JPH0663699B2 - Recovery method of carbon dioxide emitted from liquefied natural gas-fired power plant - Google Patents
Recovery method of carbon dioxide emitted from liquefied natural gas-fired power plantInfo
- Publication number
- JPH0663699B2 JPH0663699B2 JP2155753A JP15575390A JPH0663699B2 JP H0663699 B2 JPH0663699 B2 JP H0663699B2 JP 2155753 A JP2155753 A JP 2155753A JP 15575390 A JP15575390 A JP 15575390A JP H0663699 B2 JPH0663699 B2 JP H0663699B2
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- natural gas
- gas
- liquefied natural
- power plant
- 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.)
- Expired - Fee Related
Links
Classifications
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0027—Oxides of carbon, e.g. CO2
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- 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
- F25J1/0221—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 using the cold stored in an external cryogenic component in an open refrigeration loop
- F25J1/0222—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 using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an intermediate heat exchange fluid between the cryogenic component and the fluid to be liquefied
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- 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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
-
- 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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
-
- 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]
-
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Carbon And Carbon Compounds (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） この発明は、燃料として液化天然ガス（以下、LNGと表
記する）を用いる火力発電所のボイラー又はガスタービ
ンから排出される燃焼排ガス中の二酸化炭素（以下、CO
２と表記する）を回収し、大気中に放散することを防止
するCO２の回収方法に関する。DETAILED DESCRIPTION OF THE INVENTION (Industrial field of application) The present invention relates to carbon dioxide in combustion exhaust gas discharged from a boiler or a gas turbine of a thermal power plant using liquefied natural gas (hereinafter referred to as LNG) as a fuel. Carbon (hereinafter CO
(Referred to as “ 2” ) to prevent CO 2 from being released into the atmosphere.
（従来の技術） 近年、増加の一途をたどるCO２ガスによる地球の温暖化
現象が世界的な問題となっており、全世界的にその削減
が求められている。日本において発生するCO２の約３割
は火力発電所からのもので、電気事業としても今後CO２
による地球温暖化問題については有効な対応が迫られて
いる。(Prior Art) In recent years, the global warming phenomenon caused by the increasing amount of CO 2 gas has become a global problem, and its reduction is required worldwide. About 30% of the CO 2 generated in Japan comes from thermal power plants, and CO 2
There is a pressing need for effective responses to the global warming issue caused by the.
しかし、火力発電所から排出されるCO２は膨大な量にの
ぼり、これを環境保全の点からも効率的かつ経済的に回
収する方式についての報告はほとんどない。However, the amount of CO 2 emitted from a thermal power plant is enormous, and there are few reports on a method of efficiently and economically recovering this from the viewpoint of environmental protection.
一般に、CO２の回収方法としては、化学吸収法、物理吸
着法や膜分離法、水酸化カルシウムによる沈澱法などが
知られている。Generally, as a CO 2 recovery method, a chemical absorption method, a physical adsorption method, a membrane separation method, a precipitation method using calcium hydroxide and the like are known.
（発明が解決しようとする課題） しかしながら、これらの方法は比較的小規模の装置にお
いてCO２を取除く場合のもので、火力発電所から排出さ
れる膨大なCO２の回収、固定化には技術的、経済的観点
から必ずしも現実的でない。(Problems to be solved by the invention) However, these methods are for removing CO 2 in a relatively small-scale device, and are not suitable for collecting and fixing a huge amount of CO 2 emitted from a thermal power plant. Not necessarily realistic from a technical and economic perspective.
本発明は、LNGを燃料とする火力発電所から排出される
膨大な量のCO２を効率良く、かつ経済的に回収する方法
を提供することを目的とする。It is an object of the present invention to provide a method for efficiently and economically recovering a huge amount of CO 2 emitted from a LNG-fueled thermal power plant.
（課題を解決するための手段） かかる目的を達成するため本発明は、ボイラー又はガス
タービンで自らが発生させた燃焼排ガスの一部と純酸素
との混合ガスを酸化剤として燃料のLNGを燃焼させ、そ
の排ガス中のCO２をLNGを気化させる際の冷熱を利用し
て液化し、液化天然ガス焚き火力発電所から排出される
CO２を液化CO２として回収するようにしている。(Means for Solving the Problem) In order to achieve such an object, the present invention burns LNG as a fuel by using a mixed gas of a part of combustion exhaust gas generated by itself in a boiler or a gas turbine and pure oxygen as an oxidant. CO 2 in the exhaust gas is liquefied by using the cold heat when vaporizing LNG, and is discharged from the liquefied natural gas-fired power plant.
CO 2 is collected as liquefied CO 2 .
（作用） したがって、天然ガスはボイラー又はガスタービンにお
いて、純酸素と循環使用される燃焼排ガスの一部との混
合ガスを酸化剤として燃焼し、窒素酸化物（NOx）を生
成することなく、CO２と酸素と水分のみから成る燃焼排
ガスになる。そして、この燃焼排ガス中のCO２はLNGの
気化冷熱を利用して冷却され、液化CO２として回収され
る。(Operation) Therefore, natural gas burns in a boiler or a gas turbine as a oxidant using a mixed gas of pure oxygen and a part of the combustion exhaust gas that is circulated, and produces CO2 without producing nitrogen oxides (NOx). It becomes the combustion exhaust gas which consists only of 2 , oxygen and water. Then, CO 2 in the combustion exhaust gas is cooled by utilizing the cold heat of vaporization of LNG, and is recovered as liquefied CO 2 .
（実施例） 以下、この発明を図面に基づいて詳しく説明する。(Example) Hereinafter, the present invention will be described in detail with reference to the drawings.
第１図に本発明のCO２回収方法の具体例をフローチャー
トで示す。FIG. 1 is a flowchart showing a specific example of the CO 2 recovery method of the present invention.
図中符号１はLNGタンクである。このLNGタンク１に貯蔵
されるLNGは、管２を経て第１の熱交換器３に送られ
る。ここでLNGと中間熱媒体であるエチレンガスとが熱
交換し、LNGは加熱されて温度約−10℃のガス状の天然
ガスとなる。一方、エチレンガスは−55℃程度に冷却液
化される。気化した天然ガスは管４を経て第２の熱交換
器５に送られ、ここで火力発電所のボイラー又はガスタ
ービン７からの燃焼排ガスと更に熱交換して約30℃に加
熱される。そして、この天然ガスは管６を経てボイラー
又はガスタービン７に送られ燃焼する。尚、第２の熱交
換器５としては例えばコア型熱交換器の採用が好まし
い。Reference numeral 1 in the figure is an LNG tank. The LNG stored in the LNG tank 1 is sent to the first heat exchanger 3 via the pipe 2. Here, the LNG and the intermediate heat medium, ethylene gas, exchange heat, and the LNG is heated to become gaseous natural gas at a temperature of about -10 ° C. On the other hand, ethylene gas is cooled and liquefied to about -55 ° C. The vaporized natural gas is sent to the second heat exchanger 5 via the pipe 4, where it is further heat-exchanged with the combustion exhaust gas from the boiler or the gas turbine 7 of the thermal power plant and heated to about 30 ° C. Then, this natural gas is sent to the boiler or gas turbine 7 through the pipe 6 and burned. In addition, as the second heat exchanger 5, for example, a core heat exchanger is preferably adopted.
一方、図中符号８は、深冷蒸留方式による空気分離装置
である。この空気分離装置８において分離精製された酸
素ガスは、管９を経てガス混合器22に送られ、ここで分
岐管10により再循環される燃焼排ガスと混合された後、
管23を経てボイラー又はガスタービン７に送られ、酸化
剤として天然ガスを燃焼させる。したがって、ボイラー
又はガスタービン７は、空気を使用せず純酸素と燃焼排
ガスとの混合ガスを酸化剤として天然ガスを燃焼させる
ものであり、その燃焼排ガスは窒素酸化物（NOx）を含
まず、CO２と酸素と水分のみからなるものとなる。On the other hand, reference numeral 8 in the figure is an air separation device by a cryogenic distillation system. The oxygen gas separated and purified in the air separation device 8 is sent to the gas mixer 22 via the pipe 9 and mixed therewith by the combustion exhaust gas recirculated by the branch pipe 10,
It is sent to the boiler or gas turbine 7 via the pipe 23 and burns natural gas as an oxidant. Therefore, the boiler or the gas turbine 7 burns natural gas using a mixed gas of pure oxygen and combustion exhaust gas as an oxidant without using air, and the combustion exhaust gas does not contain nitrogen oxide (NOx), It consists only of CO 2 , oxygen and water.
ボイラー又はガスタービン７からの燃焼排ガスの一部、
通常65〜75％は、分岐管10を経てボイラー又はガスター
ビン７に酸化剤の酸素濃度調整用として戻され、残部が
排出される。排出される燃焼排ガスは、コンプレッサー
11に送られ、ここで約10kg／cm２Ｇに加圧されたのち、
管12を通って予備冷却器13に送られ、海水、川水、井水
などとの間の熱交換によって約40℃程度にまで冷却され
る。この予備冷却器13は、例えばシェル／チューブ型の
熱交換器が用いられ、耐蝕性の高いステンレス鋼で作ら
れたものが好ましい。この予備冷却器13での冷却に伴
い、燃焼排ガス中の水分の一部が凝縮水として分離さ
れ、排出される。次いで、予備冷却器13を出た燃焼排ガ
スは、前述の第２の熱交換器５に導入され、ここで前述
の約−10℃の天然ガスと熱交換して約10℃に冷却され
る。この冷却によって燃焼排ガス中の水分の残部のほと
んどが凝縮水として分離され、同様に排出される。更
に、この燃焼排ガスは、管14を通って脱水塔15に送られ
る。脱水塔15はモレキュラーシーブス、シリカゲルなど
の水分を吸着する吸着剤が充填された二基の吸着筒から
なり、一基が吸着工程に供されている間に他の一基が再
生され、吸着工程と再生工程とを交互に繰り返すことに
よって連続的に水分を吸着、除去するものである。燃焼
排ガスは、脱水塔15において水の凝固による閉塞が生じ
ないようにその含水量が1ppm以下の乾燥状態にされてか
ら、管16を経てCO２液化器17に送られる。CO２液化器17
は、燃焼排ガス中のCO２が熱交換器内で固結することを
避けるため、エチレンを中間熱媒体（冷媒）として採用
している。したがって、燃焼排ガスは、LNGとの熱交換
によって低温（−55℃）となった液化エチレンによって
冷却され、約−50℃の液化CO２となって管18から貯蔵タ
ンク19に貯えられる。この液化CO２は一定量が貯まる
と、適当な方法により処理あるいは処分若しくは再利用
される。一方、中間熱媒体としてのエチレンは、管20を
介して第１の熱交換器３とCO２液化器17との間を循環
し、CO２液化器17において燃焼排ガスの熱で気化し、前
記第１の熱交換器３においてLNGと熱交換して液化さ
れ、再びCO２液化器17に送られるようになっている。Part of the combustion exhaust gas from the boiler or gas turbine 7,
Usually, 65 to 75% is returned to the boiler or the gas turbine 7 for adjusting the oxygen concentration of the oxidant through the branch pipe 10, and the rest is discharged. The flue gas discharged is the compressor
After being sent to 11, where it is pressurized to about 10 kg / cm 2 G,
It is sent to the precooler 13 through the pipe 12, and is cooled to about 40 ° C. by heat exchange with seawater, river water, well water and the like. The pre-cooler 13 is preferably a shell / tube type heat exchanger and is preferably made of stainless steel having high corrosion resistance. Along with the cooling by the precooler 13, a part of the water content in the combustion exhaust gas is separated as condensed water and discharged. Next, the flue gas discharged from the precooler 13 is introduced into the second heat exchanger 5 described above, where it is heat-exchanged with the natural gas of about -10 ° C and cooled to about 10 ° C. By this cooling, most of the remaining water content in the combustion exhaust gas is separated as condensed water and is similarly discharged. Further, this combustion exhaust gas is sent to the dehydration tower 15 through the pipe 14. The dehydration tower 15 consists of two adsorption columns filled with an adsorbent that adsorbs moisture such as molecular sieves and silica gel, and while one group is being subjected to the adsorption step, the other group is regenerated and the adsorption step is performed. The water is continuously adsorbed and removed by alternately repeating the above and the regeneration process. The combustion exhaust gas is sent to the CO 2 liquefier 17 via the pipe 16 after being dried in the dehydration tower 15 so that the water content thereof is not more than 1 ppm so as not to be clogged due to the solidification of water. CO 2 liquefier 17
Uses ethylene as an intermediate heat medium (refrigerant) in order to prevent CO 2 in the combustion exhaust gas from solidifying in the heat exchanger. Therefore, the combustion exhaust gas is cooled by the liquefied ethylene that has become a low temperature (−55 ° C.) due to heat exchange with LNG, and becomes liquefied CO 2 at about −50 ° C., which is stored in the storage tank 19 from the pipe 18. When a certain amount of this liquefied CO 2 is stored, it is treated, disposed of, or reused by an appropriate method. On the other hand, ethylene as an intermediate heat medium circulates between the first heat exchanger 3 and the CO 2 liquefier 17 via the pipe 20, and is vaporized by the heat of the combustion exhaust gas in the CO 2 liquefier 17, The first heat exchanger 3 exchanges heat with LNG to be liquefied, and is sent to the CO 2 liquefier 17 again.
また、脱水塔15の吸着剤の再生は、ボイラー又はガスタ
ービン廃熱等及び空気分離器８で分離された乾燥窒素ガ
スや脱水塔15から導出される乾燥燃焼排ガスを用いるこ
とによって行われる。また、第２の熱交換器５で約30℃
に加熱された天然ガスの一部は管21から都市ガスとして
供給することもできる。さらに、予備冷却器13および第
２の熱交換器５で凝縮、分離された凝縮水は炭酸を含ん
でいて酸性であるため、アルカリで中和後、放流するこ
とが望ましい。The regeneration of the adsorbent in the dehydration tower 15 is performed by using the waste heat of the boiler or the gas turbine, the dry nitrogen gas separated by the air separator 8 or the dry combustion exhaust gas derived from the dehydration tower 15. Also, at the second heat exchanger 5, about 30 ℃
Part of the natural gas heated to the above can be supplied as city gas through the pipe 21. Furthermore, since the condensed water condensed and separated by the precooler 13 and the second heat exchanger 5 contains carbonic acid and is acidic, it is desirable to discharge the condensed water after neutralizing with alkali.
なおボイラー又はガスタービン７のスタートアップ時に
は、LNGタンク１からのLNGを通常のLNG気化装置に送っ
て気化させ、ボイラー又はガスタービン７に送る方法や
別のスタートアップ用天然ガスタンクからの天然ガスを
ボイラー又はガスタービン７に送る方法などが採用され
る。At the time of startup of the boiler or gas turbine 7, LNG from the LNG tank 1 is sent to a normal LNG vaporizer to be vaporized and sent to the boiler or gas turbine 7, or natural gas from another startup natural gas tank is used in the boiler or A method of sending to the gas turbine 7 or the like is adopted.
このようなCO２の回収方法においては、燃焼排ガス中の
CO２を液化するための冷熱にLNGの気化のための潜熱お
よび顕熱を利用しているので、系全体としてのエネルギ
ーコストが十分低いものとなり、膨大な量のCO２を安価
に回収できる。また、CO２液化のために中間熱媒体とし
てエチレンガスを用いているため、CO２のドライアイス
化が妨げられ、CO２液化器17の閉塞などのトラブルが防
止される。さらに、その例では、酸化剤として空気の代
わりに純酸素と再循環燃焼排ガスの混合ガスを用いるの
で燃焼排ガス中には窒素酸化物が全く含まれず、脱硝装
置が不要であるとともに、燃焼排ガスの流量が減少し、
配管、圧縮器等の装置の小型化およびボイラー効率の向
上が可能となる。また、燃焼排ガス中の酸素を循環使用
すれば、大気中に放出される燃焼排ガスがないため、煙
突も不要となる。In such a CO 2 recovery method,
Since the latent heat and the sensible heat for vaporizing LNG are used for the cold heat for liquefying CO 2 , the energy cost of the entire system is sufficiently low, and a huge amount of CO 2 can be recovered at low cost. Moreover, due to the use of ethylene gas as an intermediate heating medium for CO 2 liquefaction, dry ice of CO 2 is prevented, troubles such as clogging of the CO 2 liquefier 17 is prevented. Furthermore, in that example, since a mixed gas of pure oxygen and recirculated combustion exhaust gas is used instead of air as an oxidant, nitrogen oxides are not contained in the combustion exhaust gas at all, and a denitration device is not required, and the combustion exhaust gas The flow rate decreases,
It is possible to downsize equipment such as pipes and compressors and improve boiler efficiency. Further, if oxygen in the combustion exhaust gas is circulated and used, there is no combustion exhaust gas released into the atmosphere, so a chimney is not necessary.
（発明の効果） 以上の説明により明らかなように、本発明は、液化天然
ガス焚き火力発電所から排出される二酸化炭素をLNGの
気化冷熱を利用して回収するようにしているので、運転
コストを少なくすることができ、また設備的に実証され
ているものも多く、実現性が高い。(Effect of the invention) As is apparent from the above description, the present invention is designed to recover carbon dioxide emitted from a liquefied natural gas-fired thermal power plant by utilizing the cold heat of vaporization of LNG, and thus the operating cost. Can be reduced, and there are many things that have been proved to be equipment-based, so it is highly feasible.
また、燃焼用空気の代わりに燃焼排ガスの一部と純酸素
との混合ガスをボイラー又はガスタービンに供給するた
め、燃焼排ガスの主成分がCO２となる。しかも、燃焼排
ガスの一部を循環させ、これと純酸素との混合ガスを酸
化剤としてボイラーに供給するため、今まで酸化剤中に
多量に含まれていたＮ２が全く含まれないし、排ガス量
を減少でき、ボイラー効率の向上、煙道及び熱交換器の
小型化が可能となる。また、本発明によると、酸化剤中
にＮ２を含まないためNOxの発生がなくなり、脱硝装置
が不要となると共に大気中に放出するガスが殆どなくな
り、場合によっては煙突が不要となる。Moreover, since a mixed gas of a part of the combustion exhaust gas and pure oxygen is supplied to the boiler or the gas turbine instead of the combustion air, the main component of the combustion exhaust gas is CO 2 . Moreover, since a part of the combustion exhaust gas is circulated and a mixed gas of the exhaust gas and pure oxygen is supplied to the boiler as an oxidant, N 2 which is a large amount contained in the oxidant until now is not contained at all. The amount can be reduced, the boiler efficiency can be improved, and the flue and heat exchanger can be downsized. Further, according to the present invention, since NO 2 is not contained in the oxidizer, NOx is not generated, a denitration device is unnecessary, gas released into the atmosphere is almost eliminated, and a chimney is unnecessary in some cases.
第１図はこの発明のCO２回収方法の一具体例を示すフロ
ーチャートである。 １……LNGタンク、 ３……第１の熱交換器、 ５……第２の熱交換器、 ７……ボイラー又はガスタービン、 ８……空気分離装置、 11……コンプレッサー、 13……予備冷却器、 15……脱水塔、 17……CO２液化器、 19……貯蔵タンク、 22……ガス混合器。FIG. 1 is a flow chart showing a specific example of the CO 2 recovery method of the present invention. 1 ... LNG tank, 3 ... first heat exchanger, 5 ... second heat exchanger, 7 ... boiler or gas turbine, 8 ... air separation device, 11 ... compressor, 13 ... spare Cooler, 15 ... dehydration tower, 17 ... CO 2 liquefier, 19 ... Storage tank, 22 ... Gas mixer.
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 昭59−73415（ＪＰ，Ａ) 特開 昭59−73416（ＪＰ，Ａ) 特開 昭63−305915（ＪＰ，Ａ) 特公 昭63−27285（ＪＰ，Ｂ２) ─────────────────────────────────────────────────── ─── Continuation of the front page (56) References JP-A-59-73415 (JP, A) JP-A-59-73416 (JP, A) JP-A-63-305915 (JP, A) JP-B-63- 27285 (JP, B2)
Claims (4)
おいて、二酸化炭素を主成分とする燃焼排ガスと純酸素
との混合物を酸化剤として液化天然ガス燃料を燃焼さ
せ、その燃焼排ガス中の二酸化炭素を液化天然ガスの気
化熱を利用して液化することを特徴とする液化天然ガス
焚き火力発電所から排出される二酸化炭素の回収方法。1. In a boiler or a gas turbine of a thermal power plant, a liquefied natural gas fuel is burned by using a mixture of a combustion exhaust gas containing carbon dioxide as a main component and pure oxygen, and carbon dioxide in the combustion exhaust gas is removed. A method for recovering carbon dioxide discharged from a liquefied natural gas-fired thermal power plant, characterized by liquefying liquefied natural gas by utilizing heat of vaporization.
エチレンを中間熱媒体として行われる請求項１記載の液
化天然ガス焚き火力発電所から排出される二酸化炭素の
回収方法。2. Heat exchange between liquefied natural gas and carbon dioxide,
The method for recovering carbon dioxide discharged from a liquefied natural gas-fired power plant according to claim 1, wherein ethylene is used as an intermediate heat medium.
る請求項１または２記載の液化天然ガス焚き火力発電所
から排出される二酸化炭素の回収方法。3. The method for recovering carbon dioxide discharged from a liquefied natural gas-fired thermal power plant according to claim 1, wherein the discharged carbon dioxide is pre-cooled with seawater.
部をボイラー又はガスタービンにリサイクルする請求項
１ないし３のいずれかに記載の液化天然ガス焚き火力発
電所から排出される二酸化炭素の回収方法。4. A carbon dioxide discharged from a liquefied natural gas-fired power plant according to claim 1, wherein a part of combustion exhaust gas containing carbon dioxide as a main component is recycled to a boiler or a gas turbine. Recovery method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2155753A JPH0663699B2 (en) | 1990-06-14 | 1990-06-14 | Recovery method of carbon dioxide emitted from liquefied natural gas-fired power plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2155753A JPH0663699B2 (en) | 1990-06-14 | 1990-06-14 | Recovery method of carbon dioxide emitted from liquefied natural gas-fired power plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0448185A JPH0448185A (en) | 1992-02-18 |
| JPH0663699B2 true JPH0663699B2 (en) | 1994-08-22 |
Family
ID=15612667
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2155753A Expired - Fee Related JPH0663699B2 (en) | 1990-06-14 | 1990-06-14 | Recovery method of carbon dioxide emitted from liquefied natural gas-fired power plant |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR3150853A1 (en) * | 2023-07-09 | 2025-01-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for liquefying and/or solidifying a gas rich in carbon dioxide |
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| JP2566337B2 (en) * | 1990-09-11 | 1996-12-25 | 三菱重工業株式会社 | CO ▲ 2 ▼ Gas liquefaction method |
| JP2792777B2 (en) * | 1992-01-17 | 1998-09-03 | 関西電力株式会社 | Method for removing carbon dioxide from flue gas |
| DE19531842A1 (en) * | 1995-08-29 | 1997-04-30 | Messer Griesheim Gmbh | Process for reducing flue gas in combustion processes |
| JPH09145003A (en) * | 1995-11-27 | 1997-06-06 | Ishikawajima Harima Heavy Ind Co Ltd | LNG thermal power equipment |
| JP3670229B2 (en) * | 2001-09-05 | 2005-07-13 | 川崎重工業株式会社 | Method and apparatus for producing hydrogen with liquefied CO2 recovery |
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| GB0614250D0 (en) * | 2006-07-18 | 2006-08-30 | Ntnu Technology Transfer As | Apparatus and Methods for Natural Gas Transportation and Processing |
| US7927568B2 (en) * | 2006-10-26 | 2011-04-19 | Foster Wheeler Energy Corporation | Method of and apparatus for CO2 capture in oxy-combustion |
| DE102007029434A1 (en) * | 2007-06-26 | 2009-01-02 | Linde Ag | Process for the disposal of carbon dioxide |
| JP5106448B2 (en) * | 2009-03-10 | 2012-12-26 | 中国電力株式会社 | Carbon dioxide recovery system from exhaust gas |
| KR101103256B1 (en) * | 2009-11-12 | 2012-01-10 | 한국과학기술원 | Oxygen combustion system using heat exchange |
| WO2012104202A1 (en) * | 2011-02-01 | 2012-08-09 | Alstom Technology Ltd | Combined cycle power plant with co2 capture plant |
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| JP6946012B2 (en) * | 2017-02-09 | 2021-10-06 | 三菱重工業株式会社 | CO2 liquefaction system and CO2 liquefaction method |
| IT202000023167A1 (en) * | 2020-10-01 | 2022-04-01 | Saipem Spa | POWER GENERATION PROCESS USING A LIQUID FUEL, AIR AND/OR OXYGEN WITH ZERO CO2 EMISSIONS |
| JP7738314B2 (en) * | 2021-08-27 | 2025-09-16 | 株式会社Jccl | Carbon dioxide recovery device, combustion system, power generation system, and carbon dioxide recovery method |
| JP2024151444A (en) * | 2023-04-12 | 2024-10-25 | エア・ウォーター株式会社 | Manufacturing equipment and manufacturing method |
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| JP6327285B2 (en) | 2013-11-29 | 2018-05-23 | 株式会社三洋物産 | Game machine |
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| JP6327285B2 (en) | 2013-11-29 | 2018-05-23 | 株式会社三洋物産 | Game machine |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR3150853A1 (en) * | 2023-07-09 | 2025-01-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for liquefying and/or solidifying a gas rich in carbon dioxide |
| WO2025011874A2 (en) | 2023-07-09 | 2025-01-16 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for liquefying and/or solidifying a gas rich in carbon dioxide |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0448185A (en) | 1992-02-18 |
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