して蒸留カラムシステムからの少なくとも一部の低圧力窒素を昇圧しLNGベース液化装置への追加的な(又は置換する)供給を行う。本発明の鍵は補助コンプレッサーであり、且つ関連する熱交換器はLNGベース液化装置とは離れていて且つ別個のものである。このため能力増強が現実に必要になるまで、機器の購入を遅らせることが可能であり、それゆえに液化製品需要の見込み増加に基づいた過大な液化装置の建造を避けることができる。
【選択図】図1b
Description
(a)供給空気が、圧縮され、水や二酸化炭素のように低温で結氷して不純物が取り除かれ、続いて主熱交換器及び蒸留カラムシステムを有する低温の空気分離ユニット(以後「ASU」)に供給され;
(b)供給空気が、蒸留カラムシステムからの排出流れの少なくとも一部に対して、主熱交換器において間接熱交換されることによって、冷却され(そして随意的に少なくとも一部が凝縮され);
(c)冷却された供給空気が、蒸留カラムシステムにおいて、窒素を富化した流れと、酸素を富化した流れ(及び、随意的にアルゴン、クリプトン及びキセノンを含む供給空気の残留成分を富化した各々の流れ)とを包含する複数の排出流れへ、分離され;
(d)蒸留カラムシステムは、高圧力カラムと、低圧力カラムとを有し;
(e)高圧力カラムが供給空気を、高圧力カラム頂部から引き出された高圧力窒素流れを含む排出流れと、高圧力カラムの底部から引き出され且つさらなるプロセス処理のために低圧力カラムへ供給される粗製液体酸素流れと、に分離し;
(f)低圧力カラムは粗製液体酸素流れを、低圧力カラム底部から引き出された酸素生成物流れを含む排出流れと、低圧力カラム頂部から引き出された低圧力の窒素流れと、(及びしばしば低圧力カラムの上方部から引き出された窒素流れと)に分離し;そして
(g)高圧力窒素の少なくとも一部が、低圧力カラムの底部(又はサンプ(汚水貯め))に貯まり沸騰している酸素富化液体に対してリボイラー/コンデンサーにおいて凝縮し、且つ蒸留カラムシステムのリフラックス(環流)として使用されるように、高圧力カラム及び低圧力カラムは熱的に連結される。
流れ182は、LNGベース液化装置からの高温の低圧力のガス状窒素の排気流れ366と混合されて流れ370を生じる。流れ370は補助コンプレッサー(高温低圧コンプレッサー324)で圧縮され、それから後冷却熱交換器326(概して冷却媒体として冷却水又はグリコールを使用する)で冷却されて流れ184を生じる。流れ184は実質的に高圧力の液化装置への供給流れ288及び176と混合されて流れ330を生じる。LNGベース液化装置の運転は、流れ366が排気されないことを除いて、図3aで記載された運転と類似している。
低生産モードの運転(事例1)では、ASUから流れ182が(流れ486として)大気に排気され、LNGベース液化装置から流れ366が大気に排気され、そして流れ184及び386の流量は0である。高生産モード(事例2及び3)では、流れ182(流れ488として)及び386が補助プロセス処理ユニットを通過し、そして流れ366の流量は0である。これらの特定の事例2及び3の例に関して、(高圧力カラムを起源とする)流れ176の流量も0である。すなわち、事例2及び3では、昇圧した窒素と高圧力の窒素の間で、昇圧した窒素のみが高生産モードのLNGベース液化装置に供給されるように、高圧力カラムからの高圧力窒素462の全部がリボイラー/コンデンサー[418]で凝縮されそして蒸留カラムシステムのためのリフラックスとして使用される。これは必須ではないが、高生産モードにおいては標準的なシナリオである。事例2及び3の明確な差は、事例3の液体窒素生成物がより多いことである。
注釈1:液体酸素生成物が事例1から事例2で33%増し;液体酸素生成物が事例2及び3では同じであった。
注釈2:液体窒素生成物が事例1から事例2で60%増し;液体窒素生成物が事例1から事例2で140%増した。
注釈3:高圧力窒素流量が、事例1では液体窒素生成物の要求を満たすのに十分であったが、事例2及び3では0であった。
注釈4:液体酸素生成物は事例1ではかなり少なかったけれども、ASUへの空気流量は3つの事例の全てについてほぼ同じであった。これは重要な特徴である。ASUから窒素を高圧力窒素として生成することを選択すると、その場合酸素回収量は減少する。結果として、本発明を利用することにより、3つの全ての事例について同じコンプレッサー及び同じ低温ASUを利用することが可能となる。
注釈5:事例1は低圧コンプレッサーを伴わないで運転した(補助プロセス処理ユニット(3)は必要でなかった)。
Claims (11)
- 供給空気の低温分離のためのプロセス処理方法であって、
(a)供給空気が、圧縮され、水や二酸化炭素のように低温で結氷して不純物が取り除かれ、続いて主熱交換器及び蒸留カラムシステムを有する低温の空気分離ユニット(以後「ASU」)に供給され;
(b)供給空気が、蒸留カラムシステムからの排出流れの少なくとも一部に対して、主熱交換器において間接熱交換されることによって、冷却され;
(c)冷却された供給空気が、蒸留カラムシステムにおいて、窒素を富化した流れと、酸素を富化した流れ(及び、随意的にアルゴン、クリプトン及びキセノンを含む供給空気の残留成分を富化した各々の流れ)とを包含する複数の排出流れへ、分離され;
(d)蒸留カラムシステムは、高圧力カラムと、低圧力カラムとを有し;
(e)高圧力カラムが供給空気を、高圧力カラム頂部から引き出された高圧力窒素流れを含む排出流れと、高圧力カラムの底部から引き出され且つさらなるプロセス処理のために低圧力カラムへ供給される粗製液体酸素流れと、に分離し;
(f)低圧力カラムは粗製液体酸素流れを、低圧力カラム底部から引き出された酸素生成物流れを含む排出流れと、低圧力カラム頂部から引き出された低圧力の窒素流れと、に分離し;
(g)高圧力窒素の少なくとも一部が、低圧力カラムの底部(又はサンプ(汚水貯め))に貯まり沸騰している酸素富化液体に対してリボイラー/コンデンサーにおいて凝縮し、且つ蒸留カラムシステムのリフラックス(環流)として使用されるように、高圧力カラム及び低圧力カラムは熱的に連結され;
(h)少なくとも一部の生成物が液体として望まれている場合に必要なリフリジレーション冷却を提供するように、液化天然ガス(以後「LNG」)によるリフリジレーション冷却が、窒素を蒸溜カラムシステムから液化装置ユニット(以後「LNGベース液化装置」)へ供給することによって行われ、(このLNGベース液化装置では、一以上の付属コンプレッサーを使用する複数のステージで窒素を圧縮すること、及び付属熱交換器で液化天然ガスに対して間接熱交換することによって複数のステージの間で窒素を冷却することによって、液化がされる);
LNGベース液化装置用の付属コンプレッサーとは離れていて且つ別個の補助コンプレッサーを有する、LNGベース液化装置の能力を増強するためのシステムが:
(i)低生産モードでは、低圧力窒素及び高圧力窒素の間で、LNGベース液化装置に供給される窒素が、高圧力窒素の少なくとも一部のみからなり;そして
(ii)高生産モードでは、補助コンプレッサーが使用されて低圧力窒素の少なくとも一部の圧力を高圧力窒素の圧力まで昇圧し、LNGベース液化装置に供給する昇圧窒素を生じる、
プロセス方法。 - 高生産モードにおいて、LNGベース液化装置に供給される窒素が、昇圧した窒素、及び高圧力窒素の少なくとも一部の両方を含む、請求項1に記載された方法。
- 昇圧した窒素及び高圧力窒素の間で、昇圧した窒素だけが高生産モードのLNGベース液化装置に供給されるように、(g)において、高圧力窒素の全体部が、リボイラー/コンデンサーで凝縮され且つ蒸留カラムシステムのためのリフラックスとして使用される、請求項1に記載された方法。
- 低生産モード及び高生産モードの両方において、液化装置に供給される窒素が、主熱交換器において供給空気に対する間接熱交換によって気化された後に(h)で生じた液化窒素の少なくとも一部を含む、請求項1に記載された方法。
- 低圧力窒素の圧力を昇圧する前に、付属熱交換器とは離れていて且つ別個の補助的な予冷却熱交換器においてLNGに対して間接熱交換することによって、低圧力窒素が冷却され冷却した窒素流れを生じる、請求項1に記載された方法。
- 冷却した窒素流れを昇圧する前に、冷却した窒素流れがLNGベース液化装置からのガス状窒素排気流れと混合される、請求項5に記載された方法。
- 低圧力窒素流れを冷却する前に、低圧力窒素がLNGベース液化装置からのガス状窒素排気流れと混合される、請求項5に記載された方法。
- (i)低圧力窒素の圧力を昇圧する前に、低圧力窒素がLNGベース液化装置からのガス状窒素排気流れと混合され;及び
(ii)低圧力窒素の圧力を昇圧した後であるが、LNGベース液化装置に供給される前に、付属熱交換器とは離れていて且つ別個の補助的な後冷却熱交換器において冷却媒体に対して間接熱交換することによって、低圧力窒素が冷却される、
請求項1に記載された方法。 - 低生産モードの間は、いずれは補助コンプレッサーを駆動させるための空きピニオンを有する機械によって、付属コンプレッサーが駆動させられる、請求項1に記載された方法。
- 高生産モードの間は、補助コンプレッサーが空きピニオンに取り付けられる、請求項9に記載された方法。
- 高生産モードの間は、付属コンプレッサー及び補助コンプレッサーが別の機械によって駆動させられる、請求項1に記載された方法。
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Also Published As
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TW200801423A (en) | 2008-01-01 |
CN101097112B (zh) | 2012-09-19 |
CA2593649A1 (en) | 2007-12-30 |
CA2593649C (en) | 2012-03-13 |
TWI302188B (en) | 2008-10-21 |
US7712331B2 (en) | 2010-05-11 |
EP1873469A3 (en) | 2012-08-01 |
JP5015674B2 (ja) | 2012-08-29 |
KR20080002673A (ko) | 2008-01-04 |
KR100874680B1 (ko) | 2008-12-18 |
MX2007007878A (es) | 2008-12-16 |
EP1873469A2 (en) | 2008-01-02 |
SG138574A1 (en) | 2008-01-28 |
CN101097112A (zh) | 2008-01-02 |
US20080000266A1 (en) | 2008-01-03 |
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