JP6816017B2 - 混合冷媒液化システム及び方法 - Google Patents
混合冷媒液化システム及び方法 Download PDFInfo
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- JP6816017B2 JP6816017B2 JP2017553009A JP2017553009A JP6816017B2 JP 6816017 B2 JP6816017 B2 JP 6816017B2 JP 2017553009 A JP2017553009 A JP 2017553009A JP 2017553009 A JP2017553009 A JP 2017553009A JP 6816017 B2 JP6816017 B2 JP 6816017B2
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- 238000000034 method Methods 0.000 title description 40
- 239000007788 liquid Substances 0.000 claims description 115
- 239000007789 gas Substances 0.000 claims description 106
- 238000001816 cooling Methods 0.000 claims description 52
- 238000011084 recovery Methods 0.000 claims description 47
- 239000012263 liquid product Substances 0.000 claims description 26
- 238000003860 storage Methods 0.000 claims description 23
- 239000000047 product Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims 2
- 238000005201 scrubbing Methods 0.000 description 28
- 238000010992 reflux Methods 0.000 description 19
- 238000010586 diagram Methods 0.000 description 18
- 239000003949 liquefied natural gas Substances 0.000 description 16
- 239000004215 Carbon black (E152) Substances 0.000 description 10
- 229930195733 hydrocarbon Natural products 0.000 description 10
- 150000002430 hydrocarbons Chemical class 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000001112 coagulating effect Effects 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 238000007906 compression Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000000701 coagulant Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 1
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- 230000007423 decrease Effects 0.000 description 1
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- 238000005265 energy consumption Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
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- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
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- 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
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- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
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- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
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Description
[0025]図2〜7のシステムは、上記に記載したものと同様の構成要素を示す。
[0030]図1及び2のEFG冷熱回収オプションは、図2Aにおいて示すように組み合わせることができる。より具体的には、蒸気/液体分離器58から排出されるEFG流れ56は、流れ62(これは主熱交換器66の冷却流路64に送る)、及び流れ68(これは冷熱回収熱交換器72に送って、図2のシステムに関して上記に記載したように、冷熱回収熱交換器72を通して流れる1つ又は複数のMR流れ74を冷却する)に分割する。その結果、EFGの冷熱は、主熱交換器66及び冷熱回収熱交換器72の両方において、装置及びプロセスに合致する最適の割合で回収される。流れ62及び流れ68に流れるEFG流れ56の部分は、バルブ69によって制御することができる。
[0042]流れ172によってスクラビングカラム154の底部から取り出される成分は、熱交換器146に戻して冷媒を回収し、次に概して174で示されているコンデンセートストリッピングシステムのような更なる分離工程に送るか、又は燃料若しくは他の処分方法に送る。
[0049]取り出された成分は、スクラビングカラム底部の凝固性成分出口を通して送った後、ライン234を通して熱交換器216に戻して低温冷却を回収し、次に図7に示すようにライン236を通してコンデンセートストリッピングシステム238のような更なる分離工程に送るか、或いは低温冷却を回収するか又は回収しないで燃料又は他の処分方法に送ることができる。
Claims (15)
- (a)供給原料ガス入口を含む高温端、及び液化ガス出口を含む低温端を、その間に配置されている液化流路と共に有し、供給原料ガス入口は供給原料ガスを受容するように適合されており、液化熱交換器は主冷却流路も含む液化熱交換器;
(b)冷媒を主冷却流路に供給するように構成されている混合冷媒圧縮機システム;
(c)液化熱交換器の液化ガス出口と連通している膨張分離器;
(d)膨張分離器と流体連通している低温ガスライン;
(e)低温ガスラインと連通している蒸気流路、及び主冷却流路と連通している液体流路を有し、蒸気流路は低温ガスラインからの低温蒸気を受容するように構成されている冷熱回収熱交換器;
(f)混合冷媒圧縮機システムは分離装置を含み、ここで分離装置は少なくとも1つの分離装置液体出口及び分離装置蒸気出口を含む;
(g)少なくとも1つの分離装置液体出口は、液体冷媒の第一部分を冷熱回収熱交換器の液体流路へ送り、かつ液体冷媒の第二部分を液化熱交換器へ送るように構成されている;
(h)冷熱回収熱交換器は、蒸気流路内の低温蒸気を用いて液体流路内の液体冷媒の第一部分を冷却し、かつ冷却した液体冷媒の第一部分を主冷却流路に送るように構成されている;ならびに
(i)主冷却流路の外部にある合流部、ここで合流部は液体冷媒の冷却された第一部分と液体冷媒の第二部分とを受容しかつ混合するように構成されており、合流部は中温立て管を含み、中温立て管は液体冷媒の冷却された第一部分と液体冷媒の第二部分と受容するか又は液体冷媒の冷却された第一部分と液体冷媒の第二部分とが混合されたものを受容するように構成されており、かつ主冷却流路と連通している立て管蒸気出口と、液化熱交換器の主冷却流路と連通している立て管液体出口を有し、それにより、液体冷媒の冷却された第一部分と液体冷媒の第二部分が混合されたものが、立て管蒸気出口と立て管液体出口をとおって主冷却流路に与えられる;
を含む、
気体を液化するためのシステム。 - 膨張分離器は液体生成物出口及びエンドフラッシュガス出口を含み、かつ、低温ガスラインは、エンドフラッシュガス出口と連通していて、エンドフラッシュガスを冷熱回収熱交換器の蒸気流路に供給するようになっている、請求項1に記載のシステム。
- 液化熱交換器は、エンドフラッシュガス流路を含み、このエンドフラッシュガス流路も膨張分離器のエンドフラッシュガス出口に連通している、請求項2に記載のシステム。
- 膨張分離器の液体生成物出口と連通している液体生成物貯蔵タンクを更に含み、かつ、冷熱回収熱交換器は第2の蒸気流路を含み、液体生成物貯蔵タンクは、液体生成物出口から貯蔵タンクに導入される液体生成物の流れから生成物エンドフラッシュガスを生成させるように構成されており、液体生成物貯蔵タンクは、第2の蒸気流路と連通しているヘッドスペースを有していて、生成物エンドフラッシュガスを冷熱回収熱交換器の第2の蒸気流路に供給するようになっている、請求項2に記載のシステム。
- 膨張分離器の液体生成物出口と連通している液体生成物貯蔵タンクを更に含み、液体生成物貯蔵タンクは、液体生成物出口から貯蔵タンクに導入される液体生成物の流れから生成物エンドフラッシュガスを生成させるように構成されており、液体生成物貯蔵タンクは、ヘッドスペースを有しており、このヘッドスペースも冷熱回収熱交換器の蒸気流路と連通していて、生成物貯蔵タンクのヘッドスペースからの生成物エンドフラッシュガス、及び膨張分離器のエンドフラッシュガス出口からのエンドフラッシュガスを、冷熱回収熱交換器の蒸気流路に供給するようになっている、請求項2に記載のシステム。
- 膨張分離器は液体生成物出口を含み、かつ、液体生成物出口と連通している液体生成物貯蔵タンクを更に含み、液体生成物貯蔵タンクは、液体生成物出口から貯蔵タンクに導入される液体生成物の流れから生成物エンドフラッシュガスを生成させるように構成されており、液体生成物貯蔵タンクは、低温ガスラインと連通しているヘッドスペースを有していて、生成物エンドフラッシュガスを冷熱回収熱交換器の蒸気流路に供給するようになっている、請求項1に記載のシステム。
- 低温ガスライン内に配置されている圧縮機を更に含む、請求項6に記載のシステム。
- 冷熱回収熱交換器の蒸気流路の出口は圧縮機と連通している、請求項1に記載のシステム。
- 膨張分離器は、蒸気/液体分離器と液体膨張器とが統合されたものである、請求項1に記載のシステム。
- 膨張分離器は、蒸気/液体分離器と直列の液体膨張器を含む、請求項1に記載のシステム。
- 液化熱交換器の主冷却流路が第一の入口と第二の入口を含み、第一の入口は分離装置蒸気出口から冷媒流れを受容するように構成されており、第二の入口は冷熱回収熱交換器の液体流路から冷媒流れを受容するように構成されており、
冷熱回収熱交換器の液体流路から冷媒流れが第二の入口を流れるとき、冷熱回収熱交換器の液体流路からの冷媒流れは分離装置蒸気出口からの冷媒流れから分離している、
請求項1に記載のシステム。 - 合流部は、液化熱交換器に入る前に、液体冷媒の第一部分及び第二部分を混合するように構成されている、請求項1に記載のシステム。
- 少なくとも1つの分離装置液体出口は分割部を含み、分割部は分離装置出口へ結合した入口、および液体冷媒の第一部分を冷熱回収熱交換器の液体流路へ送り、そして液体冷媒の第二部分を液化熱交換器へ送るように構成されている、請求項1に記載のシステム。
- 液化熱交換器が、液体冷媒冷却流路を含み、それにより、少なくとも1つの分離装置液体出口からの液体冷媒の第二部分が、合流部へ送られる前に、液化熱交換器の液体冷媒冷却流路へ送られるように構成されている、請求項13に記載のシステム。
- 液化熱交換器が液体冷媒冷却流路を含み、それにより少なくとも1つの分離装置液体出口からの液体冷媒が、合流部へ送られる前に、液化熱交換器の液体冷媒冷却流路へ送られるように構成されている、請求項1に記載のシステム。
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US201562145929P | 2015-04-10 | 2015-04-10 | |
US62/145,929 | 2015-04-10 | ||
US201562215511P | 2015-09-08 | 2015-09-08 | |
US62/215,511 | 2015-09-08 | ||
PCT/US2016/026924 WO2016164893A1 (en) | 2015-04-10 | 2016-04-11 | Mixed refrigerant liquefaction system and method |
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US20180003430A1 (en) | 2018-01-04 |
AU2016246839A1 (en) | 2017-11-02 |
BR112017021399A2 (pt) | 2018-07-03 |
JP2021012014A (ja) | 2021-02-04 |
MX2022003665A (es) | 2022-05-10 |
EP3280963A1 (en) | 2018-02-14 |
JP2018511024A (ja) | 2018-04-19 |
US10060671B2 (en) | 2018-08-28 |
AU2021204214B2 (en) | 2022-08-25 |
MX2017012978A (es) | 2018-02-12 |
CA3202262A1 (en) | 2016-10-13 |
EP3280963A4 (en) | 2019-03-20 |
JP2022046685A (ja) | 2022-03-23 |
TW201638539A (zh) | 2016-11-01 |
CA2982210A1 (en) | 2016-10-13 |
WO2016164893A1 (en) | 2016-10-13 |
PE20180810A1 (es) | 2018-05-09 |
PE20220268A1 (es) | 2022-02-23 |
KR20180019517A (ko) | 2018-02-26 |
CN107614994B (zh) | 2021-01-01 |
JP7273941B2 (ja) | 2023-05-15 |
TWI707115B (zh) | 2020-10-11 |
CN112747563A (zh) | 2021-05-04 |
AU2021204214A1 (en) | 2021-07-15 |
US10267559B2 (en) | 2019-04-23 |
CN107614994A (zh) | 2018-01-19 |
KR102534533B1 (ko) | 2023-05-19 |
AU2016246839B2 (en) | 2021-07-22 |
US20160298898A1 (en) | 2016-10-13 |
CA2982210C (en) | 2023-08-08 |
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