JP4137594B2 - Cryogenic air separation method, liquid air production method, and apparatus used therefor - Google Patents

Cryogenic air separation method, liquid air production method, and apparatus used therefor Download PDF

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JP4137594B2
JP4137594B2 JP2002309630A JP2002309630A JP4137594B2 JP 4137594 B2 JP4137594 B2 JP 4137594B2 JP 2002309630 A JP2002309630 A JP 2002309630A JP 2002309630 A JP2002309630 A JP 2002309630A JP 4137594 B2 JP4137594 B2 JP 4137594B2
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air
liquid
pressure
gas turbine
heat
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JP2004144386A (en
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正夫 林
篤 宮本
修 梶
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Taisei Corp
Air Water Inc
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Taisei Corp
Air Water Inc
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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
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J2290/62—Details of storing a fluid in a tank

Description

【０００１】
【発明の属する技術分野】
本発明は、ＣＡＥＳ（Ｃｏｍｐｒｅｓｓｅｄ Ａｉｒ Ｅｎｅｒｇｙ Ｓｔｏｒａｇｅ：圧縮空気エネルギー貯蔵）システムと組み合わせることにより、エネルギー効率を向上させるようにした深冷空気分離方法および液体空気製造方法ならびにそれらに用いる装置に関するものである。
【０００２】
【従来の技術】
従来から、原料空気圧縮機で生成された圧縮空気を原料として利用し、これを冷却液化し窒素，酸素等の沸点の違いを利用して窒素，酸素等を分離発生させる深冷空気分離装置では、原料空気圧縮機を常時駆動させている。
【０００３】
上記の深冷空気分離装置の一例を、図１０に示す。この深冷空気分離装置は、原料空気圧縮機５１と、吸着塔等（図示せず）を備えた前処理装置５２と、熱交換器，精留塔等（ともに図示せず）を収容するコールドボックス５３と、窒素圧縮機５４と、酸素圧縮機５５等で構成されている。そして、原料空気圧縮機５１により原料空気を取り入れてこれを圧縮し、前処理装置５２で、圧縮した原料空気中の水分，ＣＯ2 等の不純物を吸着塔で除去する等の前処理を行い、つぎに、前処理を行った原料空気をコールドボックス５３内に導入し、熱交換器で超低温に冷却して精留塔に導入する。この精留塔では、導入した原料空気を冷却液化し窒素，酸素等の沸点の違いを利用して窒素，酸素等を分離発生させ、これら分離発生させた窒素，酸素をコールドボックス５３外に導出したのち、それぞれ窒素圧縮機５４，酸素圧縮機５５により圧縮して高圧窒素（Ｎ2 ），高圧酸素（Ｏ2 ）にし、製品として取り出すようにしている。
【０００４】
上記の深冷空気分離装置の他の例を、図１１に示す。この深冷空気分離装置は、製品を液体で製造するプラントにみられるものであり、コールドボックス５３から一旦窒素ガスを低圧で取り出し、循環窒素圧縮機５６で略４．５ＭＰａまで加圧後冷却し、液体を製造する。この場合に、循環窒素圧縮機５６を、夜間の安価な電力が得られる時間帯のみ駆動させる場合がある。図において、５７は液体酸素タンクで、５８は液体窒素タンクである。
【０００５】
また、上記の深冷空気分離装置には、省エネ効果を得ることを目的とした夜間電力型がある。この装置は、夜間の低価格電力を使用して液化ガスを余剰に製造し、昼間に、その余剰の液化ガスを利用して異なる液化ガスを製造するものである。例えば、液体酸素と液体窒素とを製造する装置では、夜間に液体窒素を余剰に製造しておき、昼間に、この余剰である液体窒素を利用して液体酸素を製造している。また、この深冷空気分離装置では、その深冷空気分離の過程で液体空気が製造されるため、この液体空気を夜間に余剰に製造しておき、昼間に、この余剰の液体空気を利用して液体酸素と液体窒素とを製造することもできる。また、液体空気を、原料空気圧縮機を有する専用の液体空気製造装置により、製造することもできる。
【０００６】
一方、ＣＡＥＳシステムは、安価な夜間電力を利用して高圧空気を製造し貯蔵するシステムである。
【０００７】
【発明が解決しようとする課題】
しかしながら、夜間電力型の深冷空気分離装置では、昼間は、通常に運転が行われており、原料空気は夜間と同等に必要であるため、原料空気圧縮機５１を駆動させる必要があり、電力コストの大幅な低減とはなっていない。また、夜間に液化ガス，液体空気の製造量を増大させるため、それに伴い、夜間設備，貯槽の大型化が必要となり、設備コストが増大する。また、専用の液体空気製造装置を用いる場合にも、同様の問題がある。一方、ＣＡＥＳシステムでは、夜間に高圧空気を製造する電力に比べ、昼間の発電量が少なく、設備コストに見合う経済性を見出せていない。
【０００８】
本発明は、このような事情に鑑みなされたもので、ＣＡＥＳシステムを組み合わせることにより、電力コストを大幅に低減することができ、深冷空気分離装置，液体空気製造装置を大型化させる必要のない深冷空気分離方法および液体空気製造方法ならびにそれらに用いる装置の提供をその目的とする。
【０００９】
【課題を解決するための手段】
上記の目的を達成するために、本発明は、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気を深冷空気分離装置の原料空気として用い、この深冷空気分離装置により製造した高圧液化窒素を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記高圧液体窒素をガス化し製品高圧窒素ガスとして取り出すとともに、上記高圧液体窒素の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにした深冷空気分離方法を第１の要旨とし、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気を液体空気製造装置の原料空気として用い、この液体空気製造装置により製造した液体空気を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記液体空気をガス化して取り出すとともに、上記液体空気の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにした液体空気製造方法を第２の要旨とし、深冷空気分離装置の原料空気が、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気であり、上記深冷空気分離装置により製造した高圧液化窒素を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記高圧液体窒素をガス化し製品高圧窒素ガスとして取り出すとともに、上記高圧液体窒素の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにした深冷空気分離装置を第３の要旨とし、液体空気製造装置の原料空気が、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気であり、上記液体空気製造装置により製造した液体空気を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記液体空気をガス化して取り出すとともに、上記液体空気の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにした液体空気製造装置を第４の要旨とする。
【００１０】
すなわち、本発明の深冷空気分離方法は、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気を深冷空気分離装置の原料空気として用いている。このように、本発明の深冷空気分離方法では、安価な夜間電力を利用して高圧空気を製造し貯蔵するＣＡＥＳシステムと、深冷空気分離装置とを組み合わせ、昼間に深冷空気分離装置を運転する際に、ＣＡＥＳシステムで安価に製造した高圧空気を、深冷空気分離装置の原料空気として用い、深冷空気分離装置に供給するようにしている。したがって、上記昼間の運転の際に、深冷空気分離装置の原料空気圧縮機を駆動させる必要がなく、昼間の電力コストをほぼゼロにすることができ、電力コストが大幅に低減する。しかも、深冷空気分離装置にＣＡＥＳシステムを組み合わせたものであり、深冷空気分離装置を大型化させる必要がなく、深冷空気分離装置の設備コストは増大しない。このため、深冷空気分離装置で得られる製品ガスを安価に提供することができ、ＣＡＥＳシステムの設備コストに見合うだけの経済性を見出すことができる。また、本発明の深冷空気分離装置によれば、上記深冷空気分離方法を効率よく行うことができる。一方、本発明の液体空気製造方法は、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気を液体空気製造装置の原料空気として用いている。このように、本発明の液体空気製造方法では、安価な夜間電力を利用して高圧空気を製造し貯蔵するＣＡＥＳシステムと、液体空気製造装置とを組み合わせ、昼間に液体空気製造装置を運転する際に、ＣＡＥＳシステムで安価に製造した高圧空気を、液体空気製造装置の原料空気として用い、液体空気製造装置に供給するようにしている。したがって、本発明の液体空気製造方法でも、本発明の深冷空気分離方法と同様に、上記の優れた効果を奏する。
【００１１】
なお、本発明における「深冷空気分離装置」とは、大気等の原料空気を深冷空気分離して窒素ガス，酸素ガス等を製造する（副次的に、液体窒素，液体酸素等の液体状態で製造してもよい）装置であり、一般的に、原料空気圧縮手段，原料空気中の不純物を除去する不純物除去手段，原料空気を極低温に冷却する熱交換手段，精留手段等を備えている。ＣＡＥＳシステムで製造した高圧空気のみを深冷空気分離装置の原料空気として用いる（すなわち、ＣＡＥＳシステムで製造した高圧空気のみで深冷空気分離装置を運転する）場合には、原料空気圧縮手段を省くことができる。また、本発明における「液体空気製造装置」とは、大気等の原料空気を液化して液体空気を製造する装置であり、深冷空気分離装置の一部で構成されていてもよいし、専用の装置であってもよい。一般的に、原料空気圧縮手段，原料空気中の不純物を除去する不純物除去手段，原料空気を極低温に冷却する熱交換手段等を備えており、ＣＡＥＳシステムで製造した高圧空気のみを液体空気製造装置の原料空気として用いる（すなわち、ＣＡＥＳシステムで製造した高圧空気のみで液体空気製造装置を運転する）場合には、原料空気圧縮手段を省くことができる。また、本発明において、「高圧空気貯蔵用空間」とは、地下空洞等の地下空間、海底，山頂等の各種の場所に設けた圧力容器等の内部空間，パイプ等を利用して造られた高圧空気貯蔵のための空間等であり、高圧空気を貯蔵することができる空間であれば、どのような空間でもよく、また、この空間を形成する構造物の構造も問わない。
【００１２】
また、本発明では、上記深冷空気分離装置により製造した高圧液化窒素の冷熱を発電設備に利用するようにしたため、発電効率が向上する。また、上記液体空気製造装置により製造した液体空気の冷熱を発電設備に利用するようにしたため、同様の効果を奏する。なお、発電設備としては、自家発電設備，商業用発電設備等の各種の発電設備があげられる。
【００１３】
また、本発明では、上記冷熱で発電設備のガスタービンに導入する原料空気を冷却するようにしたため、ガスタービンの空気圧縮機の動力が削減でき、その分発電量が増える。
【００１４】
【発明の実施の形態】
つぎに、本発明の実施の形態を図面にもとづいて詳しく説明する。
【００１５】
図１は本発明の深冷空気分離装置の一実施の形態を示している。図において、１はＣＡＥＳシステムで、２は酸素製造装置（深冷空気分離装置）で、３はガスタービン発電機である。上記ＣＡＥＳシステム１は、従来の岩盤空洞１２（図２参照）を設けたＣＡＥＳシステムを利用したものであり、空気を取り入れてこれを圧縮するＣＡＥＳ用圧縮機４と、このＣＡＥＳ用圧縮機４で圧縮した高圧空気（圧縮空気）を貯蔵する圧縮空気貯蔵タンク５とを備えている。
【００１６】
上記圧縮空気貯蔵タンク５は、図２に示すように、軟岩地盤中に縦方向に形成された立坑１１と、所望の深度（例えば、深度４００ｍ程度）で横方向に所望の長さ（例えば、長さ１０００ｍ程度）に形成された岩盤空洞１２（高圧空気貯蔵用空間）とを備えており、この岩盤空洞１２に、料金の安い夜間電力を利用して高圧空気を貯蔵するようにしている。
【００１７】
上記立坑１１は、公知の縦穴掘削工法を用いて軟岩地盤の地表面から鉛直下方に掘削形成された縦穴（直径６ｍ程度の円形断面を有する縦穴）からなる。この立坑１１には、これを貫通するようにして送泥管１３（直径２ｍ程度の円形断面を有する鋼管）が配設されており、この送泥管１３の上端開口部は、立坑１１に隣接する地表面に形成された（重泥水８〔図５参照〕を貯留する）重泥水貯留池１４に連通している。また、上記送泥管１３の外周面と立坑１１の内壁面との間にはグラウト材１５が充填されており、これにより、送泥管１３が立坑１１の内壁面に強固に固化されている（図３参照）。図２において、１６はコンクリート製の閉塞栓であり、立坑１１の下端部において、送泥管１３の外周面を覆った状態で固定されており（図４参照）、この閉塞栓１６によって、岩盤空洞１２に貯留された加圧状態の高圧空気や軽泥水９（図５参照）が、立坑１１の内壁面と送泥管１３の外周面との間の隙間を介して上方に漏れ出すのを防止している。
【００１８】
また、上記送泥管１３には、その内部に，直径１００ｍｍ程度のＦＲＰ（繊維強化プラスチック）製パイプからなる高圧空気流通管１７と、逆浸透膜造水管１８とが配設されている（図３参照）。上記高圧空気流通管１７の下端部は、上記送泥管１３の下端部において送泥管１３外に突出したのち閉塞栓１６内に進入してこれを貫通し、上記高圧空気流通管１７の下端開口部は閉塞栓１６の下端面から下方に向かって開口している（図４参照）。また、上記高圧空気流通管１７の上端開口部はＣＡＥＳ用圧縮機４の高圧空気出口（図示せず）に開閉弁１９ａ付き高圧空気導入管１９を介して連通しており、これにより、ＣＡＥＳ用圧縮機４で生成した高圧空気を高圧空気導入管１９，高圧空気流通管１７を介して岩盤空洞１２内に導入するようにしている。また、上記高圧空気流通管１７の上端開口部は酸素製造装置２の前処理設備６（図１参照）に開閉弁２０ａ付き高圧空気導出管２０を介して連通しており、これにより、岩盤空洞１２内の高圧空気を高圧空気流通管１７，高圧空気導出管２０を介して前処理設備６に導出するようにしている。
【００１９】
上記逆浸透膜造水管１８は、直径１ｍ程度の円形断面を有する鋼管からなる保護管２２と、この保護管２２の下部に設置された逆浸透膜モジュール２３（例えば、特開平１０−１５６３５６号公報に記載された逆浸透膜モジュール２３）とで構成されており、上記保護管２２の内部に、例えば、海水からなる塩水を投入し、上記逆浸透膜モジュール２３の淡水集水管（図示せず）を経て生産水槽に集積された淡水を、揚水ポンプ（図示せず）により揚水管２４を介して汲み上げることにより、淡水を生産するものである。この逆浸透膜造水管１８によれば、淡水集水管の内部の水を汲み上げれば、保護管２２内の塩水による逆浸透膜モジュール２３の外周への静水圧により、逆浸透膜を挟んだ淡水集水管の内圧との間に逆浸透以上の圧力差が常時自然な状態で生じていることになり、容易に逆浸透に必要な圧力差を得て、経済的かつ効率的に淡水を生産することが可能になる。なお、上記逆浸透膜造水管１８は、保護管２２の下端部が送泥管１３の下端より下方に突出して液溜まり部１２ａ（図２参照）の底部に埋設支持されており、これにより、送泥管１３に沿って安定した状態で設置されている。このようにして生産された淡水は、この実施の形態では、高炉メーカで使用されるスチームや洗浄用水等の大量の工業用水に利用される。
【００２０】
上記岩盤空洞１２は、公知の岩盤トンネル掘削工法を用いて立坑１１の下端部から左右両側に５００ｍ程度の長さで掘削形成された地下空間（直径１０〜１５ｍ程度の略円形断面の地下空間）である。この岩盤空洞１２は、立坑１１の下方に位置する部分から左右両側に向かってその直径が小さくなるように略水平に形成されており、これにより、岩盤空洞１２の天端部分２５が、この天端部分２５の左右両側から頂部２６に向かってなだらかな上り勾配に形成されている。図２において、１２ａは上記頂部２６の下方に位置する岩盤空洞１２の中央底部に凹状に拡大掘削された液溜まり部である。
【００２１】
上記岩盤空洞１２内では、高圧空気導入管１９，高圧空気流通管１７を介して導入された高圧空気が、重泥水貯留池１４から送泥管１３を介して岩盤空洞１２内に供給された重泥水８の静水圧により、下方から圧力を負荷された状態で岩盤空洞１２内に貯留されている（図５参照）。また、重泥水８の上方を覆って軽泥水９が供給配設されており、重泥水８と軽泥水９との比重差により岩盤空洞１２内の泥水は、軽泥水９による上層と重泥水８による下層との二層構造となっている。
【００２２】
上記重泥水８は、加重調整材としてのバライトやヘマタイト等の高比重微粉体を沈降しがたい安定した状態で混合させてなる懸濁液であって、１．２〜２．０程度の比重を有する比較的高価な泥水である。
【００２３】
一方、上記軽泥水９は、例えばベントナイト泥水に配合される増粘材としてのベントナイトを若干増量し、かつ、充填材として平均粒径１０〜４０μｍ程度の炭酸カルシウム粉末等を加えた比重１．０５〜１．２０の泥水である。この軽泥水９には、岩盤の空隙や割れ目を閉塞するマッドケーキが形成される際の核となる目詰め材として、例えば、逸泥防止材（ＬＣＭ）が混合されている。このような充填材と目詰め材との存在により、マッドケーキは岩盤の空隙や割れ目に確実にかつ強固に保持されることになる。
【００２４】
上記の構成において、ＣＡＥＳ用圧縮機４，圧縮空気貯蔵タンク５を稼働するのに先立って、掘削形成した岩盤空洞１２の内壁面の空隙や割れ目を閉塞して、岩盤空洞１２を気密化する作業を行う。すなわち、まず、岩盤空洞１２に水を供給して洗浄を行ったのち、重泥水８を送泥管１３から供給し、岩盤空洞１２および送泥管１３に充填する。つぎに、軽泥水９を高圧空気流通管１７（このときだけ、高圧空気流通管１７は軽泥水９の供給手段に接続される）を介して重泥水８が充填された岩盤空洞１２内に、重泥水８を押し出すようにしながら圧入供給する。このようにして、重泥水８と軽泥水９が岩盤空洞１２内に充填されることにより（図６参照）、これらの泥水成分により岩盤空洞１２の天端部分２５にはマッドケーキが形成され、岩盤の空隙や割れ目を閉塞して岩盤空洞１２を気密化する。
【００２５】
つぎに、ＣＡＥＳ用圧縮機４，圧縮空気貯蔵タンク５を稼働する場合には、例えば、料金の安い夜間電力を利用してＣＡＥＳ用圧縮機４を駆動させ、これにより高圧空気を生成し、これを高圧空気導入管１９，高圧空気流通管１７を介して岩盤空洞１２に圧送供給する。圧送された高圧空気は、その圧力によって岩盤空洞１２内の重泥水８および軽泥水９を押し下げつつ、下方から重泥水８による静水圧を負荷された状態で圧縮空気貯蔵タンク５に貯蔵される（図５参照）。また、押し下げられた重泥水８は、送泥管１３に順次流入し、この送泥管１３を介して、押し上げられるようにして重泥水貯留池１４に移動してゆく。
【００２６】
一方、例えば、多量の電力を必要とする昼間には、岩盤空洞１２内の高圧空気（４．５Ｐａ，１０℃，Ｒ．Ｈ．８０％）を高圧空気流通管１７，高圧空気導出管２０を介して酸素製造装置２の前側処理設備６に導出する。この導出により、岩盤空洞１２には、重泥水貯留池１４から移動した重泥水８が補充され、重泥水８の静水圧によって高圧空気を下方から押圧する状態を引き続き保持する。そして、高圧空気が岩盤空洞１２から全て導出された状態では、重泥水８は、岩盤空洞１２の天端部分２５に軽泥水９による上層を介在させた状態で、岩盤空洞１２に充填されることになる（図６参照）。
【００２７】
このように、ＣＡＥＳ用圧縮機４，圧縮空気貯蔵タンク５の稼働によって、高圧空気の貯蔵（導入）と取り出し（導出）とが繰り返される。なお、この実施の形態において、重泥水８に代えて、海水を用いることができる。この場合には、重泥水貯留池１４に海水を溜め、これを送泥管１３を介して岩盤空洞１２内に供給する。また、軽泥水９に代えて、気水分離膜としてシリコン油等を用いる。また、逆浸透膜造水管１８，保護管２２は不要であり、送泥管１３内に直接に逆浸透膜モジュール２３，揚水管２４等を設置すればよい。
【００２８】
上記酸素製造装置２は、上記ＣＡＥＳシステム１の岩盤空洞１２に貯蔵された高圧空気を原料空気とし、昼間に、上記高圧空気に相当する高圧酸素を製造するものであり、図７に示すように、前側処理設備６として、圧縮空気貯蔵タンク５の岩盤空洞１２（図５参照）から導出した高圧空気中の水分，炭酸ガス等の不純成分を除去する２個一対の吸着塔３１，３２を有している。また、低温部７には、熱交換器３３，３４と、膨張タービン３５，３６と、気液分離器３７と、熱交換器３８と、精留塔３９と、過冷却器４０と、液体酸素ポンプ４１等が配設されている。図において、４２は上記両吸着塔３１，３２の再生ガス（後述する排ガス）を加熱する再生ヒーターである。また、４３は液酸蒸発器（図１では、図示せず）であり、前側処理設備６を経た高圧空気の一部と、液体酸素ポンプ４１により精留塔３９の低圧塔３９ｂの底部から液体酸素取り出しパイプ４１ａを介して取り出した液体酸素とを熱交換させ、高圧空気を冷却して気液分離器３７の上部に供給するとともに、液体酸素を加温し蒸発させて製品高圧酸素ガスとして取り出す作用をする。
【００２９】
上記両熱交換器３３，３４は、前側処理設備６を経たのち気液分離器３７に導入する高圧空気と、気液分離器３７から導出する低温空気とを熱交換させ、前側処理設備６を経た高圧空気を冷却して液化する作用をする。また、第１膨張タービン３５では、前側処理設備６を経たのち第１熱交換器３３に導入する前の高圧空気の一部を導入して寒冷を発生させ、気液分離器３７の頂部から延びる低温空気導入路４４に供給する。また、第２膨張タービン３６では、第１熱交換器３３を経たのち第２熱交換器３４に導入する前の高圧低温空気の一部を導入して寒冷を発生させ、気液分離器３７の上部もしくは上記低温空気導入路４４に供給する（この実施の形態では、気液分離器３７の上部に供給している）。
【００３０】
上記気液分離器３７では、その底部に溜まる酸素リッチな液化空気（液体空気）を供給パイプ３７ａにより精留塔３９の高圧塔３９ａに供給し、その上部に溜まる低温空気を低温空気導入路４４により熱交換器３８，高圧塔３９ａの底部に導入する。また、上記熱交換器３８では、低温空気導入路４４を通る低温空気と、精留塔３９の低圧塔３９ｂの上部から排ガス取り出しパイプ３８ａおよび低圧塔３９ｂの頂部から窒素ガス取り出しパイプ３８ｂにより取り出した製品窒素ガスとを熱交換させ、低温空気を冷却して高圧塔３９ａの底部に導入するとともに、窒素ガスを昇温し製品窒素ガスとして取り出し、排ガスを再生ヒーター４２に供給する。
【００３１】
上記高圧塔３９ａでは、精留作用により、その底部に酸素リッチな液化空気を溜め、これを取り出しパイプ４０ａにより取り出して過冷却器４０に導入し、ここで過冷却して低圧塔３９ｂの上部に供給する。また、上記高圧塔３９ａの頂部に溜まる窒素ガスを、低圧塔３９ｂの底部に設けたコンデンサ３９ｃに導入し、ここで凝縮，液化し、つぎに、その一部を上記高圧塔３９ａの頂部に還流し、残りを送給パイプ４０ｂにより過冷却器４０に導入してここで過冷却したのち、その一部を低温塔３９ｂへ還流し、残りを液化窒素として取り出す。そして、取り出した液化窒素を液体ポンプ１０により所望の圧力まで上昇させ、冷却器４５に導入し、ここで、後述するガスタービン用原料空気を冷却したのち、製品高圧窒素ガスとして取り出す。一方、上記低圧塔３９ｂでも、その精留作用により、その底部に液化酸素を溜め、液酸ポンプ４１により取り出して液酸蒸発器４３に導入し、製品高圧酸素ガスとして取り出す。なお、上記低圧塔３９ｂの底部に溜めた液化酸素を、液酸ポンプ４１に導入する前に、液化酸素のままで製品として取り出してもよい。
【００３２】
一方、ガスタービン発電機３は、空気圧縮機４６により外部から取り入れたガスタービン用原料空気を圧縮して燃焼器４７に導入し、ここで燃料と燃焼させ、この燃焼器４７から噴射される燃焼ガスの推力でガスタービン４８を回転させ、この回転力により発電機４９を回転させることを行う。また、ガスタービン４８から排出される高温ガス（排ガス）は、スチーム製造等熱利用したのち、大気中に放出される。この実施の形態では、上記冷却器４５にガスタービン用原料空気を導入し、ここで高圧液化窒素と熱交換させて冷却しているため、空気圧縮機４６の動力を削減することができる。
【００３３】
例えば、６０，０００ｋＷ級のＣＡＥＳシステムを利用した場合には、２０ａｔａの高圧酸素ガスを約２５，０００ｍ3 ／ｈ（０℃、１０１３２５Ｐａ時換算）、液化窒素を約１１，０００ｍ3 ／ｈ（０℃、１０１３２５Ｐａ時換算）製造することができる。そして、液化窒素を１５，０００ｋＷ級のガスタービン発電機３の原料空気の冷却に利用した場合には、約２％の発電が向上する。
【００３４】
上記のように、この実施の形態では、従来の岩盤空洞１２を利用したＣＡＥＳシステム１を利用し、上記岩盤空洞１２に貯蔵した高圧空気を酸素製造装置２の原料空気として用いているため、昼間に、料金の安い夜間電力で製造した高圧空気により深冷空気分離装置を運転することができる。しかも、送泥管１３に設けた逆浸透膜造水管１８により、淡水を生産することができるため、大量の高圧酸素，窒素や上水を必要とする高炉メーカー等には、非常に経済効果が大きい。
【００３５】
図８は本発明の深冷空気分離装置の他の実施の形態を示している。この実施の形態では、上記実施の形態において、上記高圧液化窒素ガスの一部を液化窒素取り出しパイプ４０ｃにより昇温器４８ａに導入し、ここで排ガスと熱交換させて昇温させたのちガスタービン４８に導入し、ガスタービン４８に導入する原料空気量を増やすようにしている。それ以外の部分は上記実施の形態と同様であり、同様の部分には同じ符号を付している。
【００３６】
図９は本発明の深冷空気分離装置のその他の実施の形態を示している。この実施の形態では、図１〜図７に示す実施の形態において、上記低温部７外にタンク等（図示せず）に設け、上記気液分離器３７の底部に溜まる液化空気を上記底部から取り出して上記タンク等に溜めることができるようにしている。そして、夜間に、ＣＡＥＳシステム１の岩盤空洞１２に高圧空気を貯蔵し、この貯蔵した高圧空気を酸素製造装置２の原料空気として用いて酸素製造装置２を運転し、この運転により製造される液化空気を上記タンク等に溜めておく。また、昼間には、上記タンク等に溜めておいた液化空気および上記ＣＡＥＳシステム１の岩盤空洞１２に貯蔵しておいた高圧空気を用い、酸素製造装置２を運転するようにしている。それ以外の部分は上記実施の形態と同様であり、同様の部分には同じ符号を付している。
【００３７】
なお、上記各実施の形態では、高圧酸素ガスを製品として取り出しているが、これに限定するものではなく、液化酸素を製品として取り出してもよい。また、図１および図８に示す深冷空気分離装置において、気液分離器３７から液体空気を取り出してもよい。さらに、ＣＡＥＳシステム１の高圧空気を深冷空気分離装置の原料としているが、液体空気のみを製品として取り出す液体空気製造装置の原料空気としてもよい。
【００３８】
また、本発明のＣＡＥＳシステム１は、上記両実施の形態に限定されるものではなく、公知の各種のＣＡＥＳシステム１を用いることができる。しかも、ＣＡＥＳシステムに大容量高圧空気圧縮機を組み合わせる等、高圧空気の生産性向上等の性能アップを図ることができる。
【００３９】
【発明の効果】
以上のように、本発明の深冷空気分離方法によれば、安価な夜間電力を利用して高圧空気を製造し貯蔵するＣＡＥＳシステムと、深冷空気分離装置とを組み合わせ、昼間に深冷空気分離装置を運転する際に、ＣＡＥＳシステムで安価に製造した高圧空気を、深冷空気分離装置の原料空気として用い、深冷空気分離装置に供給するようにしている。したがって、上記昼間の運転の際に、深冷空気分離装置の原料空気圧縮機を駆動させる必要がなく、昼間の電力コストをほぼゼロにすることができ、電力コストが大幅に低減する。しかも、深冷空気分離装置にＣＡＥＳシステムを組み合わせたものであり、深冷空気分離装置を大型化させる必要がなく、深冷空気分離装置の設備コストは増大しない。このため、深冷空気分離装置で得られる製品ガスを安価に提供することができ、ＣＡＥＳシステムの設備コストに見合うだけの経済性を見出すことができる。また、本発明の深冷空気分離装置によれば、上記深冷空気分離方法を効率よく行うことができる。一方、本発明の液体空気製造方法は、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気を液体空気製造装置の原料空気として用いている。このように、本発明の液体空気製造方法では、安価な夜間電力を利用して高圧空気を製造し貯蔵するＣＡＥＳシステムと、液体空気製造装置とを組み合わせ、昼間に液体空気製造装置を運転する際に、ＣＡＥＳシステムで安価に製造した高圧空気を、液体空気製造装置の原料空気として用い、液体空気製造装置に供給するようにしている。したがって、本発明の液体空気製造方法でも、本発明の深冷空気分離方法の同様に、上記の優れた効果を奏する。
【００４０】
また、本発明では、上記深冷空気分離装置により製造した高圧液化窒素の冷熱を発電設備に利用するようにしたため、発電効率が向上する。また、上記液体空気製造装置により製造した液体空気の冷熱を発電設備に利用するようにしたため、同様の効果を奏する。
【００４１】
また、本発明では、上記冷熱で発電設備のガスタービンに導入する原料空気を冷却するようにしたため、ガスタービンの空気圧縮機の動力が削減でき、その分発電量が増える。
【図面の簡単な説明】
【図１】本発明の深冷空気分離装置の一実施の形態を示す構成図である。
【図２】ＣＡＥＳシステムの説明図である。
【図３】上記ＣＡＥＳシステムの要部を示す断面図である。
【図４】上記ＣＡＥＳシステムの他の要部を示す断面図である。
【図５】上記ＣＡＥＳシステムの作用を示す断面図である。
【図６】上記ＣＡＥＳシステムの作用を示す断面図である。
【図７】酸素製造装置を示す構成図である。
【図８】本発明の深冷空気分離装置の他の実施の形態を示す構成図である。
【図９】本発明の深冷空気分離装置のさらに他の実施の形態を示す構成図である。
【図１０】従来例の一例を示す構成図である。
【図１１】従来例の他の例を示す構成図である。
【符号の説明】
１ ＣＡＥＳシステム
２ 酸素製造装置
１２ 岩盤空洞[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a cryogenic air separation method, a liquid air production method, and an apparatus used therefor, which are improved in energy efficiency by combining with a CAES (Compressed Air Energy Storage) system.
[0002]
[Prior art]
Conventionally, a cryogenic air separation device that uses compressed air generated by a raw material air compressor as a raw material, cools and liquefies it, and separates and generates nitrogen, oxygen, etc. using differences in boiling points of nitrogen, oxygen, etc. The raw material air compressor is always driven.
[0003]
An example of the cryogenic air separation device is shown in FIG. The chilled air separation device is a cold containing a raw material air compressor 51, a pretreatment device 52 equipped with an adsorption tower or the like (not shown), a heat exchanger, a rectification tower or the like (both not shown). It is composed of a box 53, a nitrogen compressor 54, an oxygen compressor 55, and the like. Then, the raw material air compressor 51 takes in the raw material air and compresses it, and the pretreatment device 52 compresses the moisture, CO in the compressed raw material air. 2 Pretreatment such as removal of impurities such as an adsorption tower is performed, and then the pretreated raw material air is introduced into the cold box 53, cooled to an ultra-low temperature with a heat exchanger, and introduced into the rectification tower. . In this rectification tower, the introduced raw material air is cooled and liquefied to separate and generate nitrogen, oxygen, etc. using the difference in boiling points of nitrogen, oxygen, etc., and these separated nitrogen, oxygen are led out of the cold box 53. After that, the high pressure nitrogen (N 2 ), High pressure oxygen (O 2 ) And take it out as a product.
[0004]
Another example of the chilled air separation device is shown in FIG. This cryogenic air separation device is found in plants that produce products in liquid form. Once the nitrogen gas is taken out from the cold box 53 at a low pressure, the circulating nitrogen compressor 56 pressurizes the nitrogen gas to about 4.5 MPa and then cools it. Manufacturing liquids. In this case, the circulating nitrogen compressor 56 may be driven only during a time period in which inexpensive electric power is obtained at night. In the figure, 57 is a liquid oxygen tank and 58 is a liquid nitrogen tank.
[0005]
Moreover, the above-mentioned cryogenic air separation device includes a night power type for the purpose of obtaining an energy saving effect. This apparatus produces excessively liquefied gas using low-cost electric power at night, and produces different liquefied gas using the surplus liquefied gas in the daytime. For example, in an apparatus for producing liquid oxygen and liquid nitrogen, liquid nitrogen is produced excessively at night, and liquid oxygen is produced in the daytime using this excess liquid nitrogen. Further, in this cryogenic air separation device, liquid air is produced in the course of the cryogenic air separation. Therefore, this liquid air is produced excessively at night, and this excess liquid air is used during the daytime. Thus, liquid oxygen and liquid nitrogen can be produced. Moreover, liquid air can also be manufactured with the exclusive liquid air manufacturing apparatus which has a raw material air compressor.
[0006]
On the other hand, the CAES system Cheap night Producing high-pressure air using electric power Store System.
[0007]
[Problems to be solved by the invention]
However, in the night power type chilled air separation apparatus, the operation is normally performed during the daytime, and the raw material air is required to be equivalent to the nighttime. The cost has not been significantly reduced. In addition, since the production amount of liquefied gas and liquid air is increased at night, it is necessary to increase the size of night facilities and storage tanks, thereby increasing the facility cost. There is a similar problem when using a dedicated liquid-air manufacturing apparatus. On the other hand, in the CAES system, compared with electric power that produces high-pressure air at night, the amount of power generation in the daytime is small, and the economic efficiency corresponding to the equipment cost cannot be found.
[0008]
The present invention has been made in view of such circumstances, and by combining the CAES system, the power cost can be significantly reduced, and there is no need to increase the size of the chilled air separation device and the liquid air production device. It is an object of the present invention to provide a cryogenic air separation method, a liquid air production method, and an apparatus used therefor.
[0009]
[Means for Solving the Problems]
In order to achieve the above object, the present invention uses high-pressure air stored in a high-pressure air storage space of a CAES system as raw air for a chilled air separation device. The high-pressure liquefied nitrogen produced by the cryogenic air separation device is heat-exchanged with the raw material air introduced into the gas turbine of the power generation facility, and the high-pressure liquid nitrogen is gasified with the heat of the raw material air and taken out as product high-pressure nitrogen gas. The raw air introduced into the gas turbine is cooled by the cold heat of the high-pressure liquid nitrogen. First, the cryogenic air separation method is used, and the high pressure air stored in the high pressure air storage space of the CAES system is used as the raw material air of the liquid air production apparatus. The liquid air produced by the liquid air production apparatus is subjected to heat exchange with the raw material air to be introduced into the gas turbine of the power generation facility, and the liquid air is gasified and taken out with the hot heat of the raw material air. , Cooling the raw air introduced into the gas turbine The liquid air production method is a second gist, and the raw air of the cryogenic air separator is high-pressure air stored in the high-pressure air storage space of the CAES system. The high-pressure liquefied nitrogen produced by the cryogenic air separation device is heat-exchanged with the raw material air introduced into the gas turbine of the power generation facility, and the high-pressure liquid nitrogen is gasified and taken out as product high-pressure nitrogen gas by the heat of the raw material air. In addition, the raw air introduced into the gas turbine is cooled by the cold heat of the high-pressure liquid nitrogen. The cryogenic air separation device is the third gist, and the raw air of the liquid air production device is high-pressure air stored in the high-pressure air storage space of the CAES system. The liquid air produced by the liquid air production apparatus is heat-exchanged with the raw material air introduced into the gas turbine of the power generation facility, and the liquid air is gasified and taken out by the hot heat of the raw material air. The raw material air introduced into the gas turbine was cooled. Liquid air production equipment The This is the fourth gist.
[0010]
That is, the cryogenic air separation method of the present invention uses the high-pressure air stored in the high-pressure air storage space of the CAES system as the raw air of the cryogenic air separation device. As described above, the chilled air separation method of the present invention combines a CAES system that manufactures and stores high-pressure air using inexpensive nighttime power and a chilled air separation device, thereby providing a chilled air separation device in the daytime. During operation, high-pressure air produced at low cost by the CAES system is used as raw air for the cryogenic air separation device and supplied to the cryogenic air separation device. Therefore, it is not necessary to drive the raw air compressor of the chilled air separation device during the daytime operation, so that the daytime power cost can be reduced to almost zero, and the power cost is greatly reduced. In addition, since the CAES system is combined with the chilled air separator, it is not necessary to increase the size of the chilled air separator, and the equipment cost of the chilled air separator does not increase. For this reason, the product gas obtained by the cryogenic air separation device can be provided at low cost, and economic efficiency corresponding to the equipment cost of the CAES system can be found. Moreover, according to the cryogenic air separation apparatus of this invention, the said cryogenic air separation method can be performed efficiently. On the other hand, the liquid air manufacturing method of the present invention uses high-pressure air stored in a high-pressure air storage space of the CAES system as raw air for the liquid-air manufacturing apparatus. Thus, in the liquid air manufacturing method of the present invention, when the liquid air manufacturing apparatus is combined with the CAES system that manufactures and stores high-pressure air using inexpensive nighttime power and the liquid air manufacturing apparatus is operated in the daytime, In addition, high-pressure air produced at low cost by the CAES system is used as raw material air for the liquid air production apparatus and supplied to the liquid air production apparatus. Therefore, the liquid air production method of the present invention also exhibits the above-described excellent effects, similar to the chilled air separation method of the present invention.
[0011]
The “deep cold air separation device” in the present invention refers to the production of nitrogen gas, oxygen gas, etc. by separating raw air, such as the air, into cold air (secondarily, liquid such as liquid nitrogen, liquid oxygen, etc. In general, the apparatus includes a raw material air compressing means, an impurity removing means for removing impurities in the raw air, a heat exchange means for cooling the raw air to a cryogenic temperature, a rectifying means, etc. I have. When only the high-pressure air produced by the CAES system is used as the raw air for the cryogenic air separation device (that is, the cryogenic air separation device is operated only by the high-pressure air produced by the CAES system), the raw air compression means is omitted. be able to. In addition, the “liquid air production apparatus” in the present invention is an apparatus for producing liquid air by liquefying raw air such as the atmosphere, and may be constituted by a part of a cryogenic air separation apparatus or dedicated The apparatus may be used. Generally, it is equipped with raw material air compression means, impurity removal means for removing impurities in raw material air, heat exchange means for cooling raw material air to a cryogenic temperature, etc., and only high pressure air produced by CAES system is produced as liquid air When used as the raw material air of the apparatus (that is, the liquid air production apparatus is operated only with the high-pressure air produced by the CAES system), the raw air compression means can be omitted. In the present invention, the “high-pressure air storage space” is constructed using an underground space such as an underground cavity, an internal space such as a pressure vessel provided at various locations such as the sea floor and the summit, pipes, and the like. Any space can be used as long as it is a space for storing high-pressure air and can store high-pressure air, and the structure of the structure forming this space is not limited.
[0012]
Also, The present invention Then , High pressure produced by the above cryogenic air separation device Liquefied nitrogen To use the cold heat of the power generation equipment For , Power generation efficiency is improved. Moreover, the cold air of the liquid air manufactured by the liquid air manufacturing apparatus is used for power generation equipment. For Have the same effect. Examples of power generation facilities include various power generation facilities such as private power generation facilities and commercial power generation facilities.
[0013]
Also, The present invention Then The raw air to be introduced into the gas turbine of the power generation facility is cooled by the cold heat. For The power of the air compressor of the gas turbine can be reduced, and the amount of power generation increases accordingly.
[0014]
DETAILED DESCRIPTION OF THE INVENTION
Next, embodiments of the present invention will be described in detail with reference to the drawings.
[0015]
FIG. 1 shows an embodiment of the cryogenic air separation device of the present invention. In the figure, 1 is a CAES system, 2 is an oxygen production apparatus (deep cold air separation apparatus), and 3 is a gas turbine generator. The CAES system 1 uses a CAES system provided with a conventional rock cavity 12 (see FIG. 2), and includes a CAES compressor 4 that takes in air and compresses the air, and the CAES compressor 4. And a compressed air storage tank 5 for storing compressed high-pressure air (compressed air).
[0016]
As shown in FIG. 2, the compressed air storage tank 5 includes a vertical shaft 11 formed in the soft rock ground in the vertical direction and a desired length (for example, a depth of about 400 m) in the lateral direction (for example, A bedrock cavity 12 (high-pressure air storage space) formed in a length of about 1000 m is provided, and high-pressure air is stored in the bedrock cavity 12 by using night electricity with a low charge.
[0017]
The vertical shaft 11 is composed of a vertical hole (vertical hole having a circular cross section having a diameter of about 6 m) formed by excavating vertically from the ground surface of the soft rock ground using a known vertical hole excavation method. A mud feed pipe 13 (steel pipe having a circular cross section with a diameter of about 2 m) is disposed in the shaft 11 so as to penetrate the shaft, and an upper end opening of the mud feed pipe 13 is adjacent to the shaft 11. It communicates with a heavy mud reservoir 14 (which stores heavy mud 8 [see FIG. 5]) formed on the ground surface. Further, a grout material 15 is filled between the outer peripheral surface of the mud pipe 13 and the inner wall surface of the vertical shaft 11, so that the mud pipe 13 is firmly solidified on the inner wall surface of the vertical shaft 11. (See FIG. 3). In FIG. 2, reference numeral 16 denotes a concrete plug, which is fixed at the lower end of the shaft 11 so as to cover the outer peripheral surface of the mud pipe 13 (see FIG. 4). The pressurized high-pressure air or light mud water 9 (see FIG. 5) stored in the cavity 12 leaks upward through the gap between the inner wall surface of the shaft 11 and the outer peripheral surface of the mud pipe 13. It is preventing.
[0018]
The mud pipe 13 is provided with a high-pressure air circulation pipe 17 made of FRP (fiber reinforced plastic) pipe having a diameter of about 100 mm and a reverse osmosis membrane water-making pipe 18 (see FIG. 5). 3). The lower end of the high-pressure air circulation pipe 17 protrudes outside the mud feeding pipe 13 at the lower end of the mud feeding pipe 13 and then enters the closure plug 16 to penetrate therethrough. The opening is opened downward from the lower end surface of the closing plug 16 (see FIG. 4). The upper end opening of the high-pressure air circulation pipe 17 communicates with a high-pressure air outlet (not shown) of the CAES compressor 4 via a high-pressure air introduction pipe 19 with an on-off valve 19a. The high-pressure air generated by the compressor 4 is introduced into the rock cavity 12 through the high-pressure air introduction pipe 19 and the high-pressure air circulation pipe 17. The upper end opening of the high-pressure air circulation pipe 17 communicates with the pretreatment facility 6 (see FIG. 1) of the oxygen production apparatus 2 via a high-pressure air outlet pipe 20 with an on-off valve 20a. The high pressure air in 12 is led out to the pretreatment facility 6 through the high pressure air circulation pipe 17 and the high pressure air outlet pipe 20.
[0019]
The reverse osmosis membrane water producing pipe 18 includes a protective pipe 22 made of a steel pipe having a circular cross section with a diameter of about 1 m, and a reverse osmosis membrane module 23 (for example, Japanese Patent Laid-Open No. 10-156356) installed below the protective pipe 22. The reverse osmosis membrane module 23) is described in the above, and salt water made of, for example, seawater is introduced into the protective tube 22, and a fresh water collecting pipe (not shown) of the reverse osmosis membrane module 23 is provided. The fresh water collected in the production water tank is pumped through a pumping pipe 24 by a pumping pump (not shown) to produce fresh water. According to the reverse osmosis membrane water producing pipe 18, when water in the fresh water collecting pipe is pumped up, fresh water sandwiching the reverse osmosis membrane is caused by the hydrostatic pressure on the outer periphery of the reverse osmosis membrane module 23 by the salt water in the protective pipe 22. The pressure difference over reverse osmosis is always in a natural state with the internal pressure of the water collection pipe, and it is easy to obtain the pressure difference necessary for reverse osmosis and produce fresh water economically and efficiently. It becomes possible. In addition, the reverse osmosis membrane water-making pipe 18 has a lower end of the protective pipe 22 projecting downward from a lower end of the mud pipe 13 and is embedded and supported at the bottom of the liquid reservoir 12a (see FIG. 2). It is installed in a stable state along the mud pipe 13. In this embodiment, the fresh water produced in this way is used for a large amount of industrial water such as steam and cleaning water used by blast furnace manufacturers.
[0020]
The rock cavity 12 is an underground space (substantially circular section with a diameter of about 10 to 15 m) formed by excavating and forming a length of about 500 m from the lower end of the shaft 11 to the left and right sides using a known rock tunnel excavation method. It is. The rock cavity 12 is formed substantially horizontally so that its diameter decreases from the portion located below the shaft 11 toward the left and right sides, whereby the top end portion 25 of the rock cavity 12 is The end portion 25 is formed with a gentle upward slope from the left and right sides of the end portion 25 toward the top portion 26. In FIG. 2, reference numeral 12 a denotes a liquid reservoir portion that is enlarged and excavated in a concave shape at the center bottom portion of the rock cavity 12 located below the top portion 26.
[0021]
In the bedrock cavity 12, the high-pressure air introduced through the high-pressure air introduction pipe 19 and the high-pressure air circulation pipe 17 is supplied from the heavy mud water reservoir 14 into the bedrock cavity 12 through the mud pipe 13. Due to the hydrostatic pressure of the muddy water 8, it is stored in the rock cavity 12 under a pressure applied from below (see FIG. 5). Further, light mud water 9 is supplied and disposed above the heavy mud water 8. Due to the specific gravity difference between the heavy mud water 8 and the light mud water 9, the mud water in the bedrock cavity 12 is separated from the upper layer by the light mud water 9 and the heavy mud water 8. It has a two-layer structure with the lower layer.
[0022]
The heavy mud water 8 is a suspension obtained by mixing a high specific gravity fine powder such as barite or hematite as a weight adjusting material in a stable state that is difficult to settle, and has a specific gravity of about 1.2 to 2.0. Is a relatively expensive muddy water.
[0023]
On the other hand, the light mud water 9 has a specific gravity of 1.05, for example, a slightly increased amount of bentonite as a thickening material blended in bentonite mud water and a calcium carbonate powder having an average particle size of about 10 to 40 μm as a filler. It is ~ 1.20 muddy water. The light mud water 9 is mixed with, for example, a mud prevention material (LCM) as a clogging material that becomes a core when a mud cake that closes the voids and cracks of the rock mass is formed. Due to the presence of such fillers and packing materials, the mud cake is securely and firmly held in the voids and cracks of the rock mass.
[0024]
In the above configuration, prior to operating the CAES compressor 4 and the compressed air storage tank 5, work to seal the rock cavity 12 by closing the voids and cracks in the inner wall surface of the excavated rock cavity 12. I do. That is, first, water is supplied to the rock cavity 12 for cleaning, and then the heavy mud water 8 is supplied from the mud pipe 13 to fill the rock cavity 12 and the mud pipe 13. Next, the light mud water 9 is put into the rock cavity 12 filled with the heavy mud water 8 through the high-pressure air circulation pipe 17 (only at this time, the high-pressure air circulation pipe 17 is connected to the supply means of the light mud water 9). It is press-fitted while pushing out the heavy mud water 8. In this way, when the mud water 8 and the light mud water 9 are filled in the rock cavity 12 (see FIG. 6), a mud cake is formed in the top end portion 25 of the rock cavity 12 by these muddy water components. The rock cavity 12 is hermetically sealed by closing the gaps and cracks in the rock.
[0025]
Next, when the CAES compressor 4 and the compressed air storage tank 5 are operated, for example, the CAES compressor 4 is driven using low-cost night electricity, thereby generating high-pressure air. Is fed to the rock cavity 12 through the high pressure air introduction pipe 19 and the high pressure air circulation pipe 17. The pressurized high pressure air is stored in the compressed air storage tank 5 in a state in which the hydrostatic pressure by the heavy mud water 8 is loaded from below while the heavy mud water 8 and the light mud water 9 in the rock cavity 12 are pushed down by the pressure. (See FIG. 5). Further, the pushed down heavy mud water 8 sequentially flows into the mud pipe 13 and moves to the heavy mud water reservoir 14 through the mud pipe 13 so as to be pushed up.
[0026]
On the other hand, for example, during the daytime when a large amount of electric power is required, the high pressure air (4.5 Pa, 10 ° C., RH 80%) in the rock cavity 12 is connected to the high pressure air circulation pipe 17 and the high pressure air outlet pipe 20. To the front treatment facility 6 of the oxygen production apparatus 2. By this derivation, the bedrock cavity 12 is replenished with the heavy mud water 8 moved from the heavy mud water reservoir 14, and the state where the high pressure air is pressed from below by the hydrostatic pressure of the heavy mud water 8 is continuously maintained. When the high-pressure air is all derived from the rock cavity 12, the heavy mud water 8 is filled in the rock cavity 12 with the upper layer of the light mud 9 interposed at the top end portion 25 of the rock cavity 12. (See FIG. 6).
[0027]
In this manner, the storage (introduction) and extraction (derivation) of high-pressure air are repeated by the operation of the CAES compressor 4 and the compressed air storage tank 5. In this embodiment, seawater can be used in place of the heavy mud water 8. In this case, seawater is stored in the heavy mud reservoir 14 and supplied into the rock cavity 12 through the mud pipe 13. Further, instead of the light mud water 9, silicon oil or the like is used as the air / water separation membrane. Further, the reverse osmosis membrane water producing pipe 18 and the protection pipe 22 are unnecessary, and the reverse osmosis membrane module 23, the pumping pipe 24 and the like may be installed directly in the mud pipe 13.
[0028]
The oxygen production apparatus 2 produces high-pressure oxygen corresponding to the high-pressure air in the daytime using high-pressure air stored in the rock cavity 12 of the CAES system 1 as raw material air, as shown in FIG. The front-side treatment facility 6 has two pairs of adsorption towers 31 and 32 for removing impure components such as moisture and carbon dioxide in high-pressure air derived from the rock cavity 12 (see FIG. 5) of the compressed air storage tank 5. is doing. Further, the low temperature section 7 includes heat exchangers 33 and 34, expansion turbines 35 and 36, a gas-liquid separator 37, a heat exchanger 38, a rectifying tower 39, a supercooler 40, and liquid oxygen. A pump 41 and the like are provided. In the figure, reference numeral 42 denotes a regenerative heater for heating the regenerated gas (exhaust gas described later) of both adsorption towers 31 and 32. Reference numeral 43 denotes a liquid acid evaporator (not shown in FIG. 1), which is liquidated from a part of the high-pressure air that has passed through the front side treatment facility 6 and from the bottom of the low-pressure column 39b of the rectification column 39 by the liquid oxygen pump 41. Heat exchange is performed with the liquid oxygen taken out through the oxygen take-out pipe 41a, the high-pressure air is cooled and supplied to the upper part of the gas-liquid separator 37, and the liquid oxygen is heated and evaporated to be taken out as a product high-pressure oxygen gas. Works.
[0029]
The heat exchangers 33 and 34 exchange heat between the high-pressure air introduced into the gas-liquid separator 37 after passing through the front-side treatment facility 6 and the low-temperature air led out from the gas-liquid separator 37, thereby The high-pressure air that has passed through is cooled and liquefied. In the first expansion turbine 35, after passing through the front processing facility 6, a part of the high-pressure air before being introduced into the first heat exchanger 33 is introduced to generate cold, and extends from the top of the gas-liquid separator 37. Supply to the low-temperature air introduction path 44. In the second expansion turbine 36, after passing through the first heat exchanger 33, a part of the high-pressure low-temperature air before being introduced into the second heat exchanger 34 is introduced to generate cold, and the gas-liquid separator 37 It is supplied to the upper part or the low-temperature air introduction path 44 (in this embodiment, it is supplied to the upper part of the gas-liquid separator 37).
[0030]
In the gas-liquid separator 37, oxygen-rich liquefied air (liquid air) accumulated at the bottom thereof is supplied to the high-pressure column 39a of the rectifying column 39 by the supply pipe 37a, and the low-temperature air accumulated at the upper portion is supplied to the low-temperature air introduction path 44. To the bottom of the heat exchanger 38 and the high pressure column 39a. In the heat exchanger 38, the low-temperature air passing through the low-temperature air introduction passage 44 and the exhaust gas extraction pipe 38a from the upper portion of the low-pressure column 39b of the rectifying column 39 and the nitrogen gas extraction pipe 38b from the top of the low-pressure column 39b are extracted. The product nitrogen gas is heat-exchanged, the low-temperature air is cooled and introduced into the bottom of the high-pressure tower 39 a, the nitrogen gas is heated and taken out as product nitrogen gas, and the exhaust gas is supplied to the regeneration heater 42.
[0031]
In the high-pressure column 39a, oxygen-rich liquefied air is accumulated at the bottom of the high-pressure column 39a, taken out by a take-out pipe 40a and introduced into the supercooler 40, where it is supercooled and placed above the low-pressure column 39b Supply. Further, nitrogen gas accumulated at the top of the high-pressure column 39a is introduced into a condenser 39c provided at the bottom of the low-pressure column 39b, where it is condensed and liquefied, and then a part thereof is returned to the top of the high-pressure column 39a. Then, the remainder is introduced into the supercooler 40 by the feed pipe 40b and supercooled here, and then a part thereof is refluxed to the low temperature tower 39b, and the remainder is taken out as liquefied nitrogen. And the taken-out liquefied nitrogen is raised to a desired pressure with the liquid pump 10, and it introduce | transduces into the cooler 45, Here, after cooling the gas turbine raw material air mentioned later, it takes out as product high-pressure nitrogen gas. On the other hand, in the low-pressure column 39b as well, due to the rectification action, liquefied oxygen is accumulated at the bottom, taken out by the liquid acid pump 41, introduced into the liquid acid evaporator 43, and taken out as product high-pressure oxygen gas. Note that the liquefied oxygen stored in the bottom of the low-pressure column 39b may be taken out as a product as liquefied oxygen before being introduced into the liquid acid pump 41.
[0032]
On the other hand, the gas turbine generator 3 compresses the gas turbine raw air taken in from the outside by the air compressor 46 and introduces it into the combustor 47, where it is burned with fuel, and the combustion injected from the combustor 47. The gas turbine 48 is rotated by the thrust of the gas, and the generator 49 is rotated by this rotational force. Further, the high-temperature gas (exhaust gas) discharged from the gas turbine 48 is released into the atmosphere after using heat such as steam production. In this embodiment, since the gas turbine raw air is introduced into the cooler 45 and is cooled by exchanging heat with high-pressure liquefied nitrogen, the power of the air compressor 46 can be reduced.
[0033]
For example, when a 60,000 kW class CAES system is used, a high pressure oxygen gas of 20 ata is about 25,000 m. Three / H (converted at 0 ° C, 101325 Pa), liquefied nitrogen about 11,000m Three / H (converted to 0 ° C. and 101325 Pa hours). When liquefied nitrogen is used for cooling the raw air of the 15,000 kW class gas turbine generator 3, power generation is improved by about 2%.
[0034]
As described above, in this embodiment, the CAES system 1 using the conventional rock cavity 12 is used, and the high-pressure air stored in the rock cavity 12 is used as the raw material air of the oxygen production apparatus 2. In addition, the chilled air separation device can be operated with high-pressure air produced with low-cost nighttime electric power. Moreover, since the reverse osmosis membrane water producing pipe 18 provided in the mud pipe 13 can produce fresh water, it is very economical for blast furnace manufacturers who require a large amount of high-pressure oxygen, nitrogen and clean water. large.
[0035]
FIG. 8 shows another embodiment of the cryogenic air separation device of the present invention. In this embodiment, in the above embodiment, a part of the high-pressure liquefied nitrogen gas is introduced into the temperature riser 48a through the liquefied nitrogen take-out pipe 40c, where the gas turbine is heated by exchanging heat with the exhaust gas. The amount of raw material air introduced into the gas turbine 48 is increased. Other parts are the same as those in the above embodiment, and the same reference numerals are given to the same parts.
[0036]
FIG. 9 shows another embodiment of the cryogenic air separation device of the present invention. In this embodiment, in the embodiment shown in FIG. 1 to FIG. 7, liquefied air that is provided in a tank or the like (not shown) outside the low temperature portion 7 and accumulates at the bottom of the gas-liquid separator 37 is introduced from the bottom. It can be taken out and stored in the tank or the like. Then, at night, high pressure air is stored in the rock cavity 12 of the CAES system 1, the oxygen production apparatus 2 is operated using the stored high pressure air as raw material air of the oxygen production apparatus 2, and the liquefaction produced by this operation Air is stored in the tank or the like. In the daytime, the oxygen production apparatus 2 is operated using liquefied air stored in the tank or the like and high-pressure air stored in the rock cavity 12 of the CAES system 1. Other parts are the same as those in the above embodiment, and the same reference numerals are given to the same parts.
[0037]
In each of the above embodiments, the high-pressure oxygen gas is taken out as a product. However, the present invention is not limited to this, and liquefied oxygen may be taken out as a product. Also The figure 1 and FIG. 8, the liquid air may be taken out from the gas-liquid separator 37. Furthermore, although the high-pressure air of the CAES system 1 is used as the raw material of the chilled air separation device, it may be used as the raw material air of the liquid air manufacturing device that takes out only liquid air as a product.
[0038]
Further, the CAES system 1 of the present invention is not limited to both the above-described embodiments, and various known CAES systems 1 can be used. In addition, it is possible to improve performance such as productivity improvement of high-pressure air by combining a CAES system with a large-capacity high-pressure air compressor.
[0039]
【The invention's effect】
As described above, according to the chilled air separation method of the present invention, a CAES system that manufactures and stores high-pressure air using inexpensive nighttime power and a chilled air separation device are combined, and chilled air is produced in the daytime. When the separator is operated, high-pressure air produced at low cost by the CAES system is used as raw air for the cryogenic air separator and is supplied to the cryogenic air separator. Therefore, it is not necessary to drive the raw air compressor of the chilled air separation device during the daytime operation, so that the daytime power cost can be reduced to almost zero, and the power cost is greatly reduced. Moreover, the CAES system is combined with the chilled air separation device, and it is not necessary to increase the size of the chilled air separation device, and the equipment cost of the chilled air separation device does not increase. For this reason, the product gas obtained by the cryogenic air separation device can be provided at a low cost, and economic efficiency corresponding to the equipment cost of the CAES system can be found. Moreover, according to the cryogenic air separation apparatus of this invention, the said cryogenic air separation method can be performed efficiently. On the other hand, the liquid air production method of the present invention uses high-pressure air stored in a high-pressure air storage space of the CAES system as raw air for the liquid-air production apparatus. Thus, in the liquid air manufacturing method of the present invention, when the liquid air manufacturing apparatus is combined with the CAES system that manufactures and stores high-pressure air using inexpensive nighttime power and the liquid air manufacturing apparatus is operated in the daytime, In addition, high-pressure air produced at a low cost by the CAES system is used as raw material air for the liquid air production apparatus and is supplied to the liquid air production apparatus. Therefore, the liquid air production method of the present invention also exhibits the above-described excellent effects as in the case of the cold air separation method of the present invention.
[0040]
Also, The present invention Then , High pressure produced by the above cryogenic air separation device Liquefied nitrogen To use the cold heat of the power generation equipment For , Power generation efficiency is improved. Moreover, the cold air of the liquid air manufactured by the liquid air manufacturing apparatus is used for power generation equipment. For Have the same effect.
[0041]
Also, The present invention Then The raw air to be introduced into the gas turbine of the power generation facility is cooled by the cold heat. For The power of the air compressor of the gas turbine can be reduced, and the amount of power generation increases accordingly.
[Brief description of the drawings]
FIG. 1 is a configuration diagram showing an embodiment of a cryogenic air separation device of the present invention.
FIG. 2 is an explanatory diagram of a CAES system.
FIG. 3 is a cross-sectional view showing a main part of the CAES system.
FIG. 4 is a cross-sectional view showing another main part of the CAES system.
FIG. 5 is a cross-sectional view showing the operation of the CAES system.
FIG. 6 is a sectional view showing the operation of the CAES system.
FIG. 7 is a configuration diagram showing an oxygen production apparatus.
FIG. 8 is a configuration diagram showing another embodiment of the cryogenic air separation device of the present invention.
FIG. 9 is a configuration diagram showing still another embodiment of the cryogenic air separation device of the present invention.
FIG. 10 is a block diagram showing an example of a conventional example.
FIG. 11 is a configuration diagram illustrating another example of a conventional example.
[Explanation of symbols]
1 CAES system
2 Oxygen production equipment
12 Rock cavity

Claims (6)

ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気を深冷空気分離装置の原料空気として用い、この深冷空気分離装置により製造した高圧液化窒素を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記高圧液体窒素をガス化し製品高圧窒素ガスとして取り出すとともに、上記高圧液体窒素の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにしたことを特徴とする深冷空気分離方法。The high-pressure air stored in the high-pressure air storage space of the CAES system is used as the raw air for the cryogenic air separation device, and the high-pressure liquefied nitrogen produced by this deep-cooling air separation device is introduced into the gas turbine of the power generation facility and is heat exchange, the high pressure liquid nitrogen in heat of the feed air is taken out as product high pressure nitrogen gas gasified in cold of the high pressure liquid nitrogen, that was so that to cool the feed air to be introduced into the gas turbine A featured cryogenic air separation method. 上記製品高圧窒素ガスの一部を、上記ガスタービンから排出される排ガスと熱交換させて昇温させたのち上記ガスタービンに導入するようにした請求項１記載の深冷空気分離方法。2. The deep cold air separation method according to claim 1 , wherein a part of the product high-pressure nitrogen gas is heat-exchanged with exhaust gas discharged from the gas turbine to raise the temperature and then introduced into the gas turbine . ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気を液体空気製造装置の原料空気として用い、この液体空気製造装置により製造した液体空気を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記液体空気をガス化して取り出すとともに、上記液体空気の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにしたことを特徴とする液体空気製造方法。 The high-pressure air stored in the high-pressure air storage space of the CAES system is used as the raw material air of the liquid air production device, and the liquid air produced by this liquid air production device is heat-exchanged with the raw material air introduced into the gas turbine of the power generation facility. A method for producing liquid air , characterized in that the liquid air is gasified and taken out with the warm heat of the raw material air, and the raw air introduced into the gas turbine is cooled with the cold heat of the liquid air. 深冷空気分離装置の原料空気が、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気であり、上記深冷空気分離装置により製造した高圧液化窒素を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記高圧液体窒素をガス化し製品高圧窒素ガスとして取り出すとともに、上記高圧液体窒素の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにしたことを特徴とする深冷空気分離装置。 The raw air of the cryogenic air separator is the high pressure air stored in the high pressure air storage space of the CAES system, and the high pressure liquefied nitrogen produced by the cryogenic air separator is introduced into the gas turbine of the power generation facility and is heat exchanged with the high pressure liquid nitrogen in heat of the feed air is taken out as product high pressure nitrogen gas gasified in cold of the high pressure liquid nitrogen, it was so that to cool the feed air to be introduced into the gas turbine A cryogenic air separator characterized by the above. 上記製品高圧窒素ガスの一部を、上記ガスタービンから排出される排ガスと熱交換させて昇温させたのち上記ガスタービンに導入するようにした請求項４記載の深冷空気分離装置。 5. The cryogenic air separation device according to claim 4 , wherein a part of the high-pressure nitrogen gas of the product is heat-exchanged with the exhaust gas discharged from the gas turbine to raise the temperature and then introduced into the gas turbine . 液体空気製造装置の原料空気が、ＣＡＥＳシステムの高圧空気貯蔵用空間に貯蔵した高圧空気であり、上記液体空気製造装置により製造した液体空気を、発電設備のガスタービンに導入する原料空気と熱交換させ、この原料空気の温熱で上記液体空気をガス化して取り出すとともに、上記液体空気の冷熱で、上記ガスタービンに導入する原料空気を冷却するようにしたことを特徴とする液体空気製造装置。 The raw material air of the liquid air production device is high pressure air stored in the high pressure air storage space of the CAES system, and the liquid air produced by the liquid air production device exchanges heat with the raw material air introduced into the gas turbine of the power generation facility. The liquid air production apparatus is characterized in that the liquid air is gasified and taken out with the warm heat of the raw material air, and the raw air introduced into the gas turbine is cooled with the cold heat of the liquid air.
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