200838611 九、發明說明： 【發明所屬之技術領域】 器設計，利用網目結構 氧化反應觸媒及重組反 媒床堆疊組合，提供最 觸媒床的燃料重組器， 點。整合型單一通道重 氧化反應段及重組反應 段可提供重組器觸媒所 燃料重組器的組合應用 有關燃料重組器。 本發明有關燃料重組 體做為觸媒床，表面喷塗 應觸媒，採多層次網目觸 佳的微流道設計。網目式 兼具微小化及效率高等優 ，，，串接預熱蒸發段、 段等功能，其中氧化反應 茜的溫度條件環境，使得 更佳彈性與便利。本發明 【先前技術】 氣辦5 f代來臨，具有乾淨能源之稱的氫 =池4直石，，提供高效率發電功能。 機車、燃料電池發電機等，所使用之 以U前絕大部分來自於煉油過程，可配 器、燃料電池機車等，在加氫站尚 式氫氣’仍規劃以較安全、符合法規的方 得奇：知：Ϊ的ΐ氫方式，主要以石化燃料中獲 之;1^，两，次為水分解產氫。最常使用 < J、規桓石化辦料制麵 ^ /氧化紹的觸婵床及^甲酵溶液，在含銅/鋅 超過的It Λ當溫度環境條件下，可獲得 料重組器需進率。為符合可攜式產氮功能’燃 前習知的烬化、簡易化等改良設計。目 ’、'、’、重、、且為設計，在容器内裝填粒狀觸 5 200838611 ，丄甲醇溶液經蒸發後流經多孔性 氣。或根據裝置體積微小化J求床心重、, 5媒材料微小化後，噴塗固： = = f床， η? 1中’並採多層板的組合設4 m 鈿小重組器的整體構型。微流，可有效 達到體積縮小的目的，但是i 设計，雖 觸媒床平行，須辦 〃二枓〜動方向，與200838611 IX. Description of the invention: [Technical field to which the invention belongs] The device design utilizes a mesh structure oxidation reaction catalyst and a recombination reaction bed stack combination to provide a fuel recombiner for the most catalytic bed. The integrated single channel reoxidation reaction stage and the recombination reaction stage provide a combined application of the recombiner catalyst recombiner for the fuel recombiner. The invention relates to a fuel recombination body as a catalyst bed, a surface coating spray medium, and a micro flow channel design with a multi-layer mesh contact. The mesh type has the advantages of miniaturization and high efficiency, and the functions of preheating the evaporation section and the section in series, wherein the temperature condition of the oxidation reaction is better, which makes the elasticity and convenience better. [Previous Technology] The gas generation 5 f generation comes, with the name of clean energy hydrogen = pool 4 straight stone, providing high efficiency power generation function. Locomotives, fuel cell generators, etc., most of which are used in the refining process, configurable, fuel cell locomotives, etc., still in the hydrogen refueling station, still planning to be safer and comply with the regulations. : Know: ΐ ΐ hydrogen mode, mainly obtained in petrochemical fuel; 1 ^, two, times water decomposition hydrogen production. The most commonly used < J, the petrochemical material processing surface ^ / oxidation of the touch bed and the solution of the solution, in the copper / zinc excess of the temperature of the environment, the material reconstitutor needs to enter rate. In order to meet the portable nitrogen production function, the improved design of the pre-combustion, such as deuteration and simplification. The object ', ', ', heavy, and design, filled with a granular contact in the container 5 200838611, the methanol solution was evaporated and passed through the porous gas. Or, according to the volume of the device, the bed weight is determined, and after the 5 medium material is miniaturized, the solid solution is sprayed: ==f bed, η?1, and the combination of the multi-layer boards is set to the overall configuration of the 4 m small recombiner. The micro-flow can effectively achieve the purpose of volume reduction, but the i design, although the catalyst bed is parallel, must be 〃2枓~ moving direction, and
:、反應效率。為有效增加微流道i t= 率，可以增加觸媒與燃料之接觸面并床的反應效 的截面寬、高度縮小至0 5随知’將微流道 層效應。但隨著微流道 以增加邊界 刻等加工技術來完成加需藉由餘 板容易因加工過程發生龜曲變形耗=二且薄 合的密封結果。 而衫響权組組 【發明内容】 明如^據以往習用之觸媒床設計，其優缺點摘要說 媒球由於不規則的觸媒球排列，辦.ώ 於缝隙之間，燃料與觸媒床之間的 間杈長，效率較高。一般習用的觸媒球長g尺 T(l^ngthscale)約3〜5mra，表面喷、塗』^觸 媒，然而’觸媒球的表面反應盘：J 較低，空間利用效率亦偏低。槓”體和比羊 (2)微流道觸媒床—在薄板表面佈設 ?;ί道可2=面喷塗反應觸媒；不同反應 £塊可貝塗不同之反應觸媒，再將薄板狀的 6 200838611 =堆疊”組合。微流道觸媒床的空間體 目較於孔洞式觸媒床，確可減少-半 置放太&積構型。但是，由於微流道觸媒床的 撞擊停、:盘ΐίΛ動、方向平行’燃料不易完全 下，網ΐ。ϊ媒充义反應。在相同輸送條件 率，：、?、=二率：低。為增加觸媒反應效 對的ΐ二通截面積愈趨向於微小化，相 子的亦增加微流運的加工成本與困難。:, reaction efficiency. In order to effectively increase the microchannel i t= rate, the contact surface between the catalyst and the fuel can be increased and the reaction efficiency of the bed is wide and the height is reduced to 0.5. However, with the micro-flow channel, the processing technique is added to increase the boundary and engraving, and the sealing result is easy to be caused by the tortuosity deformation due to the processing process. And the shirt ring right group [invention content] Mingru ^ according to the conventional use of the catalyst bed design, its advantages and disadvantages summary said that the media ball due to irregular catalyst ball arrangement, do. Between the gap, fuel and catalyst bed The length between the two is high and the efficiency is high. The conventional catalyst ball length g (T^ngthscale) is about 3~5mra, and the surface is sprayed and coated with the medium. However, the surface reaction plate of the catalyst ball is lower, and the space utilization efficiency is also lower. Bar" body and specific sheep (2) micro-channel catalyst bed - laid on the surface of the sheet?; 道道可2 = surface spray reaction catalyst; different reaction block can be coated with different reaction catalyst, then thin sheet Shaped 6 200838611 = Stacked combination. The space of the microfluidic catalyst bed is smaller than that of the hole-type catalyst bed, and it is possible to reduce the semi-discharge type. However, due to the impact stop of the microfluidic catalyst bed, the disk is Λ Λ, and the direction is parallel. ϊ 充 充 充 。. At the same conveying condition rate, :, ?, = 2 rate: low. In order to increase the reactivity of the catalyst, the cross-sectional area of the second pass is becoming more and more miniaturized, and the phase also increases the processing cost and difficulty of micro-fluid transportation.
觸媒明設計’以網目構型做為觸媒床，將反摩 於網目上，採多層次的堆疊方式K i庆觸媒床及微流道觸媒床的優·點，使得觸 媒床的加1組裝更簡易，反應效㈣較高觸 【實施方式】 I么謹就本發明「燃料重组哭 ^ ^ 所產生的功效，西己合圖式内f’及其 例詳細說明如下。 |出本案之較佳實施 本昃明設計以網目做為觸媒床 一圖」所不，網目2 〇的正面方向罝古π ς/丄以弟 平面方向亦有彎折的流道，二者均、 二^寸十， 觸媒反應條件。在網目的表面噴好的 料2 2穿過層與層之間的流道，、； ：，媒：燃 _人的網目孔洞，與表層觸媒參與 " 氧化燃燒或重組產氫之目的。、反應，達到燃料 燃料重組器的組合設計，請參閱「 所不，在同心環組合的最内圈， =:」 1 8，其内部設置多層次的網目魎迸，=反應段 燃料（包含空氣及碳氫石化燃料）由木0， 後，經觸媒反應，轉變為水装氨 2 4 1進入 “、、礼及二氧化碳（若是 7 200838611 氧氣控制恰當，產物組成為氫氣及二氧化碳），並 釋放出反應熱。以甲醇燃料為例，理論氧化反應 方程式： ch 3〇h+q ·5〇2 亡^ c〇2 七 m 2 或 CH 2〇H +1.5〇2 =ΐ> C02 + 2H20 氧化反應段所產生之熱量，藉由熱傳途徑，The catalyst design is based on the mesh configuration as a catalyst bed, which will be anti-mosquito on the mesh. The multi-layer stacking method is used to make the catalyst bed and the micro-channel catalyst bed. The addition of 1 is easier to assemble, and the reaction effect (4) is higher. [Implementation] I. I would like to elaborate on the effect of the fuel recombination crying ^ ^ in the present invention. The preferred implementation of this case is that the design uses the mesh as a picture of the catalyst bed. The front direction of the mesh 2 罝 π π 丄 丄 丄 丄 丄 弟 弟 弟 弟 弟 弟 弟 弟 弟 弟 弟 弟 弟 弟 弟, 2 inch ten, catalyst reaction conditions. The material sprayed on the surface of the mesh 2 passes through the flow path between the layers, and the medium: the burning hole of the human body, and the surface catalyst participates in the purpose of oxidative combustion or recombinant hydrogen production. , reaction, to achieve the combined design of the fuel fuel recombinator, please refer to "No, in the innermost circle of the concentric ring combination, =:" 18. 8, the internal setting of multi-level mesh 魉迸, = reaction section fuel (including air And hydrocarbon fossil fuel) from wood 0, after the catalyst reaction, converted to water ammonia 2 4 1 into ",, and carbon dioxide (if 7 200838611 oxygen control is appropriate, the product composition is hydrogen and carbon dioxide), and released The reaction heat is taken. Taking the methanol fuel as an example, the theoretical oxidation reaction equation: ch 3〇h+q ·5〇2 死^ c〇2 七 m 2 or CH 2〇H +1.5〇2 =ΐ> C02 + 2H20 oxidation reaction The heat generated by the segment, by means of heat transfer,
攸货燃科垔組汉應段所需的觸媒反應溫度條件 重、组反應段1 6内亦置放多層次的網目觸媒床 0 1，燃料溶液（碳氫石化燃料及水）由2 4 2 ί 入反應段，經觸媒反應，轉變為氫氣及二氧化碳 由2 5 2出口流出至下一氫氣應用階段。以甲丨 燃料為例，理論重組反應方程式： CH3OH + H20 => 3H2 + C〇2 利用同心環狀的重組器組合方式，蒸發段, 別位於氧化反應段與重組反應段之前，採串— 的^合方式。氧化反應段包覆於重組器内部，I =壤Ξ中心溫度最高，重組器的表面溫度則〜 理烟、可減J重組器外部表面所需的熱防護/ j。，目的排列方式’可為與燃料流動方」 U向ΐ斜向角度。請參考「第四圖」所示 5 =裱型恶重組器，相較於三反庫 多層次的網目觸媒床201、、，= 目排列正向於燃料流動方向。 段、料重組11，串接燃料預赛 所示重應段，請參閱「第五圖 之定I由_ 知2 4，輸入燃料溶液及所曾 疋里工乳，在容器的第一段預熱段1 4， 8 200838611 燃料蒸發汽化；在第二段氧化反應段i 8，氧化 觸媒2 0 2將混合氣體内的氧氣與部分燃料充分 反應放熱，適可將混合氣體溫度提昇至適當溫度 ^佈3 ^;在第三段重組反應段i 6，重組觸媒 2 0 j完成混合氣體之重組反應，獲得最終產 ^，氫氣及二氧化碳。若氧氣成分控制不甚準確 ，二最終產物組成尚可能為氫氣、二氧化碳及水 蒸氣。以甲醇燃料為例，整合型燃料重組器 論方程式：The catalyst reaction temperature conditions required for the Hanying section of the cargo burning group are heavy, and the multi-layer mesh catalyst bed is also placed in the reaction section of the group. The fuel solution (carbon fossil fuel and water) is 2 4 2 ί Into the reaction zone, after catalyst reaction, converted to hydrogen and carbon dioxide from the outlet of 2 2 2 to the next hydrogen application stage. Taking the formazan fuel as an example, the theoretical recombination reaction equation: CH3OH + H20 => 3H2 + C〇2 using a concentric annular recombiner combination, the evaporation section, before the oxidation reaction section and the recombination reaction section, The way to ^. The oxidation reaction section is coated inside the recombiner, I = the highest temperature in the center of the soil, and the surface temperature of the recombiner is ~ the smoke protection, which can reduce the thermal protection required for the external surface of the J recombinator / j. The purpose of the arrangement 'can be from the fuel flow side" U-direction oblique angle. Please refer to the “Figure 4” for the 5 = 恶 type of recombiner, compared to the three-anti-base multi-layer mesh bed 201,, = order is in the direction of fuel flow. Section, material reorganization 11, serially connected to the fuel preliminaries, please refer to the "figure of the fifth figure I by _ know 2 4, input fuel solution and the previous work, in the first paragraph of the container Heat section 1 4, 8 200838611 Fuel evaporative vaporization; in the second stage oxidation reaction section i 8, the oxidation catalyst 2 0 2 fully reacts the oxygen in the mixed gas with a part of the fuel to exotherm, so as to raise the temperature of the mixed gas to an appropriate temperature. ^布3 ^; In the third stage of the recombination reaction section i 6, the recombination catalyst 2 0 j completes the recombination reaction of the mixed gas to obtain the final production, hydrogen and carbon dioxide. If the oxygen component is not accurately controlled, the final product composition is still It may be hydrogen, carbon dioxide and water vapor. Taking methanol fuel as an example, the integrated fuel recombiner equation:
4CH3〇H +H20 + ^/02 ^ 4C02+9H2 〇第五圖所示之整合型燃料重組器，採圓柱體 言iU部以網目做為觸媒床’堆疊多層次的網 Ζΐΐ床，可將重組器的機構尺寸微小化。請參 Ξ爲ί六圖」所示，重組器亦可設計為矩形體的 &二方式，網目觸媒床2 1 2與重組器外殼平行 f Γ二為維持重組器的氣密條件，需增加墊圈2 8保護，周圍再以焊接等方式密合。 黃金以！Ϊ媒喊重要組成為奈米白金或奈米 寻貝重金屬，喷塗黏結於網目線材表面。貴 屬觸媒噴塗過程中，可藉由氧化鍅，氧化鋁 ϋϊϊί ’加強黏結效果。重組反應觸媒的重 =复屬成V為銅、鋅、鎳等組合，金屬觸嘴 可藉由氧化錯，氧化銘或氧=喷f ^黏二效果。重組燃料，包含醇類，如甲醇、乙 醇，，烷類，如天然氣等。 哭μ ί閱「第五圖」所示，考慮縮短燃料重組 時間，重組器内設置電熱器50，初期 電能’提高燃料入口溫度至100〜150°c 後，切斷電熱器辅助加熱功能，接續完全由氧化 9 200838611 反應段的反應放熱量，維持重組器自體發熱及燃 料重組功能。 综上所述’本發明的燃料重組器，利用網目 觸媒床，可將幾何型態微小化，進而使本發明更 實用、更符合使用者之所需，確已符合發明專利 申請之要件’爰依法提出專利申請。 惟以上所述者，僅為本發明之燃料重組器設 計實施例而已，當不能以此限定本發明實施之範 圍；故’凡依本發明申請專利範圍及發明說明書 内容所作之簡單的等效變化與修飾，皆應仍屬本 發明專利涵蓋之範圍内。 【圖式簡單說明】 第一圖：係習用之燃料重組器設計示意圖。 第二圖：係本發明之網目觸媒床示意圖。 第三圖：係本發明之燃料重組器設計示意圖。 第四圖：係本發明之另一燃料重組器設計示意圖。 第五圖：係本發明之整合型燃料重組嚣設計示意 圖。 第六圖：係本發明之另一整合型燃料重組器設計 示意圖。 200838611 【主要元件符號說明】 ίο—燃料重組器 14----預熱蒸發段 16 — —重組反應段 1B-----氧化反應段 20----肩媒床 201 —-重組觸媒床 202---氧化觸媒床 211 ---微流道 212 ---網目觸媒床 22 ----燃料 23 ----空氣 24-——入口端 24卜一氧化反應段燃料入口 242——重組反應段燃料入口 25-----出口端 25卜--氧化反應段廢氣出口 252 重組反應段產物出口 26----隔板 28----塾圈片 30----溫度分佈 50----電熱器 114CH3〇H +H20 + ^/02 ^ 4C02+9H2 整合The integrated fuel recombiner shown in the fifth figure, the cylinder of the iU part uses the mesh as the catalyst bed' stacked multi-level mesh boring machine, which can The size of the reorganization unit is small. Please refer to ί六图”, the recombiner can also be designed as a rectangular body & two ways, the mesh catalyst bed 2 1 2 and the recombinator shell parallel f Γ two to maintain the airtight conditions Add washers 28 to protect them, and then close them by welding or the like. Gold to! Ϊ Media shouted an important composition for nano-platinum or nano-seeking heavy metal, sprayed on the surface of the mesh wire. During the spraying process of the catalyst, the bonding effect can be enhanced by yttrium oxide, alumina ϋϊϊί ’. The weight of the recombination reaction catalyst = the complex V is a combination of copper, zinc, nickel, etc., and the metal contact nozzle can be oxidized, oxidized or oxygen = sprayed. Recombinant fuels, including alcohols such as methanol, ethanol, and alkanes such as natural gas. Cry μ ί read "fifth figure", consider shortening the fuel reorganization time, set the electric heater 50 in the recombiner, the initial electric energy 'increasing the fuel inlet temperature to 100~150 °c, cut off the electric heater auxiliary heating function, The continuation of the reaction by the oxidation of 9 200838611 reaction section exotherms, maintaining the regenerative autothermal and fuel recombination functions. In summary, the fuel recombiner of the present invention can utilize the mesh catalyst bed to miniaturize the geometry, thereby making the invention more practical and more in line with the needs of the user, and indeed meets the requirements of the invention patent application.提出 Submit a patent application in accordance with the law. However, the above description is only for the fuel recombiner design embodiment of the present invention, and the scope of the invention is not limited thereto; therefore, the simple equivalent change made by the scope of the invention and the contents of the invention description And modifications are still within the scope of the invention. [Simple description of the diagram] The first picture: a schematic diagram of the design of a conventional fuel recombiner. Second: is a schematic diagram of a mesh bed of the present invention. Third: A schematic diagram of the design of a fuel reformer of the present invention. Fourth Figure: A schematic diagram of another fuel reformer design of the present invention. Fig. 5 is a schematic view showing the design of the integrated fuel recombination enthalpy of the present invention. Figure 6 is a schematic view of another integrated fuel reformer design of the present invention. 200838611 [Explanation of main component symbols] ίο—Fuel recombiner 14----Preheating evaporation section 16 — Recombination reaction section 1B-----Oxidation reaction section 20----Shoulder bed 201--Recombination catalyst Bed 202---oxidation catalyst bed 211 --- micro flow channel 212 --- mesh catalyst bed 22 ----fuel 23 ---- air 24 - - inlet end 24 b oxidation reaction section fuel inlet 242——Recombination reaction section fuel inlet 25-----outlet end 25---oxidation reaction section exhaust gas outlet 252 recombination reaction section product outlet 26----partition 28----ring ring piece 30--- - Temperature distribution 50----Electric heater 11