JP2008506620A - 二酸化炭素の液化法及び装置 - Google Patents
二酸化炭素の液化法及び装置 Download PDFInfo
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 162
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 80
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims description 22
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 49
- 238000007906 compression Methods 0.000 claims description 43
- 230000006835 compression Effects 0.000 claims description 43
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 239000012530 fluid Substances 0.000 claims description 31
- 238000001816 cooling Methods 0.000 claims description 22
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 230000003134 recirculating effect Effects 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 62
- 239000012071 phase Substances 0.000 description 12
- 239000013535 sea water Substances 0.000 description 10
- 239000003039 volatile agent Substances 0.000 description 10
- 238000012546 transfer Methods 0.000 description 9
- 230000015572 biosynthetic process Effects 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 7
- 238000002347 injection Methods 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 150000002430 hydrocarbons Chemical class 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000003570 air Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 238000011282 treatment Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 239000012080 ambient air Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000013256 coordination polymer Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000010587 phase diagram Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000010561 standard procedure Methods 0.000 description 1
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Abstract
Description
トンのレベルでの大量生産は決して普通のことではない。すなわち、この大量生産では、出発物質が周囲温度及び圧力又はその付近である二酸化炭素又は二酸化炭素を主成分とするものであり、この出発物質を、顕著な加圧とエネルギー除去がおこなわれる大量輸送にとって望ましい温度及び圧力の液体二酸化炭素に変換する。
供給ガスは不純物、例えば、水、窒素等を含むことがあるので、流体流を一種以上の処理に付してこれらを除去することが望ましい。装置の設計によっては、これらの除去工程により、液体CO2以外の二酸化炭素の一部が装置から必然的に除去されることがある。しかしながら、設計を注意深くすることにより、このような非液体二酸化炭素が除去されるのを最小限とすることができる。
ば、2〜8、好ましくは4)の圧縮工程が必要である。水の除去を、少なくとも1回の圧縮工程後であって且つ最終圧縮工程前、例えば、第二圧縮工程と第三圧縮工程との間、典型的には前の圧縮工程に続く冷却工程後におこなうのが好ましい。とりわけ、各圧縮工程前に水の除去をおこなうのが好ましい。CO2ガスを、最終セパレータ後の吸着によりppmレベルまで乾燥することが望ましい。
温め(例えば、リボイラーで)、このセパレータカラムに戻すことができる。別法として、リボイラーを、セパレータカラムに一体化してもよい。
ここで、本発明の実施態様を、さらに例及び以下の非限定的実施例及び添付図面を参照して説明する。
上記した加圧流体の膨張では、ジュール−トンプソンバルブを使用するのが都合がよい。別法として、上記したような加圧流体の膨張に膨張タービンを使用してもよい。これにより、プロセスのエネルギー効率を増加させることができる。
供給ガスは、熱交換器28から、導管31を介してセパレータ30に流れる。セパレータ25及び30で除去された水は、導管32及び33を介して第一セパレータ20に戻される。
ムで、揮発物を蒸留により除去する。揮発物を、カラムの頂部で除去し、CO2の大部分を液相で残す。液体二酸化炭素は、導管43から取り出される。揮発物の除去率を高めるために、リボイラー44を、カラムの底部に取り付ける。リボイラーにより、カラムの底部に熱を供給して揮発物を蒸発除去し、それによりCO2からの揮発物の分離率を高める。カラムの頂部での揮発リッチガス流におけるCO2の回収率を高めるために、凝縮器をカラムの頂部に配置する。凝縮器の必要とする冷却は、中間また製品圧力で液体CO2を蒸発させることにより可能である。
図1に示す実施態様では、コンプレッサー2の前後の圧力及び温度は、好ましくは5bar A/25℃及び11bar A/25℃である。膨張タンク15での圧力及び温度は、好ましくは6.5bar A/−50℃である。
以下、3つの実施例をあげて、プロセスを供給ガスの臨界点の上又は下での熱除去について操作できる別法について説明する。
二酸化炭素を、供給圧1barから最大圧約60barに3つの圧縮段階で圧縮する。各圧縮段階間で、供給ガスを海水又は大気を用いて冷却する。十分に加圧化した供給ガス、すなわち、最終コンプレッサーからの出力を、海水を用いて再び熱交換器で凝縮する。凝縮供給ガスを、膨張弁を用いて移送圧まで膨張させ、フラッシュタンク又はセパレータに通じさせる。セパレータにおいて、液相を除去し、移送容器又は貯蔵容器に送り、気相を圧縮段階に戻す。
供給ガスを、供給圧1barから最大圧約2.5barに2つの圧縮段階で圧縮する。中間冷却(圧縮段階間)を、海水又は大気を用いておこなう。次に、加圧供給ガスを、外部冷却回路に接続した熱交換器を用いて凝縮する。次に、凝縮供給ガスを、膨張弁を用いて移送圧まで膨張させ、フラッシュタンク又はセパレータに通じさせる。セパレータにおいて、液相を除去し、移送容器又は貯蔵容器に送り、気相を圧縮段階に戻す。
供給ガスを、供給圧1barから最大圧約85bar(すなわち、臨界圧73.8bar超)に4つの圧縮段階で圧縮する。中間冷却(圧縮段階間)を、海水又は大気を用いておこなう。次に、加圧供給ガスを、海水又は大気を用いて超臨界相に冷却する。加圧流体を、超臨界相から二相領域に移送圧まで膨張手段を用いて膨張し、フラッシュタンク又はセパレータに通じさせる。セパレータにおいて、液相を除去し、移送容器又は貯蔵容器に送り、気相を圧縮段階に戻す。
Claims (10)
- 周囲温度より低く、二酸化炭素の三重点温度より高く、且つ二酸化炭素の臨界点温度より低い温度と、周囲圧力より高く、二酸化炭素の三重点圧力より高く、二酸化炭素の臨界点圧力より低い圧力である所望の温度及び圧力の液体二酸化炭素を、二酸化炭素を含む供給ガスから製造する方法であって、入口から、膨張チャンバーに接続された出口までの流路を備えた液化装置の入口に前記供給ガスを供給することと;流体としての前記ガスを前記流路に沿って前記装置を通って流し、前記流体を複数の圧縮及び冷却サイクルに付すことにより、前記所望の温度及び圧力より高い温度及び圧力を有する液体又は超臨界二酸化炭素を生成することと;前記液体又は超臨界二酸化炭素を前記出口を通過させて前記膨張チャンバーに入れることにより、前記チャンバーにおいて前記所望温度及び圧力の気体二酸化炭素及び液体二酸化炭素を生成することと;前記気体二酸化炭素を前記圧縮及び冷却のサイクルに付されながら流れている流体に再循環することと;必要に応じて前記所望の温度及び圧力の前記液体二酸化炭素を前記膨張チャンバーから取り出すことと、を含む方法。
- 圧縮サイクルの一つ以上が、さらに膨張工程を含む、請求項1に記載の方法。
- 前記各圧縮サイクルに流れる流体が、単相性である、請求項1又は2に記載の方法。
- 前記膨張チャンバーは、液体二酸化炭素を取り出す液体除去口を備えている、前記請求項のいずれかに記載の方法。
- 前記再循環二酸化炭素が、一つ以上の熱交換器を通過する、前記請求項のいずれかに記載の方法。
- 前記再循環二酸化炭素を、上流点で流体流に戻す、前記請求項のいずれかに記載の方法。
- 4圧縮サイクルを含む、前記請求項のいずれかに記載の方法。
- 水を少なくとも1回の圧縮サイクル後及び最終の圧縮サイクル前に除去する、前記請求項のいずれかに記載の方法。
- 入口から出口への二酸化炭素通過用流路を備えている二酸化炭素液化用装置であって、前記流路が直列に配列された複数のコンプレッサー及びクーラーを備え、膨張チャンバーを前記最終コンプレッサー及びクーラーの下流の前記流路に備え、気体二酸化炭素を前記膨張チャンバーから前記最終コンプレッサー及びクーラーの上流の前記流路に戻すように配置された再循環流路を備えている、装置。
- 前記膨張チャンバーが、液体二酸化炭素を取り出すことができるような液体除去口を備えている、請求項9に記載の装置。
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GB0416001A GB2416389B (en) | 2004-07-16 | 2004-07-16 | LCD liquefaction process |
PCT/GB2005/002777 WO2006008482A1 (en) | 2004-07-16 | 2005-07-14 | Process and apparatus for the liquefaction of carbon dioxide |
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- 2005-07-14 CA CA002574034A patent/CA2574034C/en not_active Expired - Fee Related
- 2005-07-14 US US11/632,492 patent/US20080156035A1/en not_active Abandoned
-
2007
- 2007-02-14 NO NO20070850A patent/NO20070850L/no not_active Application Discontinuation
- 2007-02-16 KR KR1020077003795A patent/KR100910278B1/ko not_active IP Right Cessation
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2009
- 2009-08-14 AU AU2009208153A patent/AU2009208153A1/en not_active Abandoned
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Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
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JP2011529434A (ja) * | 2008-07-31 | 2011-12-08 | ビーピー オルタネイティブ エナジー インターナショナル リミテッド | 二酸化炭素及び水素の分離 |
JP2012530239A (ja) * | 2009-06-16 | 2012-11-29 | テーゲーエー、マリン、ガス、エンジニヤリング、ゲーエムベーハー | 二酸化炭素の排出を低減するための方法および装置 |
JP2013519056A (ja) * | 2009-09-28 | 2013-05-23 | コーニンクレッカ フィリップス エレクトロニクス エヌ ヴィ | 流体を液化及び保存するシステム並びに方法 |
JP2013515232A (ja) * | 2009-12-22 | 2013-05-02 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Co2リッチフローを乾燥および圧縮する方法および装置 |
CN104067078A (zh) * | 2011-04-14 | 2014-09-24 | 乔治洛德方法研究和开发液化空气有限公司 | 用于在超临界压力下液化气体或冷却原料气的方法和设备 |
JP2013087016A (ja) * | 2011-10-18 | 2013-05-13 | Japan Organo Co Ltd | 二酸化炭素精製供給方法及びシステム |
JP5826265B2 (ja) * | 2012-09-13 | 2015-12-02 | 三菱重工コンプレッサ株式会社 | 昇圧システム、及び気体の昇圧方法 |
US11656026B2 (en) | 2012-09-13 | 2023-05-23 | Mitsubishi Heavy Industries Compressor Corporation | Compressing system, and gas compressing method |
JP6086998B2 (ja) * | 2014-01-14 | 2017-03-01 | 三菱重工コンプレッサ株式会社 | 昇圧システム、及び気体の昇圧方法 |
US10570927B2 (en) | 2014-01-14 | 2020-02-25 | Mitsubishi Heavy Industries Compressor Corporation | Boosting system, and boosting method of gas |
WO2017138036A1 (ja) * | 2016-02-09 | 2017-08-17 | 三菱重工コンプレッサ株式会社 | 昇圧システム |
JPWO2017138036A1 (ja) * | 2016-02-09 | 2018-09-20 | 三菱重工コンプレッサ株式会社 | 昇圧システム |
Also Published As
Publication number | Publication date |
---|---|
BRPI0513429A (pt) | 2008-05-06 |
CA2574034C (en) | 2010-03-09 |
CA2574034A1 (en) | 2006-01-26 |
KR20070048195A (ko) | 2007-05-08 |
CN101052852A (zh) | 2007-10-10 |
GB2416389A (en) | 2006-01-25 |
EP1776553A1 (en) | 2007-04-25 |
AU2005263928B2 (en) | 2009-05-14 |
EA200700046A1 (ru) | 2007-08-31 |
GB0416001D0 (en) | 2004-08-18 |
EA012122B1 (ru) | 2009-08-28 |
NO20070850L (no) | 2007-04-13 |
GB2416389B (en) | 2007-01-10 |
AU2005263928A1 (en) | 2006-01-26 |
US20080156035A1 (en) | 2008-07-03 |
KR100910278B1 (ko) | 2009-08-03 |
AU2009208153A1 (en) | 2009-09-10 |
JP4913733B2 (ja) | 2012-04-11 |
WO2006008482A1 (en) | 2006-01-26 |
AU2005263928C1 (en) | 2012-08-16 |
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