JPS63174282A - Fuel cell generation process - Google Patents
Fuel cell generation processInfo
- Publication number
- JPS63174282A JPS63174282A JP62003168A JP316887A JPS63174282A JP S63174282 A JPS63174282 A JP S63174282A JP 62003168 A JP62003168 A JP 62003168A JP 316887 A JP316887 A JP 316887A JP S63174282 A JPS63174282 A JP S63174282A
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- anode
- exhaust gas
- fuel
- fuel cell
- 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.)
- Pending
Links
- 239000000446 fuel Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 102
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 50
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 50
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000001301 oxygen Substances 0.000 claims abstract description 35
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 35
- 239000007789 gas Substances 0.000 claims abstract description 29
- 239000003245 coal Substances 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 14
- 238000010248 power generation Methods 0.000 claims description 9
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 7
- 239000002737 fuel gas Substances 0.000 claims 1
- 239000007800 oxidant agent Substances 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 17
- 238000002309 gasification Methods 0.000 abstract description 6
- 238000001816 cooling Methods 0.000 abstract description 5
- 239000007795 chemical reaction product Substances 0.000 abstract description 4
- 230000007423 decrease Effects 0.000 abstract description 3
- 238000005057 refrigeration Methods 0.000 abstract 2
- 230000005494 condensation Effects 0.000 abstract 1
- 238000009833 condensation Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 238000003487 electrochemical reaction Methods 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000003507 refrigerant Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 229910002090 carbon oxide Inorganic materials 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 239000003949 liquefied natural gas Substances 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
- H01M8/0643—Gasification of solid fuel
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/14—Fuel cells with fused electrolytes
- H01M2008/147—Fuel cells with molten carbonates
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M2300/00—Electrolytes
- H01M2300/0017—Non-aqueous electrolytes
- H01M2300/0048—Molten electrolytes used at high temperature
- H01M2300/0051—Carbonates
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は溶融炭酸塩型燃料電池発電プラントに係り、特
に、酸素酸化石炭ガス化ガスを燃料とする場合のプラン
ト効率を高めるのに好適な燃料電池発電方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a molten carbonate fuel cell power generation plant, and particularly to a power generation plant suitable for increasing plant efficiency when oxygen-oxidized coal gasification gas is used as fuel. Related to fuel cell power generation method.
溶融炭酸塩型燃料電池では１発電時にカソードよりアノ
ードへ炭酸イオン（ＣＯａ”″）が移動し。In a molten carbonate fuel cell, carbonate ions (COa"") move from the cathode to the anode during one power generation.
カソードでは、酸素と二酸化炭素が消費され、アノード
では、水と二酸化炭素が発生する。従って。At the cathode, oxygen and carbon dioxide are consumed, and at the anode, water and carbon dioxide are generated. Therefore.
アノードで発生した二酸化炭素をカソードに供給するこ
とにより、電気化学反応は維持される。発電プラントで
は、未反応燃料成分を含むアノード排ガスを空気により
燃焼させ、カソードへ供給する方法が一般的である。こ
の方法では、アノード排ガス中の電気化学反応に有効な
未反応燃料成分を燃焼により消費することになり、さら
に、燃焼により生じた水および空気中の残窒素によりカ
ソードに供給される酸素および二酸化酸素の分圧を低下
させる原因となっていた。The electrochemical reaction is maintained by supplying carbon dioxide generated at the anode to the cathode. In power plants, a common method is to combust anode exhaust gas containing unreacted fuel components with air and supply it to the cathode. In this method, unreacted fuel components that are effective for electrochemical reactions in the anode exhaust gas are consumed by combustion, and oxygen and carbon dioxide are supplied to the cathode by water produced by combustion and residual nitrogen in the air. This caused a decrease in the partial pressure.
特開昭５６−６９７７５号公報では、これらの点を改良
しプラント効率を高めるべく、燃料である液化天然ガス
の冷熱を利用することにより、アノード排ガスより二酸
化炭素を分離することを示している。In order to improve these points and increase plant efficiency, JP-A-56-69775 discloses separating carbon dioxide from anode exhaust gas by utilizing the cold energy of liquefied natural gas as a fuel.
天然ガスを燃料とする燃料電池発電プラントでは、天然
ガスを改質するための熱供給源としてアノード排ガスの
燃焼が必要であるため、特開昭５６−６９７７５号公報
では、アノード排ガス中の未反応燃料成分を電気化学的
に有効には利用できなかった。In a fuel cell power generation plant that uses natural gas as fuel, it is necessary to burn the anode exhaust gas as a heat supply source for reforming the natural gas. Fuel components could not be effectively utilized electrochemically.
上記従来技術は、燃料である液化天然ガスの冷熱を利用
するため、石炭ガス化燃料を用いた場合についての検討
がなされておらず、石炭ガス化燃料を用いる溶融炭酸塩
型燃料電池には適用できなかった。Since the above conventional technology utilizes the cold energy of liquefied natural gas as a fuel, it has not been studied in the case of using coal gasified fuel, and is not applicable to molten carbonate fuel cells that use coal gasified fuel. could not.
本発明の目的は、アノード出口排ガスより二酸化炭素を
分離することにより、石炭ガス化燃料電池発電プラント
の効率を高める燃料電池発電方法を提供することにある
。An object of the present invention is to provide a fuel cell power generation method that improves the efficiency of a coal gasification fuel cell power generation plant by separating carbon dioxide from the anode outlet exhaust gas.
上記目的は、二酸化炭素を含むアノード排ガスを１石炭
ガス化に用いる酸素製造プラントで発生する冷熱により
冷却することにより達成される。The above object is achieved by cooling the anode exhaust gas containing carbon dioxide with cold heat generated in an oxygen production plant used for coal gasification.
〔作用〕
石炭ガス化炉にガス化剤としての酸素を供給する酸素製
造プラントでは、空気を断熱膨張により低温化し酸素の
液化温度−１８３℃以下を達成し。[Operation] In an oxygen production plant that supplies oxygen as a gasifying agent to a coal gasifier, air is lowered in temperature by adiabatic expansion to achieve an oxygen liquefaction temperature of -183°C or lower.
空気中より酸素を分離する６分離後の酸素および窒素は
冷熱を持っており、アノード排ガスはあらかじめ常温近
くまで冷却され水を分離した後に酸素および窒素の冷却
を用いて二酸化炭素を凝固点−７８，５℃以下に冷却し
、二酸化炭素が分離される。Separating oxygen from the air 6 After separation, oxygen and nitrogen have cold energy, and the anode exhaust gas is cooled in advance to near room temperature and after separating water, the cooling of oxygen and nitrogen is used to convert carbon dioxide to a freezing point of -78, Cool to below 5°C and carbon dioxide is separated.
分離された二酸化炭素はカソードに供給され、アノード
からカソードへは二酸化炭素のみが供給されるため、カ
ソードの酸素および二酸化炭素の分圧を高く維持できる
。また、二酸化炭素を分離する過程で水分も分離したア
ノード排ガスは、−酸化炭素、水素等の電気化学反応に
有効な成分が残り、ガスをアノード入口ヘリサイクルす
ることにより、燃料を電気化学反応に有効に利用するこ
とが可能になる。The separated carbon dioxide is supplied to the cathode, and only carbon dioxide is supplied from the anode to the cathode, so that the partial pressures of oxygen and carbon dioxide at the cathode can be maintained high. In addition, the anode exhaust gas from which moisture has been separated in the process of separating carbon dioxide remains with components effective for electrochemical reactions such as carbon oxide and hydrogen, and by recycling the gas to the anode inlet, the fuel can be used for electrochemical reactions. It becomes possible to use it effectively.
以下、本発明の一実施例を第１図により説明する。溶融
炭酸塩型燃料電池（以下燃料電池）１のアノード２には
石炭ガス化炉４より熱回収ボイラ９を通り燃料精製装置
１０を通った配管が接続される。アノード２の出口には
、熱交換器１１が接続され、さらに気水分離装置１２が
接続される。An embodiment of the present invention will be described below with reference to FIG. An anode 2 of a molten carbonate fuel cell (hereinafter referred to as a fuel cell) 1 is connected to a pipe that extends from a coal gasifier 4, passes through a heat recovery boiler 9, and passes through a fuel purification device 10. A heat exchanger 11 is connected to the outlet of the anode 2, and a steam/water separator 12 is further connected to the outlet.
酸素酸化石炭ガス化炉（以下石炭ガス化炉）４へは石炭
供給装置５および酸素製造装置７が接続されている。酸
素製造装置７は冷媒供給管１８と冷媒戻り管１９とによ
り二酸化炭素分離装置１５に接続される。二酸化炭素分
離装置１５は気水分離装置１２にも接続され、さらに（
アノードリサイクルブロワ以下単に）ブロワ２０．熱交
換器１１を経由しアノード２人口部へ接続される。A coal supply device 5 and an oxygen production device 7 are connected to an oxygen oxidation coal gasifier (hereinafter referred to as a coal gasifier) 4. The oxygen production device 7 is connected to the carbon dioxide separation device 15 by a refrigerant supply pipe 18 and a refrigerant return pipe 19. The carbon dioxide separator 15 is also connected to the steam/water separator 12, and further (
Anode recycle blower (simply referred to as anode recycle blower) Blower 20. It is connected to the anode 2 via a heat exchanger 11.
一方、燃料電池１のカソード３へは空気圧縮機２５から
の配管が接続され、カソード出口からは膨張タービン２
６へ配管が結ばれる。カソード３の出入口はカソードリ
サイクルブロワ２２（以下ブロワ２２）を経由し、リサ
イクル配管が設けられており、ブロワ２２人口へは、二
酸化炭素分離装置１５からの配管が接続されている。On the other hand, a pipe from an air compressor 25 is connected to the cathode 3 of the fuel cell 1, and an expansion turbine 2 is connected to the cathode outlet.
Piping is connected to 6. The inlet/outlet of the cathode 3 is provided with recycling piping via a cathode recycling blower 22 (hereinafter referred to as blower 22), and piping from the carbon dioxide separator 15 is connected to the blower 22.
石炭ガス化炉４では、石炭供給装置５より石炭が供給さ
れる。一方、酸素製造装置７では空気６を圧縮し、冷却
し、断熱膨張させる過程を繰り返すことにより低温化し
、空気の主成分である窒素の液化温度−１９６℃と酸素
の液化温度−１８３℃の差を利用し、窒素と酸素を分離
する分離された酸素、窒素、あるいはその両方は。Coal is supplied to the coal gasifier 4 from a coal supply device 5 . On the other hand, in the oxygen production device 7, the air 6 is compressed, cooled, and adiabatically expanded by repeating the process to lower the temperature, and the difference between the liquefaction temperature of nitrogen, which is the main component of air, -196°C and the liquefaction temperature of oxygen -183°C. Separate oxygen, nitrogen, or both to separate nitrogen and oxygen.
冷媒供給管１８を通って二酸化炭素分離装置１５へ供給
される。二酸化炭素分離装置１５から出た酸素、窒素、
またはその両方は、冷媒戻り管１９により酸素製造装置
に戻る。酸素製造装置７で分離された酸素８は、石炭ガ
ス化炉へ供給され石炭をガス化する。石炭ガス化燃料は
ガス化炉４を出て、熱回収ボイラ９に入り顕熱を回収さ
れた後に燃料精製装置１０に入り、硫黄化物等が除去さ
れ、燃料電池１が許容する燃料性状となり、燃料電池ア
ノード２に供給される。電池内では燃料の主成分である
一酸化炭素、水素等の燃料成分と、カソード３に供給さ
れた酸素および二酸化炭素が電気化学反応を生じる。こ
れらの反応はミクロ的には種々の反応過程を経由するが
、マクロ的には、アノードでは一酸化炭素および水素が
消費され、反応生成物として、二酸化炭素および水が生
じる。The refrigerant is supplied to the carbon dioxide separator 15 through the refrigerant supply pipe 18 . Oxygen and nitrogen released from the carbon dioxide separator 15,
or both return to the oxygen production device via the refrigerant return pipe 19. Oxygen 8 separated in the oxygen production device 7 is supplied to a coal gasifier to gasify coal. The coal gasified fuel leaves the gasification furnace 4, enters the heat recovery boiler 9, recovers sensible heat, and then enters the fuel purification device 10, where sulfides and the like are removed, and the fuel properties become acceptable for the fuel cell 1. It is supplied to the fuel cell anode 2. Inside the cell, an electrochemical reaction occurs between fuel components such as carbon monoxide and hydrogen, which are the main components of the fuel, and oxygen and carbon dioxide supplied to the cathode 3. Microscopically, these reactions go through various reaction processes, but macroscopically, carbon monoxide and hydrogen are consumed at the anode, and carbon dioxide and water are produced as reaction products.
一方、カソードでは、酸素および二酸化炭素が消費され
る。Meanwhile, at the cathode, oxygen and carbon dioxide are consumed.
燃料電池における反応は電気化学反応であるため、化学
反応に関係する成分の分圧が電池性能に影響する。燃流
電池１のアノードでは反応生成物である二酸化炭素、お
よび、水の分圧は低く、−酸化炭素、および、水素の分
圧は高いことが望ましく、カソードでは酸素および二酸
化炭素の分圧が高いことが望まれる。Since reactions in fuel cells are electrochemical reactions, the partial pressures of components involved in the chemical reactions affect cell performance. At the anode of the fuel flow cell 1, it is desirable that the partial pressures of carbon dioxide and water, which are reaction products, are low, and that the partial pressures of carbon oxide and hydrogen are high, and at the cathode, the partial pressures of oxygen and carbon dioxide are low. A high value is desired.
本実施例では、アノードにおける燃料利用率を従来の利
用率より低くし、アノードにおける平均水素分圧を高く
する。アノード２を出た反応生成物である水、二酸化炭
素および未利用の燃料を成分とするアノード排ガスは、
熱交換器１１に入り、顕熱を与え低温となり気水分装置
１２に入り、さらに低温とされ水分を分離する。In this embodiment, the fuel utilization rate at the anode is lower than the conventional utilization rate, and the average hydrogen partial pressure at the anode is increased. The anode exhaust gas containing water, carbon dioxide, and unused fuel as reaction products leaving the anode 2 is
It enters a heat exchanger 11, gives sensible heat, becomes low temperature, enters a steam/moisture device 12, is further reduced to a low temperature, and separates moisture.
分離された水分１４は系外に排出される０図示はしてい
ないが、この水分は処理後能の水分と共に系内、例えば
、炭素析出防止用としてアノード入口部に供給される等
利用されても良い。The separated moisture 14 is discharged outside the system.Although not shown in the figure, this moisture is used in the system together with the residual moisture after treatment, for example, by being supplied to the anode inlet to prevent carbon precipitation. Also good.
水分を分離したアノード排ガス１３は二酸化炭素分離装
置１５に供給され、酸素製造装置７よりの冷熱を用いて
二酸化炭素の凝固点−７８，５℃以下に冷却され二酸化
炭素を分離する。The anode exhaust gas 13 from which water has been separated is supplied to the carbon dioxide separator 15, where it is cooled to below the freezing point of carbon dioxide by -78.5° C. using cold heat from the oxygen production device 7, and carbon dioxide is separated.
二酸化炭素を分離したアノード排ガスは、電気化学反応
に有効な、−酸化炭素、水素が主成分となり、モータ２
１で駆動されるブロワ２０によりるブロワ２２人口へ供
給される。この二酸化炭素の温度を制御すればブロワ２
２の動力減少およびカソード冷却にも利用できる。カソ
ード３へは、空気圧縮機２５を用いて空気２４が供給さ
れ、ブロワ２２より供給された二酸化炭素もカソードへ
供給される。カソード３を出た高温のカソード排ガスは
膨張タービン２６へ供給され、空気圧縮機２５および発
電機２７を駆動する。The anode exhaust gas from which carbon dioxide has been separated contains -carbon oxide and hydrogen, which are effective for electrochemical reactions, as its main components.
A blower 22 is supplied with a blower 20 driven by a blower 1. If the temperature of this carbon dioxide is controlled, blower 2
It can also be used for power reduction and cathode cooling. Air 24 is supplied to the cathode 3 using an air compressor 25, and carbon dioxide supplied from a blower 22 is also supplied to the cathode. The high temperature cathode exhaust gas leaving the cathode 3 is supplied to an expansion turbine 26 and drives an air compressor 25 and a generator 27.
本実施例によれば、アノードにおける燃料利用率を高く
することなく供給された燃料を全て電気化学反応に利用
できるので電池性能を高める効果がある。According to this embodiment, all of the supplied fuel can be used for the electrochemical reaction without increasing the fuel utilization rate at the anode, which has the effect of improving cell performance.
本発明の他の実施例では、第１図に示す実施例に加えて
、酸素製造装置７より酸素を電池カソード３に導入する
ことである。これによりカソードにおける酸素分圧はさ
らに高くなり、電池性能は高くなる効果がある。In another embodiment of the invention, in addition to the embodiment shown in FIG. 1, oxygen is introduced into the battery cathode 3 from an oxygen production device 7. This has the effect of further increasing the oxygen partial pressure at the cathode and improving battery performance.
本発明のさらに他の実施例では、第１図に示す、実施例
に加えて、酸素製造装置７で分離された窒素をアノード
２．カソード３またはその両方に導入し、成分の分圧を
変化させ部分負荷性能を制御する６本実施例によれば、
アノード、カソードまたはその両方の流量の変化を少な
くして部分負荷を達成できる効果がある。In yet another embodiment of the present invention, in addition to the embodiment shown in FIG. According to this embodiment, the component is introduced into the cathode 3 or both to change the partial pressure of the component and control the part load performance.
The effect is that partial loading can be achieved by reducing changes in the flow rates of the anode, cathode, or both.
本発明の他の実施例を第２図に示す。Another embodiment of the invention is shown in FIG.
第１図の実施例と異なる点は、アノード２出口の熱交換
器１１を排し、排ガスタービン２９をアノード２．気水
分離器１２間に設け、ブロワ２０に代えて圧縮機２８を
設けた点である。The difference from the embodiment shown in FIG. 1 is that the heat exchanger 11 at the outlet of the anode 2 is removed, and the exhaust gas turbine 29 is connected to the anode 2. The difference is that a compressor 28 is provided between the steam and water separators 12 in place of the blower 20.
アノード２を出た高温高圧のアノード排ガスは、排ガス
タービン２９に入り膨張し低温、低圧となり気水分離器
１２に入る。二酸化炭素分離器１５では二酸化炭素の分
離を低圧で行う、二酸化炭素を分離したアノード排ガス
１６は、圧縮機２８で昇圧され、アノード２の入口へリ
サイクルされる。The high-temperature, high-pressure anode exhaust gas leaving the anode 2 enters the exhaust gas turbine 29, expands, becomes low temperature and low pressure, and enters the steam/water separator 12. The carbon dioxide separator 15 separates carbon dioxide at low pressure. The anode exhaust gas 16 from which carbon dioxide has been separated is pressurized by the compressor 28 and recycled to the inlet of the anode 2.
排ガスタービン２９を流れるガスは、水および二酸化炭
素を分離する前の高温ガスであり、圧縮機２８を流れる
ガスは、水および二酸化炭素が分離された低温ガスであ
るので、排ガスタービン２９で発生した動力は圧縮機２
８および電動発電機３０を駆動する。電動発電機３ｏは
部分負荷時等を考慮して１発電機のみならず電動機とし
て動作することが望ましい。また、実施例では、二酸化
炭素分離装置１５内で分離され二酸化炭素が昇圧される
ことを設定しているが、低温低圧の二酸化炭素が、空気
圧縮機２５の入口へ空気２４と混合して供給されても良
い。The gas flowing through the exhaust gas turbine 29 is high-temperature gas before water and carbon dioxide have been separated, and the gas flowing through the compressor 28 is low-temperature gas from which water and carbon dioxide have been separated. Power is compressor 2
8 and a motor generator 30. It is desirable that the motor-generator 3o operates not only as a generator but also as a motor in consideration of partial load and the like. Furthermore, in the embodiment, carbon dioxide is separated and pressurized in the carbon dioxide separator 15, but low-temperature, low-pressure carbon dioxide is supplied to the inlet of the air compressor 25 mixed with the air 24. It's okay to be.
本実施例によれば、二酸化炭素の分離が低圧で行える効
果がある。According to this embodiment, there is an effect that carbon dioxide can be separated at low pressure.
本発明によれば、アノード出口排ガスより二酸化炭素を
分離することができるので１石炭ガス化燃料を有効に電
気化学反応に利用できる。According to the present invention, since carbon dioxide can be separated from the exhaust gas at the anode outlet, one coal gasified fuel can be effectively used for electrochemical reactions.
第１図および第２図は本発明の一実施例の系統図である
。
１・・・溶融炭酸塩型燃料電池、１５・・・二酸化炭素
分離装置、７・・・酸素製造装置、４・・・酸素酸化石
炭ガス化炉。1 and 2 are system diagrams of one embodiment of the present invention. DESCRIPTION OF SYMBOLS 1... Molten carbonate fuel cell, 15... Carbon dioxide separation device, 7... Oxygen production device, 4... Oxygen oxidation coal gasifier.
Claims (1)
素を供給する酸素製造プラント、前記石炭ガス化炉によ
りガス化された燃料ガスを供給される溶融炭酸塩型燃料
電池を含む燃流電池発電プラントにおいて、 前記燃料電池のアノード出口ガスから前記酸素製造プラ
ントで生じる冷熱を利用し、二酸化炭素を分離すること
を特徴とする燃料電池発電方法。[Claims] 1. A coal gasifier, an oxygen production plant that supplies oxygen as an oxidizing agent to the coal gasifier, and a molten carbonate type to which fuel gas gasified by the coal gasifier is supplied. A fuel cell power generation method comprising, in a fuel cell power generation plant including a fuel cell, comprising: separating carbon dioxide from the anode outlet gas of the fuel cell by using cold heat generated in the oxygen production plant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62003168A JPS63174282A (en) | 1987-01-12 | 1987-01-12 | Fuel cell generation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62003168A JPS63174282A (en) | 1987-01-12 | 1987-01-12 | Fuel cell generation process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63174282A true JPS63174282A (en) | 1988-07-18 |
Family
ID=11549842
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62003168A Pending JPS63174282A (en) | 1987-01-12 | 1987-01-12 | Fuel cell generation process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63174282A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03106418A (en) * | 1989-09-19 | 1991-05-07 | Toshio Miyauchi | Co2 recovering process in combustion gas and device therefor |
| WO2008096623A1 (en) * | 2007-02-07 | 2008-08-14 | Central Research Institute Of Electric Power Industry | Power generating installation |
| JP2013191572A (en) * | 2008-11-18 | 2013-09-26 | Tokyo Gas Co Ltd | Mcfc power generation system and operation method thereof |
-
1987
- 1987-01-12 JP JP62003168A patent/JPS63174282A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03106418A (en) * | 1989-09-19 | 1991-05-07 | Toshio Miyauchi | Co2 recovering process in combustion gas and device therefor |
| WO2008096623A1 (en) * | 2007-02-07 | 2008-08-14 | Central Research Institute Of Electric Power Industry | Power generating installation |
| JPWO2008096623A1 (en) * | 2007-02-07 | 2010-05-20 | 財団法人電力中央研究所 | Power generation equipment |
| US8110310B2 (en) | 2007-02-07 | 2012-02-07 | Central Research Institute Of Electric Power Industry | Power generating plant |
| JP2013191572A (en) * | 2008-11-18 | 2013-09-26 | Tokyo Gas Co Ltd | Mcfc power generation system and operation method thereof |
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