JP2020180592A - 燃料改質装置及び燃料改質方法 - Google Patents
燃料改質装置及び燃料改質方法 Download PDFInfo
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- 239000000446 fuel Substances 0.000 title claims abstract description 141
- 238000002407 reforming Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims description 21
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 344
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 176
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 170
- 239000001257 hydrogen Substances 0.000 claims abstract description 156
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 156
- 238000002485 combustion reaction Methods 0.000 claims abstract description 102
- 239000007789 gas Substances 0.000 claims abstract description 85
- 239000000203 mixture Substances 0.000 claims abstract description 10
- 150000002431 hydrogen Chemical class 0.000 claims description 34
- 238000000354 decomposition reaction Methods 0.000 claims description 23
- 239000003054 catalyst Substances 0.000 claims description 21
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 239000012528 membrane Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 239000002737 fuel gas Substances 0.000 claims description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 238000010248 power generation Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000003502 gasoline Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- NAWXUBYGYWOOIX-SFHVURJKSA-N (2s)-2-[[4-[2-(2,4-diaminoquinazolin-6-yl)ethyl]benzoyl]amino]-4-methylidenepentanedioic acid Chemical compound C1=CC2=NC(N)=NC(N)=C2C=C1CCC1=CC=C(C(=O)N[C@@H](CC(=C)C(O)=O)C(O)=O)C=C1 NAWXUBYGYWOOIX-SFHVURJKSA-N 0.000 description 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
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Abstract
Description
ここで、S0は基準燃料の燃焼速度であり、SHは水素の燃焼速度であり、SAはアンモニアの燃焼速度であり、Cは混合ガスの燃焼速度係数である。さらに本発明の燃料改質装置の制御手段は、式(2)に基づいて混合タンクに供給するアンモニアと水素の体積比を決定している。
ここで、Mは混合ガスに占める水素の体積比であり、A、Bは定数である。
ここで、Hmは混合ガスの高位発熱量であり、HHは水素の高位発熱量であり、HAはアンモニアの高位発熱量であり、H0は基準燃料の高位発熱量であり、Wmは基準燃料に対する混合ガスの重量基準の流量分率である。
ここでmwは混合燃料の分子量であり、W0は燃焼装置から要求された基準燃料の燃料要求速度であり、Fmは、燃焼装置に供給する混合ガスの供給量である。
MH=(100×M−H2L)/(100−H2L)
に基づいて決定する。ここで、H2Lは低濃度タンクのガスの水素濃度(体積%、N2フリー基準)である。ここで、Mは混合ガスに占める水素の体積比である。
ここで、S0は基準燃料の燃焼速度であり、SHは水素の燃焼速度であり、SAはアンモニアの燃焼速度であり、Cは混合ガスの燃焼速度係数である。さらに本発明の燃料改質方法は、式(2)に基づいて混合タンクに供給する水素の体積比を決定しており、
ここで、Mは混合ガスに占める水素の体積比であり、A、Bは定数であり、アンモニアと前記高濃度水素ガスの混合比を、(1−M):Mに制御することを特徴とする。
ここで、S0は基準燃料の燃焼速度(cm/s)であり、SHは水素の燃焼速度であり、SAはアンモニアの燃焼速度である。表1に示した例に従えば、SHは346cm/sであり、水素の燃焼速度であり、SAは8cm/sである。この式を用いて、制御手段10は、混合ガスの燃焼速度係数Cを算出する。
ここで、A、Bは定数であり、最も好適な値は、A=6.0、B=3.5である。
ここで、H2Lは低濃度タンクのガスの水素濃度(体積%、N2フリー基準)である。
ここで、Fm’は燃焼装置に供給する混合ガスの燃料供給速度(NL/h、N2含有基準)である。
ここで、N2Lは低濃度タンクのガスの窒素濃度(体積%)である。
基準燃料がメタンであり、燃料供給速度W0=1.0kg/h、発電量1000Whの燃焼装置の燃料を製造するために本発明の燃料改質装置1を適用した例を示す。
次に、実施例1と同様の、基準燃料がメタンであり、燃料供給速度W0=1.0kg/h、発電量1000Whの燃焼装置の燃料を製造するために本発明の燃料改質装置30を適用した例を示す。本実施例で、アンモニア分解触媒反応器31が製造する低濃度水素ガスの水素濃度H2Lは、7.7体積%である。
燃料改質装置30をメタンガスエンジンの燃料の製造に適用した例を示す。制御手段10は、アンモニア分解触媒反応器31の温度を250℃に設定し、アンモニア分解率10%の低濃度水素混合ガスを製造して低濃度水素タンク32に貯蔵した。生成した低濃度水素混合ガスの組成は、水素7.5%、アンモニア90%、窒素2.5%である。次に、改質器5で、含有率99%の水素ガスを生成し、高濃度水素タンク6に貯留した。そして、混合タンク7で、低濃度水素ガス73.8%、高濃度水素ガス26.2%を混合し、貯蔵した。この混合燃料の最大燃焼速度は43cm/sでありメタンの最大燃焼速度と一致していた。また、この混合燃料の高位発熱量は61MJ/kgであり、メタンの高位発熱量55.5MJ/kgより大きいため、混合燃料のメタンガスエンジンへの流量を0.92倍にするようにバルブ23の流量を制御した。これにより、燃焼装置2の良好な燃焼を得ることができた。
2 燃焼装置
3 負荷
4 アンモニアタンク
5 改質器
6 高濃度水素タンク
7 混合タンク
8 空気ブロア
10 制御手段
Claims (6)
- 燃焼装置に、アンモニア及び水素を含む燃料ガスを供給する燃料改質装置であって、
アンモニアタンクと、
アンモニアを改質して、水素含有率が99%以上である高濃度水素ガスを生成する改質器と、
アンモニアと前記高濃度水素ガスとを混合した混合ガスを一時保管し、前記燃焼装置に燃料ガスとして供給する混合タンクと、
前記混合タンクに供給するアンモニアと前記高濃度水素ガスのそれぞれの供給量と、前記燃焼装置に送り出す混合ガスの量を制御する制御手段と、
を備えており、
前記制御手段が、燃焼装置で用いる基準燃料、水素、およびアンモニアの燃焼速度を記憶しており、下記式(1)によって、基準燃料に対する混合ガスの燃焼速度係数Cを算出し、
ここで、S0は基準燃料の燃焼速度であり、SHは水素の燃焼速度であり、SAはアンモニアの燃焼速度であり、Cは混合ガスの燃焼速度係数であり、
さらに式(2)に基づいて混合タンクに供給するアンモニアと水素の体積比を決定しており、
ここで、Mは混合ガスに占める水素の体積比であり、A、Bは定数である、
ことを特徴とする燃料改質装置。 - 前記制御手段が、さらに、前記燃焼装置で用いる基準燃料、水素、およびアンモニアの高位発熱量を記憶しており、基準燃料の高位発熱量に対する混合ガスの高位発熱量の比に基づいて、混合ガスの供給量の基準燃料に対する流量分率を、下記式(3)および式(4)によって決定しており、
ここで、Hmは混合ガスの高位発熱量であり、HHは水素の高位発熱量であり、HAはアンモニアの高位発熱量であり、H0は基準燃料の高位発熱量であり、Wmは基準燃料に対する混合ガスの重量基準の流量分率であり、
さらに、前記燃焼装置から基準燃料の燃料要求速度を入力して、前記混合タンクから前記燃焼装置に供給する混合ガスの供給量を、下記式(5)および式(6)に基づいて決定しており、
ここでmwは混合燃料の分子量であり、W0は燃焼装置から要求された基準燃料の燃料要求速度であり、Fmは、燃焼装置に供給する混合ガスの供給量である、
ことを特徴とする請求項1記載の燃料改質装置。 - 前記改質器が、
アンモニアを分解してプラズマとするためのプラズマ反応容器と、
プラズマ発生用電源と、
前記プラズマ反応容器内に配置された水素分離膜であって、アンモニアのプラズマから水素を分離して、高濃度水素ガスとして混合タンク側の出口に通過させる水素分離膜と、
を備えており、
前記制御手段が、プラズマ発生用電源の電圧とアンモニアタンクからのアンモニア流量を制御して前記高濃度水素ガスの生成量を制御していることを特徴とする請求項1記載の燃料改質装置。 - アンモニアの一部を分解して水素含有率5〜15%である低濃度水素ガスを生成するアンモニア分解触媒反応器と、
生成した前記低濃度水素ガスを一時貯蔵して前記混合タンクに供給する低濃度水素タンクと、
を更に備えており、
前記制御手段が、前記改質器から前記混合タンクに供給する高濃度水素ガスの体積基準の混合分率MHを下記式、すなわち、
MH=(100×M−H2L)/(100−H2L)
に基づいて決定しており、
ここで、H2Lは低濃度タンクのガスの水素濃度(体積%、N2フリー基準)であることを特徴とする請求項1に記載の燃料改質装置。 - 前記制御手段が、
前記アンモニアタンクから前記改質器に供給するアンモニアの供給量を制御する第一のバルブと、
前記アンモニアタンクから前記アンモニア分解触媒反応器に供給するアンモニアの供給量を制御する第二のバルブと、
前記低濃度水素タンクから前記混合タンクに供給する前記低濃度水素ガスの供給量を制御する第三のバルブと、
前記改質器に電力を供給する高電圧電源の電圧と、
前記アンモニア分解触媒反応器に供給する電力の供給量と、
前記燃焼装置に供給する混合ガスの供給量と、
を制御することを特徴とする請求項4に記載の燃料改質装置。 - 燃焼装置にアンモニア及び水素を含む燃料ガスを供給する燃料改質方法であって、
アンモニアと水素の混合比を決定する工程と、
改質器でアンモニアを改質して、水素含有率が99%以上である高濃度水素ガスを生成する工程と、
アンモニアと前記高濃度水素ガスとを混合して混合ガスとする工程と、
前記混合ガスを燃焼装置に供給する工程と、
を備えており、
アンモニアと水素の混合比を決定する工程が、
燃焼装置で用いる基準燃料、水素、およびアンモニアのそれぞれの燃焼速度に基づいて、下記式(1)によって基準燃料に対する混合ガスの燃焼速度係数Cを算出し、
ここで、S0は基準燃料の燃焼速度であり、SHは水素の燃焼速度であり、SAはアンモニアの燃焼速度であり、Cは混合ガスの燃焼速度係数であり、
さらに式(2)に基づいて混合タンクに供給する水素の体積比を決定しており、
ここで、Mは混合ガスに占める水素の体積比であり、A、Bは定数であり、
アンモニアと前記高濃度水素ガスの混合比を、(1−M):Mとすることを特徴とする燃料改質方法。
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