TWI788940B - Plate Recombiner - Google Patents
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Abstract
一種平板型重組器包含一本體、複數個波浪結構、一蓋板，及一觸媒層，該本體包括一設置面，該設置面形成一流道，該流道朝著一行經路徑延伸，該本體還形成一入口及一出口，該流道連接在該入口及該出口之間，且與該入口及該出口連通，該等波浪結構沿著該行經路徑連續地設置在該流道，該蓋板可移動地覆蓋該設置面，該觸媒層設置在該蓋板，在該蓋板覆蓋該本體時，該觸媒層在該蓋板與該本體之間，且對應在該設置面。 A flat plate recombiner includes a body, a plurality of wave structures, a cover plate, and a catalyst layer, the body includes a setting surface, the setting surface forms a flow channel, the flow channel extends toward a path, the body An inlet and an outlet are also formed, the flow channel is connected between the inlet and the outlet, and communicated with the inlet and the outlet, the wave structures are continuously arranged on the flow channel along the traveling path, and the cover plate The setting surface is movably covered, the catalyst layer is set on the cover plate, and when the cover plate covers the body, the catalyst layer is between the cover plate and the body and corresponds to the setting surface.
Description
本發明係關於一種平板型重組器，尤指利用複數個波浪結構以提升反應物轉換率的平板型重組器。 The invention relates to a flat-plate recombiner, especially a flat-plate recombiner which utilizes a plurality of wave structures to increase the conversion rate of reactants.
質子交換膜燃料電池(Proton Exchange Membrane Fuel Cell,PEMFC)是一種以氫氣為燃料，透過空氣中的氧氣為氧化劑進行氧化還原反應，產生電力與熱。由於質子交換膜燃料電池的工作溫度較低(常溫至100℃)、高效率、無汙染、低噪音、並可於室溫達到高功率電流密度輸出等優點，近年來被視為攜帶式電源的最佳選擇。其中氫氣可由甲醇及水(燃料)在重組器內加熱經由觸媒催化進行重組反應獲得，燃料與觸媒愈充分接觸，將有助於提高重組器產氫性能。化學式為：CH3OH+H2O+熱量→CO2+3H2。 Proton Exchange Membrane Fuel Cell (PEMFC) is a kind of hydrogen as fuel, through the oxygen in the air as the oxidant for redox reaction to generate electricity and heat. Due to the advantages of low operating temperature (room temperature to 100°C), high efficiency, no pollution, low noise, and high power current density output at room temperature, the proton exchange membrane fuel cell has been regarded as a portable power source in recent years. best choice. Among them, hydrogen can be obtained by heating methanol and water (fuel) in the recombiner through catalytic recombination reaction. The more fully the fuel and the catalyst are in contact, the better the hydrogen production performance of the recombiner will be. The chemical formula is: CH 3 OH + H 2 O + heat → CO 2 + 3H 2 .
參閱第二十一圖至第二十三圖，傳統的重組器10包括一本體101，及一蓋板102，該本體101形成一流道103、一入口104，及一出口105，該流道103與該入口104、該出口105連通，一觸媒層106設置在該蓋板102，該蓋板102覆蓋該本體101時，該觸媒層106對應在該流道103的一側面，該流道103的高度以符號H’表示，為該流道103的底端至該觸媒層106之間的距離，該流道103的其中一直線延伸的長度以L’表示，在進行重組反應時，加熱該蓋板102，使熱傳至該流道103內，燃料從該入口104進入該流道103內流動，同時與該觸媒層106接觸，之後從該出口105輸出。然而，在傳統的重組器10中，燃料在該流道103內只有靠近該觸媒層106的燃料比較容易接觸到該觸媒層106，燃料在
還沒充分接觸到106該觸媒層即從該出口105排出，導致產氫性能不高，因此，如何能提高產氫性能一直是本領域研究的目標。
Referring to the twenty-first figure to the twenty-third figure, the
爰此，本發明人為提高反應物的轉換率及重組性能，而提出一種平板型重組器。 Therefore, in order to improve the conversion rate and recombination performance of reactants, the present inventor proposes a flat plate recombiner.
該平板型重組器包含一本體、複數個波浪結構、一蓋板，及一觸媒層，該本體包括一設置面，該設置面形成一流道，該流道朝著一行經路徑延伸，該本體還形成一入口及一出口，該流道連接在該入口及該出口之間，且與該入口及該出口連通，該等波浪結構沿著該行經路徑連續地設置在該流道，該蓋板可移動地覆蓋該設置面，該觸媒層設置在該蓋板，在該蓋板覆蓋該本體時，該觸媒層在該蓋板與該本體之間，且對應在該設置面，該流道的高度為每一波浪結構的平衡位置至該觸媒層之間的距離，該流道的高度與所述每一波浪結構的振幅的比例介於1.14至2.1之間。 The flat-plate recombiner includes a body, a plurality of wave structures, a cover plate, and a catalyst layer, the body includes a setting surface, the setting surface forms a flow channel, and the flow channel extends toward a path, the body An inlet and an outlet are also formed, the flow channel is connected between the inlet and the outlet, and communicated with the inlet and the outlet, the wave structures are continuously arranged on the flow channel along the traveling path, and the cover plate movably cover the setting surface, the catalyst layer is arranged on the cover plate, when the cover plate covers the body, the catalyst layer is between the cover plate and the body, and corresponds to the setting surface, the flow The height of the channel is the distance from the equilibrium position of each wave structure to the catalyst layer, and the ratio of the height of the flow channel to the amplitude of each wave structure is between 1.14 and 2.1.
進一步，該流道的高度為每一波浪結構的平衡位置至該觸媒層之間的距離，在該流道的高度為1.5mm時，所述每一波浪結構的振幅介於0.713mm至1.31mm之間。 Further, the height of the channel is the distance from the equilibrium position of each wave structure to the catalyst layer, and when the height of the channel is 1.5 mm, the amplitude of each wave structure is between 0.713 mm and 1.31 mm. between mm.
進一步，該流道的其中一直線延伸的長度與所述每一波浪結構的波長的比例介於7.91至21之間。 Further, the ratio of the length of a straight line of the channel to the wavelength of each wave structure is between 7.91 and 21.
進一步，該流道的其中一直線延伸的長度為50mm時，所述每一波浪結構的波長介於2.38mm至6.3mm之間。 Further, when the length of one straight line of the channel is 50 mm, the wavelength of each wave structure is between 2.38 mm and 6.3 mm.
進一步，該本體概呈一長方體，該本體還包括一入口面及一出口面，該入口面及該出口面皆連接該設置面，且分別位於該設置面的二相反側， 該入口形成在該入口面，且經由一入口通道連通該流道，該出口形成在該出口面，該流道經由一出口通道連通該出口。 Further, the body is generally in the shape of a cuboid, and the body also includes an inlet surface and an outlet surface, the inlet surface and the outlet surface are both connected to the installation surface, and are respectively located on two opposite sides of the installation surface, The inlet is formed on the inlet surface and communicates with the flow channel through an inlet channel, and the outlet is formed on the outlet surface, and the flow channel communicates with the outlet through an outlet channel.
根據上述技術特徵可達成以下功效： According to the above-mentioned technical features, the following effects can be achieved:
1.藉由該等波浪結構的波峰區段會阻擋一反應物流動，以擠壓的方式強迫該反應物進入該觸媒層，進而使得該觸媒層內部能夠擁有更多的反應物參與觸媒反應，以提升重組性能，而該等波浪結構的波谷區段會對觸媒內部的反應物流體形成所謂的陷阱效應，以延長該反應物於平板型重組器內部之停滯時間，進而使得該反應物於該觸媒層內部能獲得更充分的觸媒反應。 1. The crest section of the wave structure will block the flow of a reactant, and force the reactant to enter the catalyst layer by squeezing, so that more reactants can participate in the catalyst layer. media reaction to improve recombination performance, and the trough section of the wave structure will form a so-called trap effect on the reactant fluid inside the catalyst to prolong the stagnation time of the reactant inside the flat plate recombiner, thereby making the The reactant can obtain more sufficient catalytic reaction inside the catalyst layer.
2.藉由該流道的高度與所述每一波浪結構的振幅的比例介於1.14至2.1之間，獲得更高的反應物的轉換率及重組性能。 2. As the ratio of the height of the channel to the amplitude of each wave structure is between 1.14 and 2.1, a higher conversion rate and recombination performance of reactants can be obtained.
3.藉由該流道的其中一直線延伸的長度與所述每一波浪結構的波長的比例介於7.91至21之間，獲得更高的反應物的轉換率及重組性能。 3. As the ratio of the length of a straight line of the channel to the wavelength of each wave structure is between 7.91 and 21, a higher conversion rate and recombination performance of reactants can be obtained.
1:本體 1: Ontology
11:設置面 11: Setting the surface
12:入口面 12: Entrance face
13:出口面 13: Export side
14:流道 14: Runner
15:入口 15: Entrance
16:出口 16: Export
17:入口通道 17: Entryway
18:出口通道 18: Exit channel
2:波浪結構 2: Wave structure
3:蓋板 3: Cover
31:凹槽 31: Groove
4:觸媒層 4: Catalyst layer
10:重組器 10: Reassembler
101:本體 101: Ontology
102:蓋板 102: cover plate
103:流道 103: Runner
104:入口 104: Entrance
105:出口 105: export
106:觸媒層 106: Catalyst layer
H:流道的高度 H: the height of the runner
W:流道的寬度 W: the width of the runner
L:流道的其中一直線延伸的長度 L: the length of one of the straight lines of the runner
A:波浪結構的振幅 A: The amplitude of the wave structure
λ:波浪結構的波長 λ: wavelength of the wave structure
H’:傳統重組器流道的高度 H': the height of the flow channel of the traditional reformer
L’:傳統重組器流道的其中一直線延伸的長度 L': the length of one of the straight lines of the traditional recombiner channel
[第一圖]是一立體分解圖，說明本發明平板型重組器的一實施例。 [Fig. 1] is an exploded perspective view illustrating an embodiment of the flat-plate recombiner of the present invention.
[第二圖]是一立體圖，說明該實施例的外觀。 [Second Figure] is a perspective view illustrating the appearance of this embodiment.
[第三圖]是一剖視圖，說明該實施例的結構。 [Third Figure] is a sectional view illustrating the structure of this embodiment.
[第四圖]是一局部剖視圖，說明該實施例的一流道及複數個波浪結構。 [Fig. 4] is a partial cross-sectional view illustrating the channel and a plurality of wave structures of this embodiment.
[第五圖]是一局部剖視圖，說明該實施例的該流道及該等波浪結構。 [Fig. 5] is a partial sectional view illustrating the channel and the wave structures of the embodiment.
[第六圖]是一示意圖，說明一反應物在該實施例內進行重組反應時的流向。 [Figure 6] is a schematic diagram illustrating the flow direction of a reactant during a recombination reaction in this embodiment.
[第七圖]是一示意圖，說明一反應物在該實施例內進行重組反應時的狀況。 [Figure 7] is a schematic diagram illustrating the state of a reactant undergoing a recombination reaction in this embodiment.
[第八A圖]是一模擬圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器內，各自的該流道內甲醇的質量分率分佈。 [Eighth Figure A] is a simulation diagram illustrating the mass fraction distribution of methanol in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different amplitudes.
[第八B圖]是一模擬圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器內，各自的該流道內水的質量分率分佈。 [Eighth Figure B] is a simulation diagram illustrating the mass fraction distribution of water in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different amplitudes.
[第九A圖]是一模擬圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器內，各自的該流道內氫的質量分率分佈。 [Ninth Figure A] is a simulation diagram illustrating the mass fraction distribution of hydrogen in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different amplitudes.
[第九B圖]是一模擬圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器內，各自的該流道內二氧化碳的質量分率分佈。 [Figure 9B] is a simulation diagram illustrating the mass fraction distribution of carbon dioxide in the respective flow channels in the traditional recombiner and the flat plate recombiner with three different amplitude wave structures.
[第九C圖]是一模擬圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器內，各自的該流道內該反應物的速度分佈示意。 [Figure 9C] is a simulation diagram illustrating the velocity distribution of the reactants in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different amplitudes.
[第十A圖]是一比較圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器的甲醇轉換率的比較。 [Figure 10A] is a comparison chart illustrating the comparison of methanol conversion rates between a traditional recombiner and three planar recombiners with wave structures of different amplitudes.
[第十B圖]是一比較圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器的氫氣質量分率的比較。 [Figure 10B] is a comparison chart illustrating the comparison of the hydrogen mass fractions of a traditional recombiner and three planar recombiners with wave structures of different amplitudes.
[第十C圖]是一比較圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器的二氧化碳質量分率的比較。 [Figure 10C] is a comparison chart illustrating the comparison of the mass fraction of carbon dioxide in a traditional recombiner and three planar recombiners with wave structures of different amplitudes.
[第十一A圖]是一模擬圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器內，各自的該流道內甲醇的質量分率分佈。 [Figure 11A] is a simulated figure, illustrating the mass fraction distribution of methanol in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十一B圖]是一模擬圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器內，各自的該流道內水的質量分率分佈。 [Figure 11B] is a simulation diagram illustrating the mass fraction distribution of water in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十二A圖]是一模擬圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器內，各自的該流道內氫的質量分率分佈。 [Figure 12A] is a simulation diagram illustrating the mass fraction distribution of hydrogen in the respective flow channels in a conventional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十二B圖]是一模擬圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器內，各自的該流道內二氧化碳的質量分率分佈。 [Figure 12B] is a simulation diagram illustrating the mass fraction distribution of carbon dioxide in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十二C圖]是一模擬圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器內，各自的該流道內該反應物的速度分佈示意。 [Figure 12C] is a simulation diagram illustrating the velocity distribution of the reactants in the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十三A圖]是一比較圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器的甲醇轉換率的比較。 [Figure 13A] is a comparison chart illustrating the comparison of methanol conversion rates between a conventional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十三B圖]是一比較圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器的氫氣質量分率的比較。 [Figure 13B] is a comparison chart illustrating the comparison of the mass fraction of hydrogen in a traditional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十三C圖]是一比較圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器的二氧化碳質量分率的比較。 [Figure 13C] is a comparison chart illustrating the comparison of the mass fraction of carbon dioxide in a traditional recombiner and a planar recombiner with wave structures of three different wavelengths.
[第十四A圖]是一模擬圖，說明操作在三種不同操作溫度的平板型重組器內，各自的該流道內甲醇的質量分率分佈。 [Figure 14A] is a simulated figure illustrating the mass fraction distribution of methanol in the respective flow channels in the flat-plate recombiner operating at three different operating temperatures.
[第十四B圖]是一模擬圖，說明操作在三種不同操作溫度的平板型重組器內，各自的該流道內水的質量分率分佈。 [Figure 14B] is a simulated figure illustrating the mass fraction distribution of water in the respective flow channels in the flat-plate recombiner operating at three different operating temperatures.
[第十五A圖]是一模擬圖，說明操作在三種不同操作溫度的平板型重組器內，各自的該流道內氫的質量分率分佈。 [Figure 15A] is a simulated figure illustrating the mass fraction distribution of hydrogen in the respective flow channels in the flat-plate recombiner operating at three different operating temperatures.
[第十五B圖]是一模擬圖，說明操作在三種不同操作溫度的平板型重組器內，各自的該流道內二氧化碳的質量分率分佈。 [Figure 15B] is a simulated figure illustrating the mass fraction distribution of carbon dioxide in the respective flow channels in the flat-plate recombiner operating at three different operating temperatures.
[第十六A圖]是一關係圖，說明平板型重組器的甲醇轉換率與操作溫度的關係。 [Figure 16A] is a relationship diagram illustrating the relationship between the conversion rate of methanol and the operating temperature of a plate type recombiner.
[第十六B圖]是一關係圖，說明平板型重組器的氫氣質量分率與操作溫度的關係。 [Sixteenth Figure B] is a relationship diagram illustrating the relationship between the hydrogen mass fraction and the operating temperature of the flat-plate reformer.
[第十六C圖]是一關係圖，說明平板型重組器的二氧化碳質量分率與操作溫度的關係。 [Figure 16C] is a relationship diagram illustrating the relationship between the mass fraction of carbon dioxide and the operating temperature of a flat-plate recombiner.
[第十七A圖]是一模擬圖，說明操作在三種不同操作溫度的平板型重組器內，各自的該流道的壓力分佈。 [Figure 17A] is a simulated figure illustrating the pressure distribution of the respective flow channels in the flat-plate recombiner operating at three different operating temperatures.
[第十七B圖]是一模擬圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器內，各自的該流道的壓力分佈。 [Figure 17B] is a simulation diagram illustrating the pressure distribution of the respective flow channels in the traditional recombiner and the flat plate recombiner with wave structures of three different amplitudes.
[第十七C圖]是一模擬圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器內，各自的該流道的壓力分佈。 [Figure 17C] is a simulation diagram illustrating the pressure distribution of the respective flow channels in a traditional recombiner and a flat plate recombiner with wave structures of three different wavelengths.
[第十八A圖]是一關係圖，說明平板型重組器的流道的壓力降與操作溫度的關係。 [Figure 18A] is a relationship diagram illustrating the relationship between the pressure drop of the flow channel of the plate type recombiner and the operating temperature.
[第十八B圖]是一關係圖，說明平板型重組器的實質燃料電池輸出淨功率與操作溫度的關係。 [Figure 18B] is a relationship diagram illustrating the relationship between the actual fuel cell output net power and operating temperature of a flat-plate reformer.
[第十八C圖]是一比較圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器內，各自流道的壓力降的比較。 [Figure 18C] is a comparison diagram illustrating the comparison of the pressure drops in the respective flow channels in the traditional recombiner and the flat plate recombiner with wave structures of three different amplitudes.
[第十八D圖]是一比較圖，說明傳統的重組器、及三種不同振幅之波浪結構的平板型重組器，各自實質燃料電池輸出淨功率的比較。 [Figure 18D] is a comparison diagram illustrating the comparison of the net output power of the actual fuel cell for a traditional recombiner and three planar recombiners with wave structures with different amplitudes.
[第十八E圖]是一比較圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器內，各自流道的壓力降的比較。 [Figure 18E] is a comparison diagram, illustrating the comparison of the pressure drop of the respective flow channels in the traditional recombiner and the flat plate recombiner with wave structures of three different wavelengths.
[第十八F圖]是一比較圖，說明傳統的重組器、及三種不同波長之波浪結構的平板型重組器，各自實質燃料電池輸出淨功率的比較。 [Figure 18F] is a comparison diagram, illustrating the comparison of the net output power of the actual fuel cell for the traditional recombiner and the planar recombiner with wave structure of three different wavelengths.
[第十九圖]是一示意圖，說明實際利用該平板型重組器進行重組反應。 [Figure 19] is a schematic diagram illustrating the actual use of the plate-type recombiner for recombination reactions.
[第二十圖]是一比較圖，說明實際量測、模擬之甲醇轉換率及氫氣質量分率之比較。 [Figure 20] is a comparison chart, illustrating the comparison between actual measurement and simulated methanol conversion rate and hydrogen mass fraction.
[第二十一圖]是一立體分解圖，說明傳統的重組器。 [Figure 21] is a three-dimensional exploded view illustrating a traditional recombiner.
[第二十二圖]是一局部剖視圖，說明該重組器的一流道。 [Figure 22] is a partial sectional view illustrating the flow path of the recombiner.
[第二十三圖]是一示意圖，說明一反應物在該重組器內進行重組反應時的狀況。 [Figure 23] is a schematic diagram illustrating the state of a reactant undergoing a recombination reaction in the recombiner.
綜合上述技術特徵，本發明平板型重組器的主要功效將可於下述實施例清楚呈現。 Based on the above technical features, the main functions of the flat plate recombiner of the present invention will be clearly presented in the following embodiments.
參閱第一圖至第三圖，本發明平板型重組器的一實施例，該平板型重組器包含一本體1、複數個波浪結構2、一蓋板3，及一觸媒層4。
Referring to the first figure to the third figure, an embodiment of the flat plate recombiner of the present invention, the flat plate recombiner includes a
該本體1概呈一立方體，該本體1包括一設置面11、一入口面12及一出口面13。該設置面11概呈一正方形，位於該本體1的頂面，該入口面12及該出口面13各自概呈一矩形，該入口面12及該出口面13分別連接於該設置面11的二相反側，該設置面11形成一流道14，該流道14朝著一行經路徑延伸，該入口面12形成一入口15，該出口面13形成一出口16，該流道14連接在該入口15及該出口16之間，該入口15經由一入口通道17連通該流道14，該流道14經由一出口通道18連通該出口16。
The
該等波浪結構2鉛著該行經路徑連續地設置在該流道14。
The
該蓋板3可移動地覆蓋該設置面11，該蓋板3形成一凹槽31。
The
該觸媒層4設置在該凹槽31內，在該蓋板3覆蓋該本體1時，該觸媒層4在該蓋板3與該本體1之間，且對應在該設置面11上的流道14。
The
參閱第四圖至第六圖，該流道14的高度以符號H表示，為每一波浪結構2的平衡位置至該觸媒層4之間的距離，該流道14的寬度以符號W表示，該流道14的其中一直線延伸的長度以L表示。每一波浪結構2的振幅以符號A表示，每一波浪結構2的波長以符號λ表示。其中，該流道14的高度與所述每一波浪結構2的振幅的比例介於1.14至2.1之間，更進一步，在該流道14的高度為1.5
mm時，所述每一波浪結構2的振幅介於0.713mm至1.31mm之間。該流道14的其中一直線延伸的長度與所述每一波浪結構2的波長的比例介於7.91至21之間，更進一步，在該流道14的其中一直線延伸的長度為50mm時，所述每一波浪結構2的波長介於2.38mm至6.3mm之間。
Referring to the fourth figure to the sixth figure, the height of the
參閱第一圖、第六圖及第七圖，該平板型重組器在進行重組反應，從該入口15進入的一反應物(甲醇水溶液)在遇到該等波浪結構2時，該等波浪結構2的波峰區段會阻擋該反應物流動，以擠壓的方式強迫該反應物接觸該觸媒層4，進而使得該反應物更大量的與該觸媒層4反應，以提升重組性能，更進一步，該等波浪結構2的波谷區段會對流道內的反應物流體形成所謂的陷阱效應，以延長該反應物於平板型重組器內部之停滯時間，進而使得該反應物與該觸媒層4獲得更充分的觸媒反應，藉由該等波浪結構2突縮突擴的流道效應將會促進流體的混合，以利於該反應物轉換成一產物(氫氣及二氧化碳)。
Referring to the first figure, the sixth figure and the seventh figure, the plate type recombiner is carrying out the recombination reaction, and when a reactant (methanol water solution) entering from the
發明人使用三維數值模擬分析，以SIMPLE-C有限體積法之數值程序，選用(38×80×1250)之網格密度作為所有模擬的網格密度標準，針對傳統的重組器10(第二十一圖)及本發明平板型重組器進行模擬分析，證實該平板型重組器的該等波浪結構2在不同的振幅大小、不同的波長皆會影響該產物的轉換率。
The inventor uses three-dimensional numerical simulation analysis, uses the numerical program of SIMPLE-C finite volume method, selects the grid density of (38 × 80 × 1250) as the grid density standard of all simulations, for the traditional recombiner 10 (twentieth Figure 1) and the flat panel recombiner of the present invention are simulated and analyzed, and it is confirmed that the
以下為不同的振幅的模擬：參閱第八A圖、第八B圖、第九A圖及第九B圖，在操作溫度為250℃之條件下，傳統的重組器10的該流道的高度為1.5mm，三種平板型重組器的該流道高度皆為1.5mm，三種平板型重組器的每一波浪結構2的振幅分別為0.75mm、1.0mm、1.25mm，且波長皆為2.5mm，經由模擬驗證，該反應物在遇到
該等波浪結構2時，的確會讓該流道因為該等波浪結構2產生突縮突擴的流道效應，促進該反應物的轉換，圖示的色彩分布代表流道中某一成分的質量分率的分佈。因此，在上述擠壓、陷阱與突縮突擴等效應加成下，該平板型重組器能夠獲得比傳統的該重組器更高的化學反應效率與更佳的重組性能。此外，由於化學重組反應僅發生在該觸媒層內部之緣故，所以該反應物濃度在該觸媒層內部(虛線上方)比該流道(虛線下方)更低，且該產物濃度在觸媒層內部比該流道更高，又由於每一波浪結構2更大的振幅能引起更強的擠壓、陷阱與突縮突擴效應，進而獲得更高的甲醇轉換率及產氫性能。在相同操作條件之下，對三種不同振幅而言，最佳之重組性能是發生在振幅為1.25mm的時候，從速度分布的示意圖第九C圖看出，越靠近該等波浪結構2的波峰區段，該反應物因為遭受擠壓，速度越快、顏色越深，而越靠近波谷區段，該反應物流體形成所謂的陷阱效應，以延長該反應物於該平板型重組器內部之停滯時間，速度越慢、顏色越淺。
The following are the simulations of different amplitudes: refer to the eighth figure A, the eighth figure B, the ninth figure A and the ninth figure B, under the condition that the operating temperature is 250 ° C, the height of the flow channel of the
配合參閱第十A圖至第十C圖，表示傳統的重組器與三種平板型重組器對甲醇轉換率、產生氫氣與二氧化碳的整體影響，其中，甲醇轉換率、氫氣產量與二氧化碳釋放量隨著每一波浪結構的振幅增加而明顯增加，圖式內的O代表傳統的重組器的甲醇轉換率、氫氣質量分率及二氧化碳質量分率。 Refer to Figure 10A to Figure 10C together, showing the overall impact of the traditional reformer and three flat plate reformers on the conversion rate of methanol, the production of hydrogen and carbon dioxide, in which the conversion rate of methanol, hydrogen production and carbon dioxide release The amplitude of each wave structure increases significantly, and the O in the diagram represents the methanol conversion rate, hydrogen mass fraction and carbon dioxide mass fraction of the traditional reformer.
以下為不同的波長的模擬：參閱第十一A圖、第十一B圖、第十二A圖及第十二B圖，在操作溫度為250℃之條件下，傳統的重組器的該流道的其中一直線延伸的長度為50mm，三種平板型重組器的該流道的其中一直線延伸的長度皆為50mm，三種平板型重組器的每一波浪結構的波長分別為2.5mm、4.0mm、6.0mm，且振幅皆 為1.0mm，經由模擬驗證，與傳統的該重組器相較之下，平板型重組器內部的該反應物(甲醇與水)濃度明顯較低，且該產物(氫氣與二氧化碳)濃度明顯較高，特別是該觸媒層內部且介於該等波浪結構的波峰區段之區域，須注意的是，圖示的色彩分布代表流道中某一成分的質量分率的分佈，為使圖式更清楚明瞭，只顯示流道的部分，而省略示意傳統的重組器及該等波浪結構。由此可知，該平板型重組器透過該等波浪結構，對該反應物流體產生擠壓與陷阱效應，進而使得該平板型重組器能夠比傳統的該重組器獲得更佳的觸媒化學反應率以及重組性能。此外，越短波長的該等波浪結構能夠產生更佳的甲醇重組性能。此乃由於，越短波長的該等波浪結構能引起該流道形成更密集的擠壓效應，更頻繁的強迫該反應物流體接觸該觸媒層，而且也能更密集的擾亂該流道壁面附近的流體，進而引起更頻繁的壁面摩擦，從速度向量分布圖的速度變化(第十二C圖)，更能明顯得知。此頻繁的壁面摩擦能夠更有效的促進反應物之混合，以提升平板型重組器之甲醇重組性能。在相同操作條件之下，對三種不同波長而言，最佳之重組性能是發生在波長為2.5mm的時候。 The following are simulations of different wavelengths: Refer to Figure 11A, Figure 11B, Figure 12A and Figure 12B, under the condition that the operating temperature is 250 ° C, the flow of the traditional recombiner The length of one of the linear extensions of the channel is 50mm, and the length of one of the linear extensions of the flow channels of the three flat-type recombiners is 50mm, and the wavelengths of each wave structure of the three flat-type recombiners are 2.5mm, 4.0mm, 6.0 mm, and the amplitude is It is 1.0 mm. After simulation verification, compared with the traditional recombiner, the concentration of the reactants (methanol and water) inside the flat recombiner is significantly lower, and the concentration of the products (hydrogen and carbon dioxide) is significantly higher. , especially the area inside the catalyst layer and between the crest sections of the wave structures, it should be noted that the color distribution in the diagram represents the distribution of the mass fraction of a certain component in the flow channel, in order to make the diagram more clear Clearly, only the part of the flow channel is shown, and the conventional recombiner and the wave structures are omitted. It can be seen that, through the wavy structure, the flat plate recombiner can squeeze and trap the reactant fluid, so that the flat plate recombiner can obtain a better catalyst chemical reaction rate than the traditional recombiner and restructuring performance. In addition, the wave structures with shorter wavelengths can lead to better methanol recombination performance. This is because the wave structures with shorter wavelengths can cause the flow channel to form a more intensive squeezing effect, force the reactant fluid to contact the catalyst layer more frequently, and also disturb the flow channel wall more intensively The nearby fluid, which in turn causes more frequent wall friction, can be more clearly known from the velocity variation of the velocity vector distribution diagram (figure 12C). This frequent wall friction can promote the mixing of reactants more effectively, so as to improve the methanol reforming performance of the flat plate reformer. Under the same operating conditions, for the three different wavelengths, the best recombination performance occurs at a wavelength of 2.5 mm.
配合參閱第十三A圖至第十三C圖，表示傳統的重組器與三種平板型重組器對甲醇轉換率、產生氫氣與二氧化碳的整體影響，其中，甲醇轉換率、氫氣產量與二氧化碳釋放量隨著每一波浪結構的波長變短而明顯增加。 Refer to Figure 13A to Figure 13C together, showing the overall impact of the traditional reformer and three flat plate reformers on methanol conversion rate, hydrogen and carbon dioxide production, among which, methanol conversion rate, hydrogen production and carbon dioxide release It increases significantly as the wavelength of each wave structure becomes shorter.
以下為不同的操作溫度的模擬：參閱第十四A圖、第十四B圖、第十五A圖及第十五B圖，發明人對該平板型重組器在多個操作溫度Top也做模擬，以觀察操作溫度Top的效應對甲醇轉換率、產生氫氣與二氧化碳的整體影響，模擬條件為每一波浪結構的振幅為1.0mm，且波長為2.5mm，固定空間流速(SV=3000h-1)及該反應物之水醇 比(S/C=1.1)的條件下，該反應物(甲醇與水)會沿著該流道下游而逐漸減少，且該產物(氫氣與二氧化碳)會沿著該流道下游而逐漸增加，更進一步，該平板型重組器內部的該反應物、該產物與溫度分佈的差異，會隨著操作溫度增加而變得更顯著，因為操作溫度越高，能提供更多的熱能，便更能提高化學反應的效率，因而提昇甲醇轉換率、增加氫氣與二氧化碳的產生。因此，該平板型重組器最佳產氫性能是發生在操作溫度為300℃時。 The following are the simulations of different operating temperatures: referring to the fourteenth A figure, the fourteenth B figure, the fifteenth A figure and the fifteenth B figure, the inventor also performed a plurality of operating temperatures T op on the flat plate recombiner Do a simulation to observe the effect of the operating temperature T op on the methanol conversion rate and the overall impact of hydrogen and carbon dioxide production. The simulation conditions are that the amplitude of each wave structure is 1.0mm, and the wavelength is 2.5mm, and the space velocity is fixed (SV=3000h -1 ) and the water-alcohol ratio of the reactant (S/C=1.1), the reactant (methanol and water) will gradually decrease along the downstream of the channel, and the product (hydrogen and carbon dioxide) will gradually increase along the downstream of the flow channel, and further, the difference between the reactant, the product and the temperature distribution inside the flat plate reformer will become more significant as the operating temperature increases, because the higher the operating temperature, The more heat energy can be provided, the more efficient the chemical reaction can be, thus improving the conversion rate of methanol and increasing the production of hydrogen and carbon dioxide. Therefore, the best hydrogen production performance of the flat-plate recombiner occurs when the operating temperature is 300°C.
配合參閱第十六A圖至第十六C圖，表示甲醇轉換率、產生氫氣與二氧化碳隨著操作溫度增加而明顯增加。即越高的操作溫度，能獲得更高的觸媒化學反應效率，以提昇甲醇轉換率，並增加氫氣產出與釋放更多二氧化碳。因此，提高操作溫度能明顯提昇該平板型重組器之重組性能。 Refer to Figures 16A to 16C together, which show that the conversion rate of methanol, the generation of hydrogen and carbon dioxide increase significantly with the increase of operating temperature. That is, the higher the operating temperature, the higher the catalytic chemical reaction efficiency can be obtained, so as to improve the methanol conversion rate, increase the hydrogen output and release more carbon dioxide. Therefore, increasing the operating temperature can significantly improve the recombination performance of the flat-plate recombiner.
以下為不同操作溫度造成不同壓力降的模擬：參閱第十七A圖、第十八A圖，及第十八B圖，當該平板型重組器的內部之壓力降過大時，將會導致燃料電池系統需付出更多用來輸送該產物與該反應物的額外推進動力成本，以致實際可以利用之質子交換膜燃料電池的淨輸出功率降低。發明人針對該平板型重組器的每一波浪結構的振幅設為1.0mm，波長為2.5mm，在三種操作溫度Top分別為250℃、275℃、300℃的狀況下的壓力分佈，模擬結果為越高的操作溫度，將導致更大的壓力降，因而需要更大的額外推進動力來輸送該平板型重組器內部的該反應物與該產物。實質燃料電池輸出淨功率可將模擬結果代入以下公式運算獲得。 The following is a simulation of different pressure drops caused by different operating temperatures: Refer to Figure 17A, Figure 18A, and Figure 18B. When the pressure drop inside the flat-plate reformer is too large, it will cause fuel The battery system needs to pay more extra propulsion power cost for transporting the product and the reactant, so that the net output power of the practically available proton exchange membrane fuel cell is reduced. The inventor set the amplitude of each wave structure of the flat-plate recombiner to 1.0mm, the wavelength to 2.5mm, and the pressure distribution under the conditions of three operating temperatures T op of 250°C, 275°C, and 300°C respectively, and the simulation results A higher operating temperature will result in a greater pressure drop, thus requiring greater additional propulsion power to transport the reactants and the products inside the flat plate reformer. The actual fuel cell output net power can be obtained by substituting the simulation results into the following formula.
WP=△P×Ach×uin----------(2) W P =△P×A ch ×u in ----------(2)
其中，Wnet為實質燃料電池輸出淨功率(單位為W)、WPEMFC為理論質子交換膜燃料電池輸出功率(單位為W)、WP為因該平板型重組器內部壓力降所導致須額外付出輸送該反應物及該產物的推進功率(單位為W)、△P為流道進出口之壓力降(可由模擬結果獲得，單位為Pa)、Ach為該流道入口面積(單位為m2)、uin為入口流速(單位為m/s)。在本例中，以當該平板型重組器產氫流量為375sccm時，可以讓理論質子交換膜燃料電池輸出功率(WPEMFC)為67W之依據，並分別考量氫氣有效使用率(
以下為不同振幅造成不同壓力降的模擬：參閱第十七B圖、第十八C圖，及第十八D圖，發明人針對傳統的重組器與三種平板型重組器進行壓力分佈之模擬。設定參數為操作溫度為250℃，傳統的重組器的該流道的高度為1.5mm，三種平板型重組器的該流道高度皆為1.5mm，三種平板型重組器的每一波浪結構的振幅分別為0.75mm、1.0mm、1.25mm，且波長皆為2.5mm。模擬結果為該等波浪結構的振幅越大，將會導致更大更明顯的壓力降，而且該等平板型重組器都比傳統的重組器需要較大的額外推進動力。 The simulations of different pressure drops caused by different amplitudes are as follows: Refer to Figure 17B, Figure 18C, and Figure 18D, the inventors simulated the pressure distribution for a traditional reformer and three flat plate reformers. The set parameters are as follows: the operating temperature is 250°C, the height of the channel of the traditional recombiner is 1.5mm, the height of the channel of the three flat-type recombiners is 1.5mm, and the amplitude of each wave structure of the three flat-type recombiners They are 0.75mm, 1.0mm, and 1.25mm respectively, and the wavelengths are all 2.5mm. The simulation results show that the larger the amplitude of the wave structure, the greater and more obvious the pressure drop will be, and the flat-plate reformers require greater additional propulsion power than the traditional reformers.
以下為不同波長造成不同壓力降的模擬：參閱第十七C圖、第十八E圖，及第十八F圖，發明人針對傳統的重組器與三種平板型重組器進行壓力分佈之模擬。設定參數為操作溫度為250℃，傳統的重組器的該流道的其中一直線延伸的長度為50mm，三種平板型重組器的該流道的其中一直線延伸的長度皆為50mm，三種平板型重組器的每一波浪結構的波長分別為2.5mm、4.0mm、6.0mm，且振幅皆為1.0mm。模擬結 果為該等波浪結構的波長越縮短，將會導致更大更明顯的壓力降，而且該等平板型重組器都比傳統的重組器需要較大的額外推進動力。 The simulations of different pressure drops caused by different wavelengths are as follows: Refer to Fig. 17C, Fig. 18E, and Fig. 18F. The inventors simulated the pressure distribution for the traditional recombiner and three flat-type recombiners. The set parameters are as follows: the operating temperature is 250°C, the length of one straight line of the flow channel of the traditional recombiner is 50mm, the length of one of the straight lines of the flow channel of the three flat type recombiners is 50mm, and the three flat The wavelengths of each wave structure are 2.5mm, 4.0mm, 6.0mm respectively, and the amplitudes are all 1.0mm. simulated junction Because the shorter the wavelength of these wave structures, the larger and more obvious pressure drop will be caused, and these flat-plate reformers require greater additional propulsion power than traditional reformers.
經由上述不同操作溫度、不同振幅、不同波長造成不同壓力降的模擬及計算結果，該平板型重組器的每一波浪結構在振幅為1.0mm、波長為2.5mm時，將會產生最大之實質燃料電池輸出淨功率。此乃由於在此結構參數能適當地對該反應物引起擠壓、陷阱與突縮突擴效應，以提高該平板型重組器之產氫性能與重組性能，亦能避免過大波幅與過短波長，限制過大壓力降之發生，即能避免實質燃料電池輸出淨功率之降低。每一波浪結構在波幅為1.0mm且波長為2.5mm為最佳結構參數，換算該流道的高度與振幅的比例為1.5，該流道的其中一直線延伸的長度與波長的比例為20。 According to the above simulation and calculation results of different pressure drops caused by different operating temperatures, different amplitudes, and different wavelengths, each wave structure of the flat plate reformer will produce the largest actual fuel when the amplitude is 1.0mm and the wavelength is 2.5mm. The battery outputs net power. This is due to the fact that the structural parameters can properly cause extrusion, trapping and sudden contraction and expansion effects on the reactant, so as to improve the hydrogen production performance and recombination performance of the flat-plate recombiner, and can also avoid excessive amplitude and short wavelength. , to limit the occurrence of excessive pressure drop, that is, to avoid the reduction of the actual net output power of the fuel cell. The optimal structural parameters of each wave structure are 1.0 mm in wave amplitude and 2.5 mm in wavelength. The ratio of the height to the amplitude of the channel is 1.5, and the ratio of the length of a straight line of the channel to the wavelength is 20.
配合參考表一至表三，本發明人將傳統的重組器、不同結構參數的該等平板型重組器與不同操作溫度，模擬且計算出甲醇轉換率、氫氣、二氧化碳的濃度及實質燃料電池輸出淨功率。當操作溫度升高時，實質燃料電池輸出淨功率、甲醇轉換率、氫氣產量與二氧化碳釋放量亦隨之增加。在該等平板型重組器中，當該等波浪結構為波幅1.25mm與波長2.5mm時，能夠產生最高的甲醇轉換率、最多的氫氣產量與二氧化碳產量，但在考慮壓力降的影響時，在該等波浪結構為波幅1.0mm與波長2.5mm時能產生最大的實質燃料電池輸出淨功率。 With reference to Tables 1 to 3, the inventor simulated and calculated the conversion rate of methanol, the concentrations of hydrogen and carbon dioxide, and the net output of the actual fuel cell by using the traditional recombiner, the flat-plate recombiner with different structural parameters and different operating temperatures. power. When the operating temperature increases, the actual fuel cell output net power, methanol conversion rate, hydrogen production and carbon dioxide release also increase. In these flat-plate reformers, when the wave structure has an amplitude of 1.25 mm and a wavelength of 2.5 mm, the highest conversion rate of methanol, the largest production of hydrogen and carbon dioxide can be produced, but when considering the influence of pressure drop, in When the wave structure is 1.0 mm in wave amplitude and 2.5 mm in wavelength, it can generate the maximum net output power of the actual fuel cell.
參閱第一圖及第十九圖，在執行重組反應的實測時，利用一甲醇及水分混合物供應系統將甲醇與水混合成一甲醇水溶液，並加以預熱、揮發，隨即導入該平板型重組器的該入口15，在該蓋板3上設置一電子加熱器，以對該平板型重組器加熱，同時為方便觀察該流道14的溫度變化，在該流道14內設置多個熱電偶，以監測設置點的溫度，在該出口16則將導出的氣體產物經由冷
卻方式將水蒸汽凝結由一氣體集氣袋收集，隨即以氣相層析儀乾基(Dry base)方式量測分析，量測項目包括氫氣及二氧化碳。
Referring to Figure 1 and Figure 19, when carrying out the actual measurement of the recombination reaction, a methanol and water mixture supply system is used to mix methanol and water into a methanol aqueous solution, which is preheated and volatilized, and then introduced into the flat plate recombiner The
配合參閱第二十圖，將同樣的該平板型重組器的結構參數進行實測與模擬的數據比對，數值模擬結果之分佈趨勢與實驗數據之分佈趨勢相似，甲醇轉換率之最大相對誤差約3.52%，產生氫氣質量分率之最大相對誤差約2.41%，再次驗證模擬結果的準確性。 With reference to Figure 20, the structural parameters of the same planar reformer are compared with the measured and simulated data. The distribution trend of the numerical simulation results is similar to the distribution trend of the experimental data, and the maximum relative error of the conversion rate of methanol is about 3.52 %, the maximum relative error of the hydrogen mass fraction is about 2.41%, which verifies the accuracy of the simulation results again.
綜合上述實施例之說明，當可充分瞭解本發明之操作、使用及本發明產生之功效，惟以上所述實施例僅係為本發明之較佳實施例，當不能以此限定本發明實施之範圍，即依本發明申請專利範圍及發明說明內容所作簡單的等效變化與修飾，皆屬本發明涵蓋之範圍內。 Based on the description of the above-mentioned embodiments, it is possible to fully understand the operation of the present invention, use and the effect that the present invention produces, but the above-mentioned embodiments are only preferred embodiments of the present invention, and should not be used to limit the implementation of the present invention. The scope, that is, the simple equivalent changes and modifications made according to the patent scope of the present invention and the content of the description of the invention, all fall within the scope of the present invention.
1:本體 1: Ontology
11:設置面 11: Setting the surface
12:入口面 12: Entrance face
13:出口面 13: Export side
14:流道 14: Runner
15:入口 15: Entrance
16:出口 16: Export
17:入口通道 17: Entryway
18:出口通道 18: Exit channel
2:波浪結構 2: Wave structure
3:蓋板 3: Cover
31:凹槽 31: Groove
4:觸媒層 4: Catalyst layer
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