JPS62274561A - Molten carbonate fuel cell - Google Patents
Molten carbonate fuel cellInfo
- Publication number
- JPS62274561A JPS62274561A JP61118068A JP11806886A JPS62274561A JP S62274561 A JPS62274561 A JP S62274561A JP 61118068 A JP61118068 A JP 61118068A JP 11806886 A JP11806886 A JP 11806886A JP S62274561 A JPS62274561 A JP S62274561A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- cathode
- carbon dioxide
- anode
- 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 55
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 title claims abstract description 37
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 85
- 239000007789 gas Substances 0.000 claims abstract description 68
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 44
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 39
- 238000001179 sorption measurement Methods 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims description 8
- 239000002737 fuel gas Substances 0.000 claims description 2
- 239000012495 reaction gas Substances 0.000 abstract description 19
- 238000004064 recycling Methods 0.000 abstract 3
- 239000000203 mixture Substances 0.000 abstract 1
- 239000003463 adsorbent Substances 0.000 description 7
- 239000003792 electrolyte Substances 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 239000002250 absorbent Substances 0.000 description 5
- 230000002745 absorbent Effects 0.000 description 5
- 239000006096 absorbing agent Substances 0.000 description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 229910021536 Zeolite Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 239000010457 zeolite Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- BKHJHGONWLDYCV-UHFFFAOYSA-N [C]=O.[C] Chemical compound [C]=O.[C] BKHJHGONWLDYCV-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
-
- 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
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04097—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with recycling of the reactants
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Energy (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Fuel Cell (AREA)
Abstract
Description
【発明の詳細な説明】
３、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に関し、特にカソードへ
の二酸化炭素の供給系の改良に係る。DETAILED DESCRIPTION OF THE INVENTION 3. Detailed Description of the Invention [Field of Industrial Application] The present invention relates to a molten carbonate fuel cell, and particularly relates to an improvement in a carbon dioxide supply system to a cathode.
溶融炭酸塩型燃料電池の単電池は空気極（カソード）と
だδ斜陽（アノード）との間に電解質（溶融炭酸塩）を
介在させて構成されている。そして、下記（Ｉ＞式に示
すように空気極へは空気と二酸化炭素とが供給され、外
部回路から電子を受取って炭酸イオンとなる。また、下
記（ＩＩ）式又は（ＤＩ）式に示すように燃料極３へは
水素や一酸化炭素が供給され、電解質中を移動してきた
炭酸イオンと反応して二酸化炭素や水を生成するととも
に電子を外部回路へ放出する。A unit cell of a molten carbonate fuel cell is constructed by interposing an electrolyte (molten carbonate) between an air electrode (cathode) and an anode. Then, air and carbon dioxide are supplied to the air electrode as shown in the following formula (I>), and they receive electrons from the external circuit and become carbonate ions. Also, as shown in the following formula (II) or (DI) Hydrogen and carbon monoxide are supplied to the fuel electrode 3, which reacts with carbonate ions that have moved through the electrolyte to generate carbon dioxide and water and release electrons to an external circuit.
１／λ
Ｃ０２＋’Ｖ−ｔ’０２＋２ｅ−ＩＣ○３２−−・−（
Ｉ）Ｈ２＋ＣＯ３２−−＋Ｈ２０＋ＣＯ２−１−２８（
Ｉ［＞ＧＯ＋ＣＯ３２−→２ＣＯ２＋２ｅ −（Ｉ
ＩＩ）上述したように、溶融炭酸塩型燃料電池では、電
解質中を移動するイオン種が炭酸イオン（ＣＯ３２−）
であるため、カソード反応ガスとして二酸化炭素が必要
である。カソード反応ガス中のＣ○２ガス濃度は、電池
本体を製作するメーカーによってそれぞれ異なり、５〜
５０％の範囲にある。そして、カソードへのＣＯ２ガス
の供給システムも種々提案されている。こうしたＣＯ２
ガスの供給システムが異なる従来の溶融炭酸塩型燃料電
池を第４図〜第６図を参照して説明する。なお、第５図
及び第６図において第４図と同一の機器には同一番号を
付して説明する。1/λ C02+'V-t'02+2e-IC○32--・-(
I) H2+CO32--+H20+CO2-1-28(
I[>GO+CO32−→2CO2+2e −(I
II) As mentioned above, in molten carbonate fuel cells, the ionic species moving in the electrolyte is carbonate ion (CO32-).
Therefore, carbon dioxide is required as the cathode reaction gas. The C○2 gas concentration in the cathode reaction gas varies depending on the manufacturer of the battery body, and varies from 5 to
It is in the range of 50%. Various CO2 gas supply systems to the cathode have also been proposed. These CO2
Conventional molten carbonate fuel cells with different gas supply systems will be described with reference to FIGS. 4 to 6. Note that in FIGS. 5 and 6, the same equipment as in FIG. 4 is given the same number and will be explained.
第４図〜第６図において、燃Ｆ４′Ｒ池本体１の単電池
は燃料極（アノード）２と空気極（カソード）３との間
に電解質（溶融炭酸塩）４を介在させて構成されている
。4 to 6, the unit cell of the fuel F4'R battery body 1 is constructed by interposing an electrolyte (molten carbonate) 4 between a fuel electrode (anode) 2 and an air electrode (cathode) 3. ing.
第４図の溶融炭酸塩−型燃料電池では、燃料極２及び空
気極３への反応ガス供給系統はそれぞれ以下のようなも
のである。燃料Ｉ！ｉ２へは、■燃料予熱器５を通過し
た改質ガスａ、及び■アノードガス再循環ブロワ６によ
って循環されるアノード排出ガスｂ（二酸化炭素及び未
反応の一酸化炭素や水素を含む）の一部、が混合されて
アノード反応ガスＣとして供給される。そして、アノー
ド排出ガスｂの一部は燃焼器又は触媒燃焼器７へ送られ
る。一方１．空気極３へは、■空気圧縮機８と空気予熱
器９とを順次通過した空気ｄと、燃焼器又は触媒燃焼器
７内でのアノード排出ガスｂの一部の燃焼により生成し
た二酸化炭素との混合ガス、及び■熱交換器１０を通過
し、カソードガス再循環ブロワ１１によって循環される
カソード排出ガスｅの一部、が混合されてカソード反応
ガスｆとして供給される。In the molten carbonate fuel cell shown in FIG. 4, the reaction gas supply systems to the fuel electrode 2 and air electrode 3 are as follows. Fuel I! The reformed gas a that has passed through the fuel preheater 5 and the anode exhaust gas b (including carbon dioxide and unreacted carbon monoxide and hydrogen) that is circulated by the anode gas recirculation blower 6 are sent to i2. , are mixed and supplied as the anode reaction gas C. A part of the anode exhaust gas b is then sent to the combustor or catalytic combustor 7. On the other hand 1. To the air electrode 3 are air d that has passed through the air compressor 8 and air preheater 9 in sequence, and carbon dioxide generated by combustion of a part of the anode exhaust gas b in the combustor or catalytic combustor 7. and (1) a portion of the cathode exhaust gas e which passes through the heat exchanger 10 and is circulated by the cathode gas recirculation blower 11 are mixed and supplied as the cathode reaction gas f.
これらの反応ガスの供給により上述した（Ｉ）〜（［）
の反応が起り直流電流が発生する。また、カソード排出
ガスｅの一部は膨張タービン１２へ送られ、その後大気
中に放出される。この膨張タービン１２の出力の一部は
空気圧縮機８の動力として使用され、その出力の残りの
一部は発電機１３の動力として使用される。By supplying these reaction gases, the above-mentioned (I) to ([)
The reaction occurs and direct current is generated. Further, a portion of the cathode exhaust gas e is sent to the expansion turbine 12 and then released into the atmosphere. A part of the output of the expansion turbine 12 is used as power for the air compressor 8, and the remaining part of the output is used as power for the generator 13.
第５図の溶融炭酸塩型撚ｎ電池では、燃料極２及び空気
極３への反応ガス供給系統はそれぞれ以下のようなもの
である。燃料極２へは、■原料ガスｑ、■７ノードガス
再ｍｌブロワ６によって循環されるアノード排出ガスｂ
、及び■空気圧ｔｌＢＲ料予熱器５を通過して７ノ一ド
反応ガスＣとして供給される。一方、空気極３へは、■
空気圧縮機８と空気予熱器９とを順次通過した空気ｄの
一部、■熱交換器１０を通過し、カソードガス再循環７
部、が混合されてカソード反応ガスｆとして供給される
。In the molten carbonate type twisted n cell shown in FIG. 5, the reaction gas supply systems to the fuel electrode 2 and the air electrode 3 are as follows. To the fuel electrode 2, ■ raw material gas q, ■ 7 node gas re-ml, anode exhaust gas b circulated by the blower 6.
, and (2) passes through a pneumatic tlBR material preheater 5 and is supplied as a 7-node reaction gas C. On the other hand, to air electrode 3, ■
A part of the air d that has sequentially passed through the air compressor 8 and the air preheater 9, ■ Passes through the heat exchanger 10 and is recirculated to the cathode gas 7
, are mixed and supplied as cathode reaction gas f.
第６図の溶融炭酸塩型燃料電池では、燃料極２及び空気
極３への反応ガス供給系統はそれぞれ以下のようなもの
である。燃料極２へは、■燃料予熱器５を通過した改質
ガスａ１及び■アノード排出ガスｂが熱交換器１５と吸
収器１６とを順次通過して二酸化炭素が除去された成分
からなり、アノードガス再循環ブロワ６によって循環さ
れるアノードリサイクルガスｈ、が混合されてアノード
反応ガスＣとして供給される。そして、吸収器１６内で
二酸化炭素を吸収した吸収剤ｑは再生器１７へ移送され
る。一方、空気極３へは、■空気圧縮機８と空気予熱器
９とを順次通過した空気ｄと、この空気が再生器１７内
で吸収剤と接触することにより放出された二酸化炭素と
からなり、熱交換器１８を通過した混合ガス、及び■熱
交換器１ｏを通過し、カソードガス再循環ブロワ１１に
よって循環されるカソード排出ガスｅの一部、が混合さ
れてカソード反応ガスｆとして供給される。In the molten carbonate fuel cell shown in FIG. 6, the reaction gas supply systems to the fuel electrode 2 and air electrode 3 are as follows. The reformed gas a1 that has passed through the fuel preheater 5 and the anode exhaust gas b that have passed through the heat exchanger 15 and the absorber 16 in order to remove carbon dioxide are sent to the fuel electrode 2. The anode recycle gas h, which is circulated by the gas recirculation blower 6, is mixed and supplied as the anode reaction gas C. Then, the absorbent q that has absorbed carbon dioxide in the absorber 16 is transferred to the regenerator 17. On the other hand, the air to the air electrode 3 consists of (1) air d that has passed through the air compressor 8 and air preheater 9 in sequence, and carbon dioxide released when this air comes into contact with the absorbent in the regenerator 17. , the mixed gas that has passed through the heat exchanger 18, and (1) a part of the cathode exhaust gas e that has passed through the heat exchanger 1o and is circulated by the cathode gas recirculation blower 11, and is mixed and supplied as a cathode reaction gas f. Ru.
そして、再生器１７内で二酸化炭素を放出して再生した
吸収剤ｒは吸収器１６へ移送される。Then, the absorbent r regenerated by releasing carbon dioxide in the regenerator 17 is transferred to the absorber 16.
なお、第５図及び第６因のＷＪ融炭酸塩型燃料電池でも
、燃料電池本体１における直流電流の発生及び膨張ター
ビン１２の出力が空気圧縮機８と発ｉｆ！１１３の動力
として使用されることは、第４図の溶融炭酸塩型燃料電
池の場合と同様である。Note that even in the WJ molten carbonate fuel cell shown in FIG. 113 is used as the power source in the same manner as in the case of the molten carbonate fuel cell shown in FIG.
しかしながら、第４図及び第５図図示の溶融炭酸塩型燃
料電池には以下のような問題がある。すなわち、これら
の溶融炭酸塩型燃料電池では、燃焼器又は触媒燃焼器７
や改質器１４における一酸化炭素（及び／又は炭素）の
酸化により、カソード反応ガスとなる二酸化炭素を得て
おり、−酸化炭素（炭素）の有する燃焼熱を発電に利用
することができないため、全体的にはプラント効率が低
下する。また、燃焼器又は触媒燃焼器７や改質器１４に
よって二酸化炭素を供給する場合には、カソードでの二
酸化炭素の要求量の変化に追従することが困難であり、
安定した運転を可能にするためには複雑な制御システム
が必要となる。However, the molten carbonate fuel cells shown in FIGS. 4 and 5 have the following problems. That is, in these molten carbonate fuel cells, the combustor or catalytic combustor 7
Carbon monoxide (and/or carbon) is oxidized in the reformer 14 to obtain carbon dioxide, which becomes the cathode reaction gas, and the combustion heat of the carbon oxide (carbon) cannot be used for power generation. , overall plant efficiency decreases. Furthermore, when carbon dioxide is supplied by the combustor or catalytic combustor 7 or the reformer 14, it is difficult to follow changes in the amount of carbon dioxide required at the cathode.
A complex control system is required to enable stable operation.
一方、第６図の溶融炭酸塩型撚Ｆｔ電池では、吸収器１
６及び再生器１７を使用してアノード排出ガス中の二酸
化炭素のみをカソードへ供給しており、第４図及び第５
図図示の溶融炭酸塩型燃料電池と異なり一酸化炭素（炭
素）を有効に利用することができるので、−見合理的に
みえる。しかし、この溶融炭酸塩型燃料電池では、吸収
器１６と再生器１７との間で吸収剤を移送しなければな
らないため、かなり複雑なシステムになることは明らか
である。また、吸収剤の移動のためにエネルギーを要す
るので、やはりプラント効率の低下をＩＲく。On the other hand, in the molten carbonate type twisted Ft battery shown in Fig. 6, the absorber 1
6 and regenerator 17 are used to supply only carbon dioxide in the anode exhaust gas to the cathode, as shown in Figs. 4 and 5.
Unlike the molten carbonate fuel cell shown in the figure, carbon monoxide (carbon) can be used effectively, so it looks reasonable. However, it is clear that this molten carbonate fuel cell results in a rather complex system since the absorbent must be transferred between the absorber 16 and the regenerator 17. Furthermore, since energy is required to move the absorbent, it also reduces plant efficiency.
本発明は上記問題点を解決するためになされたものであ
り、プラント効率が高く、！ｌ制御の容易な溶融炭酸塩
型燃料電池を提供することを目的とする。The present invention was made to solve the above problems, and has high plant efficiency! An object of the present invention is to provide a molten carbonate fuel cell that is easy to control.
本発明の溶融炭酸塩型燃料電池は、溶融炭酸塩型燃料電
池本体と、該燃料電池のアノードへ燃料ガスを供給する
系統と、前記燃料電池のカソードへ空気及びアノード出
口ガスに含まれる二Ｍ化炭素を供給する系統とを有する
溶融炭酸塩型燃料電池において、前記アノード出口ガス
中の二酸化炭素を分離してこの二酸化炭素をカソードへ
供給する圧力スイング吸着式ガス分ＩＩ装置を設けたこ
とを特徴とするものである。The molten carbonate fuel cell of the present invention includes a molten carbonate fuel cell main body, a system for supplying fuel gas to the anode of the fuel cell, air to the cathode of the fuel cell, and 2 M contained in the anode outlet gas. In a molten carbonate fuel cell having a system for supplying carbon dioxide, a pressure swing adsorption type gas fraction II device is provided which separates carbon dioxide from the anode outlet gas and supplies this carbon dioxide to the cathode. This is a characteristic feature.
本発明において用いられる圧力スイング吸着式％式％
式と記す）ガス分ｌｉＩ！ｌ装置は、ゼオライト等の吸
着剤が充填された吸着塔を有し、その内部ヘアノード排
出ガスを導入して高圧下で二酸化炭素のみを吸着した後
、圧力を低下させて二酸化炭素を脱着させ、この二酸化
炭素をカソードへ供給するものである。Pressure swing adsorption formula used in the present invention (denoted as % formula) gas content liI! The device has an adsorption tower filled with an adsorbent such as zeolite, introduces the internal hair node exhaust gas, adsorbs only carbon dioxide under high pressure, and then reduces the pressure to desorb carbon dioxide. This carbon dioxide is supplied to the cathode.
したがって、本発明の溶融炭酸塩型燃料電池によれば、
アノード排出ガス中の二酸化炭素のみをカソードへ供給
し、−酸化炭素（炭素）を有効に利用することができる
ので、プラント効率を向上することができる。また、吸
着塔を複数基設ければ二酸化炭素の吸着・脱着のサイク
ルを繰返すことにより連続運転が可能となり、その操作
はバルブの切換え操作だけでよいので制御が容易である
。Therefore, according to the molten carbonate fuel cell of the present invention,
Since only carbon dioxide in the anode exhaust gas can be supplied to the cathode and carbon oxide (carbon) can be effectively used, plant efficiency can be improved. In addition, if a plurality of adsorption towers are provided, continuous operation is possible by repeating the cycle of adsorption and desorption of carbon dioxide, and the operation is easy because only switching of valves is required.
更に、吸着剤であるゼオライト等は熱に強く、高温運転
が可能であり、熱交換器等が不要となるので、熱損失を
低減することができる。Furthermore, the adsorbent, such as zeolite, is resistant to heat and can be operated at high temperatures, eliminating the need for a heat exchanger or the like, thereby reducing heat loss.
以下、本発明の実施例を第１図及び第２図を参照して説
明する。Embodiments of the present invention will be described below with reference to FIGS. 1 and 2.
第１図において、燃料電池本体２１の単電池は燃料極（
アノード）２２と空気極（カソード）２３との間に電解
質（溶融炭酸塩）２４を介在させて構成されている。In FIG. 1, the single cell of the fuel cell main body 21 has a fuel electrode (
An electrolyte (molten carbonate) 24 is interposed between an anode (anode) 22 and an air electrode (cathode) 23.
前記燃料極２２及び空気極２３への反応ガス供給系統は
それぞれ以下のようなものである。燃料極２２へは、■
燃料予熱器２５を通過した改質ガスａ、及び■アノード
排出ガスｂに１化炭素及び未反応の一酸化炭素や水素を
含む）がＰＳＡ式ガス分離Ｓ！８２６を通過して二酸化
炭素が除去された成分からなり、アノードガス再循環ブ
ロワ２７によって循環されるアノードリサイクルガスｈ
、が混合されてアノード反応ガスＣとして供給される。Reaction gas supply systems to the fuel electrode 22 and air electrode 23 are as follows. To the fuel electrode 22, ■
The reformed gas a that has passed through the fuel preheater 25 and (contains carbon monide and unreacted carbon monoxide and hydrogen in the anode exhaust gas b) are separated by PSA type gas separation S! Anode recycle gas h consisting of a component from which carbon dioxide has been removed by passing through 826 and circulated by an anode gas recirculation blower 27
, are mixed and supplied as the anode reaction gas C.
一方、空気極２３へは、■空気圧縮擺２８と空気予熱器
２９とを順次通過した空気ｄ、■ＰＳＡ式ガス分Ｗｉ＠
置２装から脱着された二酸化炭素、及び■熱交換器３０
を通過し、カソードガス再循環ブロワ３１によって循環
されるカソード排出ガスｅの一部、が混合器３２で混合
されてＣ０２１度５〜５０％に成分調整され、カソード
反応ガスｆとして供給される。On the other hand, to the air electrode 23 are: ■ Air d that has passed through the air compressor 28 and the air preheater 29 in sequence, ■ PSA type gas Wi @
Carbon dioxide desorbed from the equipment 2 and the heat exchanger 30
A part of the cathode exhaust gas e that passes through the cathode gas recirculation blower 31 and is circulated by the cathode gas recirculation blower 31 is mixed in the mixer 32 and adjusted to have a C021 degree of 5 to 50%, and is supplied as the cathode reaction gas f.
これらの反応ガスの供給により溶融用ｉ！［！ｉ塩型燃
料電池本体２１で直流電流が発生する。また、カソード
排出ガスｅの一部は膨張タービン３３へ送られ、その後
大気中に放出される。この膨張タービン３３の出力の一
部は空気圧縮機２８の動力として使用され、その出力の
残りの一部は発電機３４の動力として使用される。By supplying these reaction gases, melting i! [! Direct current is generated in the i-salt fuel cell main body 21. Further, a part of the cathode exhaust gas e is sent to the expansion turbine 33 and then released into the atmosphere. A portion of the output of the expansion turbine 33 is used as power for the air compressor 28 , and the remaining portion of the output is used as power for the generator 34 .
前記ＰＳＡ式ガス分離装置３２は、例えば第２図に示す
ように吸着塔が４基併設された構造を有している。第２
図において、アノード排出ガスｂは前処理装置３５で不
純物や水分等が除去された後、入口バルブ３６１．３６
２．３６３．３６４を介して吸着塔３７ｔ 、３７２．
３７３．３７４へ送られる。これら吸着塔３７１．３７
２．３７３．３７４内部にはゼオライト等の吸着剤３８
、・・・が充填されており、高圧下で二酸化炭素のみが
吸着される。吸着剤３８、・・・に吸着されなかった一
酸化炭素や水素等のガスは出口バルブ３９ｉ 、３９２
．３９３．３９４を介してアノードリサイクルガスｈと
して循環され、改質ガスａと混合されてアノード反応ガ
スＣとして燃料極２２へ供給される。また、吸着塔の入
口側には二酸化炭素放出バルブ４０１．４０２．４０３
．４０４が設けられており、図示しない真空ポンプ等に
より達成される低圧下で吸着剤３８、・・・がら脱着し
た二酸化炭素はこれらバルブを介して混合器３２へ送ら
れる。また、吸着塔の出口側には均圧バルブ４１ｓ 、
４１２．４１３．４１４が設けられている。なお、前記
各吸着塔３７１．３７２．３７３．３７４は、二酸化炭
素吸着、塔間均圧、二酸化炭素吸着、塔間均圧の４サイ
クルを順次繰返しており、制御装置４２がらの信号によ
り各吸着塔に付属するバルブの開閉が制御されている。The PSA type gas separation apparatus 32 has a structure in which four adsorption towers are installed, for example, as shown in FIG. Second
In the figure, the anode exhaust gas b is removed from the inlet valve 361.36 after impurities, moisture, etc. are removed by the pretreatment device 35.
2.363.364 to adsorption tower 37t, 372.
Sent to 373.374. These adsorption towers 371.37
2.373.374 Inside is adsorbent 38 such as zeolite.
,... are filled, and only carbon dioxide is adsorbed under high pressure. Gases such as carbon monoxide and hydrogen that are not adsorbed by the adsorbents 38, . . . are discharged through the outlet valves 39i, 392.
．． 393 and 394 as an anode recycle gas h, mixed with the reformed gas a, and supplied to the fuel electrode 22 as an anode reaction gas C. In addition, a carbon dioxide release valve 401, 402, 403 is installed on the inlet side of the adsorption tower.
．． 404 are provided, and the carbon dioxide desorbed from the adsorbent 38 under low pressure achieved by a vacuum pump (not shown) or the like is sent to the mixer 32 via these valves. In addition, a pressure equalizing valve 41s is installed on the outlet side of the adsorption tower.
412.413.414 are provided. Each of the adsorption towers 371, 372, 373, and 374 sequentially repeats four cycles of carbon dioxide adsorption, inter-column pressure equalization, carbon dioxide adsorption, and inter-column pressure equalization, and each adsorption tower is controlled by a signal from the control device 42. The opening and closing of valves attached to the tower are controlled.
また、ＰＳＡ式ガス分離装置は第２図図示のように、吸
着塔を４基設けたものでなくてもよく、吸着塔を２基以
上設ければ連続運転が可能となる。Further, the PSA type gas separation apparatus does not need to be equipped with four adsorption towers as shown in FIG. 2, and can be operated continuously if two or more adsorption towers are installed.
このような溶融炭酸塩型燃料電池によれば、ＰＳＡ式ガ
ス分離装置２６によりアノード排出ガス中の二酸化炭素
のみを分離してカソード反応ガスとして供給しており、
燃焼器等を用いる場合と異なり、−酸化炭素（炭素）を
有効に利用することができるので、プラント効率を向上
することができる。また、吸着塔を複数基併設したＰＳ
Ａ式ガス分離装置２６のバルブの切換え操作によって二
酸化炭素の吸着・脱着のサイクルを繰返して連続運転す
ることができるので、制御性が良好であり、カソードに
おける二酸化炭素の必要量の変化にも追従することがで
きる。更に、ＰＳＡ式ガス分離装置２６の吸着塔に充填
されたゼオライト等の吸着剤は熱に強く、高温運転が可
能であり、熱交換器等が不要となるので、熱損失を低減
することができる。According to such a molten carbonate fuel cell, only carbon dioxide in the anode exhaust gas is separated by the PSA gas separation device 26 and supplied as a cathode reaction gas.
Unlike the case where a combustor or the like is used, -carbon oxide (carbon) can be used effectively, so plant efficiency can be improved. In addition, PS equipped with multiple adsorption towers
The cycle of adsorption and desorption of carbon dioxide can be repeated and operated continuously by switching the valves of the type A gas separation device 26, so it has good controllability and can also follow changes in the amount of carbon dioxide required at the cathode. can do. Furthermore, the adsorbent such as zeolite packed in the adsorption tower of the PSA gas separation device 26 is resistant to heat and can be operated at high temperatures, eliminating the need for a heat exchanger, etc., thereby reducing heat loss. .
なお、本発明の溶融炭酸塩型燃料電池における各機器の
構成は、上記実施例で示したものに限らず、例えば第３
図に示すものでもよい。第３図の溶融炭酸塩型燃料電池
は、第１図図示の構成に加えて、改質ガスａの一部及び
空気ｄの一部を燃焼する燃焼器又は触媒燃焼器４３を設
け、空気及び二酸化炭素の混合ガスを混合器３２へ供給
するようにしたものである。It should be noted that the configuration of each device in the molten carbonate fuel cell of the present invention is not limited to that shown in the above embodiment.
It may be as shown in the figure. In addition to the configuration shown in FIG. 1, the molten carbonate fuel cell shown in FIG. A mixed gas of carbon dioxide is supplied to the mixer 32.
以上詳述した如く本発明によれば、プラント効率が高く
、しかも制ｕ性の良好な溶融炭酸塩型態Ｆｌ電池を提供
できるものである。As described in detail above, according to the present invention, it is possible to provide a molten carbonate type Fl battery with high plant efficiency and good u-control properties.
第１図は本発明の実施例における溶融炭酸塩型燃料電池
の構成図、第２図は同溶融炭酸場型燃料電池に用いられ
るＰＳＡ式ガメガ２分１１装置成図、第３図は本発明の
他の実施例における溶融炭酸塩型燃料電池の構成図、第
４図〜第６図はそれぞれ従来の溶融炭酸塩型燃料電池の
構成図である。
２１・・・溶融炭酸塩型燃料電池本体、２２・・・燃料
極（アノード）、２３・・・空気極（カソード）、２４
・・・電解質、２５・・・燃料予熱器、２６・・・ＰＳ
Ａ式ガス分離装置、２７・・・アノードガス再循環ブロ
ワ、２８・・・空気圧縮器、２９・・・空気予熱器、３
０・・・熱交換器、３１・・・カソードガス再循環ブロ
ワ、３２・・・混合器、３３・・・−張タービン、３４
・・・発電機、３５・・・前処理装置、３６１．３６２
．３６３．３６４・・・入口バルブ、３７１，３７２．
３７３．３７４・・・吸着塔、３８・・・吸着剤、３９
＋ 、３９２．３９３．３９４・・・出口バルブ、４０
ｔ 、４０２．４０３．４０４・・・二酸化炭素吸着バ
ルブ、４１１．４１２．４１３．４１４・・・均圧バル
ブ、４２・・・１ｔｉｌｌＩＩＩ装置、４３・・・燃焼
器又は触媒燃焼器。
第３図 ４３Fig. 1 is a block diagram of a molten carbonate fuel cell according to an embodiment of the present invention, Fig. 2 is a diagram of a PSA type Gamega 2/11 device used in the molten carbonate field fuel cell, and Fig. 3 is a diagram of the invention. FIGS. 4 to 6 are block diagrams of conventional molten carbonate fuel cells, respectively. 21... Molten carbonate fuel cell main body, 22... Fuel electrode (anode), 23... Air electrode (cathode), 24
...Electrolyte, 25...Fuel preheater, 26...PS
Type A gas separation device, 27... Anode gas recirculation blower, 28... Air compressor, 29... Air preheater, 3
0... Heat exchanger, 31... Cathode gas recirculation blower, 32... Mixer, 33... - tension turbine, 34
... Generator, 35 ... Pretreatment device, 361.362
．． 363.364...Inlet valve, 371,372.
373.374...Adsorption tower, 38...Adsorbent, 39
+, 392.393.394...Outlet valve, 40
t, 402.403.404... Carbon dioxide adsorption valve, 411.412.413.414... Pressure equalization valve, 42... 1tillIII device, 43... Combustor or catalytic combustor. Figure 3 43
Claims (1)
燃料ガスを供給する系統と、前記燃料電池のカソードへ
空気及びアノード出口ガスに含まれる二酸化炭素を供給
する系統とを有する溶融炭酸塩型燃料電池において、前
記アノード出口ガス中の二酸化炭素を分離してこの二酸
化炭素をカソードへ供給する圧力スイング吸着式ガス分
離装置を設けたことを特徴とする溶融炭酸塩型燃料電池
。A molten carbonate type fuel cell having a main body, a system for supplying fuel gas to the anode of the fuel cell, and a system for supplying air and carbon dioxide contained in the anode outlet gas to the cathode of the fuel cell. A molten carbonate fuel cell, characterized in that the fuel cell is equipped with a pressure swing adsorption gas separation device that separates carbon dioxide from the anode outlet gas and supplies the carbon dioxide to the cathode.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61118068A JPS62274561A (en) | 1986-05-22 | 1986-05-22 | Molten carbonate fuel cell |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61118068A JPS62274561A (en) | 1986-05-22 | 1986-05-22 | Molten carbonate fuel cell |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS62274561A true JPS62274561A (en) | 1987-11-28 |
Family
ID=14727210
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61118068A Pending JPS62274561A (en) | 1986-05-22 | 1986-05-22 | Molten carbonate fuel cell |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62274561A (en) |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01187775A (en) * | 1988-01-22 | 1989-07-27 | Central Res Inst Of Electric Power Ind | Fuel battery with fusion carbonate |
| WO2002067353A1 (en) * | 2001-02-21 | 2002-08-29 | Ballard Power Systems Inc. | Fuel cell system having a pressure swing adsorption unit |
| WO2004068623A1 (en) * | 2003-01-30 | 2004-08-12 | Nissan Motor Co., Ltd. | Fuel cell system and related method |
| US6846584B2 (en) | 2001-07-12 | 2005-01-25 | Co2 Solution Inc. | Process for generating electricity with a hydrogen fuel cell |
| US6902602B2 (en) | 2002-03-14 | 2005-06-07 | Questair Technologies Inc. | Gas separation by combined pressure swing and displacement purge |
| US6921597B2 (en) | 1998-09-14 | 2005-07-26 | Questair Technologies Inc. | Electrical current generation system |
| US7041272B2 (en) | 2000-10-27 | 2006-05-09 | Questair Technologies Inc. | Systems and processes for providing hydrogen to fuel cells |
| US7087331B2 (en) * | 2000-10-30 | 2006-08-08 | Questair Technologies Inc. | Energy efficient gas separation for fuel cells |
| US7097925B2 (en) * | 2000-10-30 | 2006-08-29 | Questair Technologies Inc. | High temperature fuel cell power plant |
| US7189280B2 (en) | 2004-06-29 | 2007-03-13 | Questair Technologies Inc. | Adsorptive separation of gas streams |
| US7285350B2 (en) | 2002-09-27 | 2007-10-23 | Questair Technologies Inc. | Enhanced solid oxide fuel cell systems |
| US7387849B2 (en) * | 2002-03-14 | 2008-06-17 | Questair Technologies Inc. | Hydrogen recycle for solid oxide fuel cell |
| EP1639665A4 (en) * | 2003-05-15 | 2010-03-03 | Fuelcell Energy Inc | FUEL CELL SYSTEM WITH ANODE EXHAUST GAS RECYCLING |
| WO2010058750A1 (en) * | 2008-11-18 | 2010-05-27 | 東京瓦斯株式会社 | Hydrogen-recycling mcfc power-generating system |
-
1986
- 1986-05-22 JP JP61118068A patent/JPS62274561A/en active Pending
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01187775A (en) * | 1988-01-22 | 1989-07-27 | Central Res Inst Of Electric Power Ind | Fuel battery with fusion carbonate |
| US6921597B2 (en) | 1998-09-14 | 2005-07-26 | Questair Technologies Inc. | Electrical current generation system |
| US7041272B2 (en) | 2000-10-27 | 2006-05-09 | Questair Technologies Inc. | Systems and processes for providing hydrogen to fuel cells |
| US7087331B2 (en) * | 2000-10-30 | 2006-08-08 | Questair Technologies Inc. | Energy efficient gas separation for fuel cells |
| US7097925B2 (en) * | 2000-10-30 | 2006-08-29 | Questair Technologies Inc. | High temperature fuel cell power plant |
| WO2002067353A1 (en) * | 2001-02-21 | 2002-08-29 | Ballard Power Systems Inc. | Fuel cell system having a pressure swing adsorption unit |
| US6846584B2 (en) | 2001-07-12 | 2005-01-25 | Co2 Solution Inc. | Process for generating electricity with a hydrogen fuel cell |
| US6902602B2 (en) | 2002-03-14 | 2005-06-07 | Questair Technologies Inc. | Gas separation by combined pressure swing and displacement purge |
| US7387849B2 (en) * | 2002-03-14 | 2008-06-17 | Questair Technologies Inc. | Hydrogen recycle for solid oxide fuel cell |
| US7285350B2 (en) | 2002-09-27 | 2007-10-23 | Questair Technologies Inc. | Enhanced solid oxide fuel cell systems |
| WO2004068623A1 (en) * | 2003-01-30 | 2004-08-12 | Nissan Motor Co., Ltd. | Fuel cell system and related method |
| CN1324751C (en) * | 2003-01-30 | 2007-07-04 | 日产自动车株式会社 | Fuel cell system and related method |
| EP1639665A4 (en) * | 2003-05-15 | 2010-03-03 | Fuelcell Energy Inc | FUEL CELL SYSTEM WITH ANODE EXHAUST GAS RECYCLING |
| US7189280B2 (en) | 2004-06-29 | 2007-03-13 | Questair Technologies Inc. | Adsorptive separation of gas streams |
| WO2010058750A1 (en) * | 2008-11-18 | 2010-05-27 | 東京瓦斯株式会社 | Hydrogen-recycling mcfc power-generating system |
| JP5282103B2 (en) * | 2008-11-18 | 2013-09-04 | 東京瓦斯株式会社 | Hydrogen recycling type MCFC power generation system |
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