1310699 九、發明說明： 【發明所屬之技術領域】 本發明係關於一種新穎之分解戴奥辛的方法及裝置， 利用氧化鐵(例如：FeOOH)催化臭氧分解戴奥辛之反應，可 有效分解戴奥辛同時節省能量並解決製程污染問題。 【先前技術】 戴奥辛是世界各國一致公認可能致癌的物質，仍亦導 致孕婦流產或產下畸形兒，也會損害人體肝臟功能與免疫 系統，因此如何避免戴奥辛污染是全世界高度關切的問 題。戴奥辛的來源主要有經由燃燒冶煉金屬、製造水泥、 火力發電、露天燃燒廢電纜廢五金等。為了防止戴奥辛污 染，各國皆致力於研究戴奥辛處理技術。 戴奥辛屬於非常穩定的化合物，因此不易分解，目前 國内最常使用的戴奥辛處理技術為活性碳吸附法，雖具有 不錯的除去效率，但此方法有幾個缺點，包括：活性碳吸 附只是相變化戴奥辛，但其仍存在於集塵灰中，並未徹底 破壞戴奥辛，因此恐有二次污染；又活性碳可能是提供戴 奥辛在合成的碳源，在適當情況下有可能使戴奥辛再合 成；此外，使用活性碳吸附法會使飛灰處理量增加，而提 高固化及掩埋成本。另外，電弧爐是台灣地區戴奥辛主要 的排放源之一，活性碳儲存與操作不當，恐有引起火災之 虞，因此無法適用。此外，在亞洲地區，日本已針對飛灰 中的戴奥辛訂定管制法規（3.0ng-TEQ/g)國内環保署廢管 處已草擬修正部分條款並辦理公聽會，其修正内容包括：（1) 將 2,3,7,8四氯戴奥辛之溶出試驗標準調整為 P10940022TW(本所案號 05P0450) 5 1310699 1000ng-TEQ/kg的總標準量；（2)含戴奥辛廢棄物需以熔融 法處理或以分區獨立衛生掩埋處置或封閉掩埋處置，未來 國内若進行相同管制，活性碳法之適用性將面臨嚴重的衝 擊。因此開發活性碳替代技術是非常重要且急迫的。近年 來利用觸媒處理戴奥辛技術逐漸受到重視，可將戴奥辛分 解或去毒。目前所使用的觸媒多為責金屬觸媒(V,w)，這一 類的觸媒反應溫度較高（約需160°C -380°C )，在應用上， 需要於除塵設備（以袋式集塵機操作溫度為例，焚化爐為 100°C-150°C，電弧爐為60°C-100°C )，之後再加熱至觸媒反 應溫度（160°C -380°C )，在能量利用效率上較不具經濟效 益。 目前國外的戴奥辛分解觸媒多為高溫處理，溫度範圍 . 由160~380 C。曰本選擇性觸媒還原系統中（Selective Catalytic Reduction systems ’ SCR system)所使用之觸媒 ' (NIPPON SHOKUBAI)的活性成份主要為v205/Mo03，載體 為特殊的Ti氧化物，比表面積為loo m2/g，孔隙大小為 0·35~0.4·5 cm3/g ’反應器為蜂巢式(Honeycomb)，其可依照 • 入口之粒狀物濃度而有各式的蜂巢式形狀，限制是粒狀物 濃度須低於50 mg/m3，反應溫度須高於20(TC，分解效率可 達92%以上，它能同時用來處理NOx及戴奥辛。 另外REMEDIA ™ 催化過濾系統中（REMEDIA ™ Catalytic Filter System)，其戴奥辛觸媒分解濾袋能同時去除 氣相及固相之戴奥辛，將其氧化分解破壞生成H20、C02 及HC1 ’至於生成之HC1可利用附著於濾袋上之Ca(OH)2 所吸收，因此能有效去除HC1。觸媒濾袋溫度操作範圍為 180〜260°C、過濾速度為0.8〜1.4 m/min。又，Shell戴奥辛 破壞系統（Shell Dioxin Destruction System (SDDS))可分成 P10940022TW(本所案號 05P0450) 6 1310699 兩大主要部份：一為觸媒(catalyst)，一為模組(module)，模 組内包含觸媒（S-090)，由Shell的Amsterdam研究實驗室發 展出來’主要成份為鈦/鈒’是一具有高活性、高表面積、 多孔隙的金屬化合物，具有良好的氣體擴散能力，反應溫 度160〜380°C，傳統一般的SCR多為蜂巢式型式，SDDS 為側流式反應器（Lateral Flow Reactor; LFR)，内含觸媒， 100%氣體通過，當氣體通過薄層觸媒時，壓降很低，而SDDS •使用的限制為低粒狀物濃度（< 1〇 mg/Nm3)、低SOx濃度。 φ 然而前述幾種習知分解戴奥辛之技術，其反應溫度都 需160°C以上，甚至200°C以上，因此需額外提供加熱裝置 使其溫度達到反應溫度範圍，如此將造成裝置成本上的增 加’而不符經濟效應。因此，為改善上述習知戴奥辛分解 - 之技術之缺點’研發一種將戴奥辛於低溫分解破壞的技術 成為值得研究課題。 【發明内容】 由前述可知，先前技術中之戴奥辛分解技術—活性碳吸 # 附法對於飛灰處理效果有限，而且容易使戴奥辛再合成， 另一方面成本也較高；而傳統觸媒處理技術係需於高溫下 作用’因此本發明提供一種用於分解戴奥辛的裝置及方 法，其主要目的在於低溫下將戴奥辛分解破壞。 為達上述目的，本發明提供一種分解戴奥辛的裝置， 係包含：臭氧產生單元，係用以產生臭氧；以及氧化鐵觸 媒反應單元，前述臭氧產生單元產生之臭氧係導入前述氧 化鐵觸媒反應單元。該臭氧產生單元之臭氧係作為一強氧 化劑，與廢氣中之戴奥辛接觸後，藉由氧化鐵觸媒之催化， 將戴奥辛分解。前述廢氣為煙道廢氣。 P10940022TW(本所案號 05P0450) 7 1310699 在一較佳實施例中，觸媒反應單元之反應溫度為60°C 至！5(rc，較佳為loot：至125T：，最佳為loot至120〇C。 在另一實施例中，分解戴奥辛裝置之臭氧產生單元所 1生之臭氧與戴奥辛接觸後再連接至氧化鐵觸媒反應單 ^ °在另一實施例中，臭氧產生單元所產生之臭氧直接與 : 氧化鐵觸媒反應單元連接。 .本發明之分解戴奥辛裝置中之氧化鐵觸媒反應單元可 進一步與一引風機連接，用以抽氣，使氣體可順利通過氧 • 化鐵觸媒反應單元。 在一較佳實施例中，分解戴奥辛裝置可使用於焚化 爐、電弧爐、燒結爐、非鐵金屬冶煉或火化爐燃燒後之廢 氣。 • 本發明另提供一種利用上述分解戴奥辛裝置用以分解 戴奥辛的方法，係包含： (a) 將含有戴奥辛之廢氣與臭氧產生單元所產生之臭氧 以及氧化鐵觸媒反應單元接觸並反應； (b) 前述臭氧經氧化鐵催化，將戴奥辛分解為二氧化 • 碳、氣化氫以及水。前述含有戴奥辛之廢氣可與臭氧產生 單元所產生之臭氧預先接觸後再導入氧化鐵觸媒反應單 元。前述廢氣為煙道廢氣。 在一較佳實施例中，步驟（a)之反應溫度為6〇°C至150 C，較佳為l〇〇°C至125°c，更佳為loot：至120°C。在另 一較佳實施例中，前述分解戴奥辛的方法可使用於焚化 爐、電弧爐、燒結爐、非鐵金屬冶煉或火化爐產生之廢氣。 本發明之又提供一種分解戴奥辛的方法，係包含：將 含戴奥辛之廢氣與臭氧及氧化鐵接觸反應，藉此將戴奥辛 分解為一氧化碳、氣化氫以及水。前述廢氣為煙道廢氣。 P10940022TW(本所案號 05P0450) 8 1310699 月ίι述臭氧係作為強氧化劑，氧化鐵係作為催化劑。 在一較佳實施例中’上述反應之溫度為60¾至15〇。(：， 較佳為100。〇至125。(：，更佳為10CTC至120〇C。 ^ 本發明提供改良習知技術之分解戴奥辛的方法，利用 氧化鐵，化臭氧於低溫下（60〇C至15(TC )分解戴奥辛之反 應’可節省能量並解決製程污染問題。綜上所述，本發明 開發之分解戴奥辛的裝置與方法，可有效改善習知技彳^ 缺失與弊端。 【實施方式】 本發明所沿用的現有技藝，在此謹作重點式的引用， 以助本發明之闡述。並且下述内文中相關圖式並未依比例 繪製’其作用僅在表現本發明之結構特徵。 本發明根據金屬氧化物觸媒異相催化臭氧 (heterogeneous catalytic ozonation)之能力，包括觸媒種類、 比表面積、孔洞大小及分佈、臭氧濃度等因子選擇轉化能 力較強且不會造成污染且反應溫度低之FeOOH (參考表一b) 作為分解戴奥辛之觸媒。本發明利用觸媒轉化臭氧的^ 伴隨生成的高反應物質，再利用此生成物質進一步 ^ 辛分解破壞。一般常用的觸媒材質，如Mn，c〇 ,冲:、厂 f V為環保署公告列管之重金屬，因此在廢觸媒處理e 若有疏忽，有可能導致二次污染。鐵為綠色材質且 ， 生利用的環境觸媒，成本低廉，故本發明採用氧化 ϋ、虱，由於氣相臭氧會先與Fe(II)(還原態）觸媒反應某 將大乳分解生成〇Λ、〇2-、ΟΗ·與Fe(m)(氧化態），、吸^ Fe(III)(氧化態）表面之戴奥辛分子則被〇Η·進一步 、； 應機制如第一圖所示。 鮮’反 P10940022TW(本所案號 05Ρ0450) 9 1310699 一_堯二$屬氧化物/ γ-Αΐ2ο3轉化臭七比較表 金屬氧化物 (metal oxide) 臭氧轉化率 (%) 速率 (mol s'1 g of oxide'1') 速率 (ΙΠΟί S ^ mnl nf ^ FeOOH 24 0.52xl0'5 0.04xl0'3 V2〇, 8 0.20x10 s 0.018x10—3 CuO 5 0.08x10-5 0.006xl〇·3 本發明所利用之分解戴奥辛的裝置10之一實施態樣 如第二a所示，其係包含臭氧產生機丨、氧化鐵觸媒反^槽 2以及引風機3。其中臭氧產生機1係直接連接於氧化鐵觸 媒反應槽2’使含戴奥辛之廢棄與臭氧於氧化鐵觸媒反應槽 2混合後反應分解戴奥辛。 本發明之分解戴奥辛的裝置1〇,之另一實施態樣如 第二B圖所示，其係包含臭氧產生機1，、氧化鐵觸媒反應 槽2’以及引風機3’。其中臭氧產生機1，係與廢氣進氣管線 4’連結，使臭氧與戴奥辛預先混合後再進入氧化鐵觸媒反應 槽2’反應，分解戴奥辛。 本發明之實施例使用之實驗設備規格如下： (A) 臭氧產生機： (a) 型式：CFS-1 (b) 臭氧產生量：75 g/hr (c) 尺寸：860 mm(L)x380 mm(W)x480 mm(H) ⑷電力規格·· 230 V(單向），760 Watt(VA) (e)附件：〇2鋼瓶 (B) 觸媒反應床：壹座 (a) 型式：臥式 (b) 本體尺寸：〇.92m(直筒長度)x〇.26m(寬)x0.26m(高） P10940022TW(本所案號 〇5p〇450) 10 1310699 (c) 本體材質及厚度：SUS304(3 mm) (d) 保溫：岩棉5〇mm，外覆銘皮 (e) 附件：控制球閥、動靜壓量測孔（量測 計、控制盤 '^1)、差壓 (C) 氧化鐵(FeOOH)觸媒： 〇)平均粒徑：2~5 mm (b) 比表面積：2.8605 (m2/g) (c) 平均孔徑：74.7253 (人） (句密度：3.4475 (g/cm3) (e)Bulk Density · 1.161 (g/cm3) (D) 引風機 (a) 型式：環型鼓風機1310699 IX. Description of the Invention: [Technical Field] The present invention relates to a novel method and apparatus for decomposing dioxin, which utilizes iron oxide (for example, FeOOH) to catalyze the decomposition of dioxin by ozone, which can effectively decompose dioxin and save energy. Solve process pollution problems. [Prior Art] Dioxin is a drug that is recognized by all countries in the world as a possible carcinogen. It still causes miscarriage or birth of deformed children, and it also impairs the function of the liver and the immune system. Therefore, how to avoid dioxin pollution is a matter of global concern. Dioxin's sources include smelting metals, manufacturing cement, thermal power generation, and open-air burning waste cable scrap hardware. In order to prevent Dioxin pollution, all countries are committed to researching Dioxin treatment technology. Dioxin is a very stable compound, so it is not easy to decompose. At present, the most commonly used Dioxin treatment technology in China is activated carbon adsorption. Although it has good removal efficiency, this method has several disadvantages, including: activated carbon adsorption is only phase change. Dioxin, but it still exists in the dust collection ash, which does not completely destroy Dioxin, so there is fear of secondary pollution; and activated carbon may provide the carbon source for the synthesis of Dioxin, and may, if appropriate, re-synthesize Dioxin; The use of activated carbon adsorption will increase the amount of fly ash treatment and increase the cost of solidification and burial. In addition, the electric arc furnace is one of the main sources of Dionxin in Taiwan. The improper storage and operation of activated carbon may cause fires and therefore cannot be applied. In addition, in Asia, Japan has established regulations for Dioxin in fly ash (3.0 ng-TEQ/g). The EPA Waste Management Office has drafted amendments to some of the provisions and conducted public hearings. The amendments include: 1) Adjust the dissolution test standard of 2,3,7,8 tetrachlorodioxin to P10940022TW (Our Office No. 05P0450) 5 1310699 1000ng-TEQ/kg total standard amount; (2) Dioxin-containing waste needs to be melted Treatment or disposal by district independent sanitary burial or closed burial disposal. If the same regulation is carried out in the future in China, the applicability of the activated carbon method will face severe impact. Therefore, the development of activated carbon replacement technology is very important and urgent. In recent years, the use of catalysts to treat Dioxin technology has gradually gained attention, and Dioxin can be decomposed or detoxified. At present, the catalyst used is mostly responsible for the metal catalyst (V, w). This type of catalyst has a high reaction temperature (about 160 ° C -380 ° C). In application, it needs to be used in dust removal equipment (in bags). For example, the operation temperature of the dust collector is 100 ° C - 150 ° C for the incinerator, and the electric arc furnace is 60 ° C - 100 ° C), and then heated to the catalyst reaction temperature (160 ° C - 380 ° C) at the energy. The utilization efficiency is less economical. At present, foreign Dioxin decomposition catalysts are mostly treated at high temperatures, and the temperature range is from 160 to 380 C. The active ingredient of NIPPON SHOKUBAI used in Selective Catalytic Reduction Systems 'SCR system is mainly v205/Mo03, the carrier is special Ti oxide, and the specific surface area is loo m2. /g, pore size is 0·35~0.4·5 cm3/g 'The reactor is Honeycomb, which can have various honeycomb shapes according to the concentration of the inlet particles. The limit is granular. The concentration must be less than 50 mg/m3, the reaction temperature must be higher than 20 (TC, the decomposition efficiency can reach more than 92%, it can be used to treat both NOx and dioxin. In addition, REMEDIA TM Catalytic Filter System, The Dioxin catalytic decomposition filter bag can simultaneously remove the gas phase and the solid phase of dioxin, and oxidize and decompose it to form H20, C02 and HC1'. The resulting HC1 can be absorbed by Ca(OH)2 attached to the filter bag. Therefore, HC1 can be effectively removed. The temperature range of the catalyst filter bag is 180~260°C, and the filtration speed is 0.8~1.4 m/min. In addition, the Shell Dioxin Destruction System (SDDS) can be divided into P10940022TW. (Our Case No. 05P0450) 6 1310699 Two main parts: one is catalyst, one is module, and the module contains catalyst (S-090), by Shell's Amsterdam Research Laboratory Developed 'the main component is titanium / niobium' is a metal compound with high activity, high surface area and porosity, with good gas diffusion capacity, reaction temperature of 160~380 °C, the traditional general SCR is mostly honeycomb type, The SDDS is a Lateral Flow Reactor (LFR) containing a catalyst. 100% gas passes. When the gas passes through the thin layer of catalyst, the pressure drop is very low, while the SDDS • is limited to low granularity. Concentration (<1〇mg/Nm3), low SOx concentration. φ However, the above-mentioned several techniques for decomposing dioxin have a reaction temperature of 160 ° C or more, or even 200 ° C or more, so an additional heating device is required. The temperature reaches the reaction temperature range, which will cause an increase in the cost of the device 'inconsistent with the economic effect. Therefore, in order to improve the shortcomings of the above-mentioned conventional dioxin decomposition technology, a technique for decomposing the damage of dioxin in low temperature is developed. According to the foregoing, it can be seen that the prior art dioxin decomposition technology-active carbon absorption # attached method has limited effect on fly ash treatment, and is easy to re-synthesize dioxin, on the other hand, the cost is high; Catalyst processing technology is required to act at high temperatures. Thus, the present invention provides an apparatus and method for decomposing dioxin, the main purpose of which is to decompose and destroy dioxin at a low temperature. In order to achieve the above object, the present invention provides a device for decomposing dioxin, comprising: an ozone generating unit for generating ozone; and an iron oxide catalyst reaction unit, wherein the ozone generated by the ozone generating unit is introduced into the iron oxide catalyst reaction unit. The ozone of the ozone generating unit acts as a strong oxidizing agent, and after contact with the dioxin in the exhaust gas, the dioxin is decomposed by the catalysis of the iron oxide catalyst. The aforementioned exhaust gas is a flue gas. P10940022TW (Our Office No. 05P0450) 7 1310699 In a preferred embodiment, the reaction temperature of the catalyst reaction unit is 60 ° C to! 5 (rc, preferably loot: to 125T:, preferably from loot to 120 〇 C. In another embodiment, the ozone generated by the ozone generating unit decomposing the dioxin device is contacted with dioxin and then connected to the iron oxide. Catalyst Reaction Unit In another embodiment, the ozone generated by the ozone generating unit is directly connected to: the iron oxide catalyst reaction unit. The iron oxide catalyst reaction unit in the decomposition dioxin device of the present invention may further be combined with The induced draft fan is connected for pumping gas so that the gas can smoothly pass through the oxygen/iron catalyst reaction unit. In a preferred embodiment, the deionizing device can be used for incinerator, electric arc furnace, sintering furnace, non-ferrous metal smelting. Or the exhaust gas after the combustion of the cremator. The present invention further provides a method for decomposing dioxin by using the above-mentioned decomposed dioxin device, which comprises: (a) ozone and iron oxide catalyst generated by the exhaust gas and ozone generating unit containing dioxin The reaction unit contacts and reacts; (b) the ozone is catalyzed by iron oxide to decompose dioxin into carbon dioxide, carbon, hydrogen and water. The exhaust gas may be introduced into the iron oxide catalyst reaction unit before being contacted with the ozone generated by the ozone generating unit. The exhaust gas is flue gas. In a preferred embodiment, the reaction temperature of the step (a) is 6 〇 ° C to 150 C, preferably l ° ° C to 125 ° C, more preferably loot: to 120 ° C. In another preferred embodiment, the aforementioned method of decomposing dioxin can be used in incinerators, electric arc furnaces, sintering The invention further provides a method for decomposing dioxin, which comprises: contacting a dioxin-containing exhaust gas with ozone and iron oxide, thereby decomposing dioxin into carbon monoxide and gasifying Hydrogen and water. The above-mentioned exhaust gas is flue gas. P10940022TW (Our Office No. 05P0450) 8 1310699 month Ozone is used as a strong oxidant, and iron oxide is used as a catalyst. In a preferred embodiment, the temperature of the above reaction is 603⁄4. To 15: (:, preferably 100. 〇 to 125. (:, more preferably 10 CTC to 120 〇 C.) The present invention provides a method for improving the decomposition of dioxin by conventional techniques, using iron oxide to lower ozone The lower (60〇C to 15(TC) decomposes the reaction of dioxin' can save energy and solve the problem of process pollution. In summary, the device and method for decomposing dioxin developed by the present invention can effectively improve the conventional technique and the lack of [Embodiment] The prior art of the present invention is hereby incorporated by reference in its entirety for the purposes of the present disclosure. Structural features of the invention. According to the ability of the metal oxide catalyst heterogeneous catalytic ozonation, including the type of catalyst, specific surface area, pore size and distribution, ozone concentration and the like, the conversion ability is strong and does not cause FeOOH which is polluted and has a low reaction temperature (refer to Table 1b) serves as a catalyst for decomposing dioxin. The present invention utilizes a catalyst to convert ozone into a highly reactive substance which is generated, and further utilizes the produced substance to further decompose and destroy. Commonly used catalyst materials, such as Mn, c〇, rush:, factory f V is the heavy metal announced by the Environmental Protection Agency, so if there is negligence in the waste catalyst treatment e, it may lead to secondary pollution. Iron is a green material, and the environmental catalyst used by the user is low in cost. Therefore, the present invention uses cerium oxide and lanthanum. Since the gas phase ozone first reacts with the Fe(II) (reduced state) catalyst, the large milk is decomposed into strontium. The dioxin molecules on the surface of Λ, 〇2-, ΟΗ· and Fe(m) (oxidized state), and Fe(III) (oxidized state) are further described; the mechanism is as shown in the first figure. Fresh 'anti-P10940022TW (Our Office No. 05Ρ0450) 9 1310699 一_尧二$属oxide / γ-Αΐ2ο3 conversion odor seven comparison table metal oxide (metal oxide) ozone conversion rate (%) rate (mol s'1 g Of oxide '1') Rate (ΙΠΟί S ^ mnl nf ^ FeOOH 24 0.52xl0'5 0.04xl0'3 V2〇, 8 0.20x10 s 0.018x10-3 CuO 5 0.08x10-5 0.006xl〇·3 utilized by the present invention One embodiment of the device 10 for decomposing dioxin is as shown in the second a, which comprises an ozone generator, an iron oxide catalyst, and an induced draft fan 3. The ozone generator 1 is directly connected to the iron oxide. The catalyst reaction tank 2' reacts the dioxin-containing waste with the ozone in the iron oxide catalyst reaction tank 2 to decompose the dioxin. The apparatus for decomposing the dioxin of the present invention is another one, as shown in the second B. The system includes an ozone generator 1, an iron oxide catalyst reaction tank 2', and an induced draft fan 3'. The ozone generator 1 is connected to the exhaust gas intake line 4' to pre-mix the ozone with the dioxin and then enter the oxidation. The iron catalyst reaction tank 2' reacts to decompose dioxin. Embodiments of the invention The specifications of the experimental equipment used are as follows: (A) Ozone generator: (a) Type: CFS-1 (b) Ozone production: 75 g/hr (c) Dimensions: 860 mm (L) x 380 mm (W) x 480 mm (H) (4) Power specifications · · 230 V (one-way), 760 Watt (VA) (e) Accessories: 〇 2 cylinder (B) Catalytic reaction bed: squat (a) Type: horizontal (b) body size : 〇.92m (straight length) x 〇.26m (width) x0.26m (height) P10940022TW (Oh, 案5p〇450) 10 1310699 (c) Body material and thickness: SUS304 (3 mm) (d) Insulation: rock wool 5〇mm, outer cover (e) Accessories: control ball valve, dynamic and static pressure measuring hole (measuring meter, control panel '^1), differential pressure (C) iron oxide (FeOOH) catalyst: 〇) Average particle size: 2~5 mm (b) Specific surface area: 2.8605 (m2/g) (c) Average pore diameter: 74.7253 (person) (sentence density: 3.4475 (g/cm3) (e) Bulk Density · 1.161 ( g/cm3) (D) induced draft fan (a) type: ring blower
(b) 馬力：3 HP (c) 電力規格：3 p x220Vx60Hz (d) 靜壓：1600 mmH20 (e) 風量：5.5 m3/min.(b) Horsepower: 3 HP (c) Power specification: 3 p x 220Vx60Hz (d) Static pressure: 1600 mmH20 (e) Air volume: 5.5 m3/min.
以下係提供利用本發明之實施例詳細說明書本發明 技術及特點，然本實施例並非用以限定本發明了任^熟= 此技藝者，在不脫離本發明之精神和範圍内，當可 之更動與潤飾。 胃 種 實施例 置盛企1二^：_以本發明之裝置處理煙氣中 利用本發明之裝置（如前述第二A圖），進行將焚化 爐真實煙氣中的戴奥辛分解實驗測試，操作條件如表二所 示。測試結果如表三所示。一般焚化爐出口廢氣中含戴奥 P10940022TW(本所案號 05P0450) 11 1310699 辛之平均濃度為>l〇ng-TEQ/Nm3。經實場實驗測試，發現經 本發明裝置處理後，廢氣中戴奥辛去除效率在Run 1為97.4 %，於Run 2為85.6 %。此外，觸媒中戴奥辛濃度為2.73x 10_3ng-TEQ/g，濃度相當低，顯示戴奥辛物種是被本發明之 方式分解，而非吸附作用。由本實驗可知，利用本發明之 臭氧/氧化鐵裝置，可有效處理戴奥辛，將戴奥辛分解為無 毒物質。The present invention is not limited to the embodiments of the present invention, and the present invention is not limited to the spirit and scope of the present invention. Change and retouch. Example of a stomach species is set up in a factory: using the apparatus of the present invention to treat flue gas by using the apparatus of the present invention (such as the aforementioned second A diagram), performing a test of the Deoxin decomposition in the real flue gas of the incinerator, operation The conditions are shown in Table 2. The test results are shown in Table 3. The general incineration furnace exhaust gas contains Dai O P10940022TW (Our Office No. 05P0450) 11 1310699 The average concentration of Xin is > l〇ng-TEQ/Nm3. After field experiment, it was found that the dioxin removal efficiency in the exhaust gas was 97.4% in Run 1 and 85.6 % in Run 2 after treatment by the apparatus of the present invention. In addition, the concentration of dioxin in the catalyst was 2.73 x 10_3 ng-TEQ/g, and the concentration was rather low, indicating that the dioxin species was decomposed by the present invention rather than adsorbed. From the experiment, it is known that the ozone/iron oxide device of the present invention can effectively treat dioxin and decompose dioxin into a non-toxic substance.
表二：實驗操作條件 項目 Runl 單位 入口 出口 1.氣量 m3/hr 106 2.空間速度 1/hr 5400 3.操作溫度 °C 125 4.〇3 〇3產生量(g/hr) 20 〇3 濃度(mg/m3) 200 5.乾式氣體體積 (Ym(std),latm,0〇C) Nm3(dscm) 2.116 2.074 6.排氣含氧量(％) % 15.1 16.6Table 2: Experimental operating conditions Item Runl Unit inlet outlet 1. Volume m3/hr 106 2. Space velocity 1/hr 5400 3. Operating temperature °C 125 4.〇3 〇3 production amount (g/hr) 20 〇3 concentration (mg/m3) 200 5. Dry gas volume (Ym(std), lapm, 0〇C) Nm3(dscm) 2.116 2.074 6. Exhaust oxygen content (%) % 15.1 16.6
項目 Run2 單位 入口 出σ 1.氣量 m3/hr 110 2.空間速度 l/hr 5400 3.操作溫度 °C 120 4.〇3 〇3產生量(g/hr) 20 〇3 濃度(mg/m3) 200 5.乾式氣體體積 (Vm(std),latm,0〇C) Nm3(dscm) 2.118 2.113 6_排氣含氧量(％) % 15.1 15.7 P10940022TW(本所案號 05P0450) 12 1310699 表三：戴奥辛處理效率Item Run2 Unit inlet σ 1. Volume m3/hr 110 2. Space velocity l/hr 5400 3. Operating temperature °C 120 4. 〇3 〇3 production amount (g/hr) 20 〇3 concentration (mg/m3) 200 5. Dry gas volume (Vm(std),latm,0〇C) Nm3(dscm) 2.118 2.113 6_Exhaust oxygen content (%) % 15.1 15.7 P10940022TW (Our Office No. 05P0450) 12 1310699 Table 3: Dioxin treatment efficiency
位置 實廠煙氣引出處 (實驗模廠入口處) (控制前） 實驗模廠出口處 (控制後） 戴奥辛去除效率 (%)Location Factory flue gas outlet (at the entrance of the experimental mold factory) (before control) Exit of the experimental mold factory (after control) Dioxin removal efficiency (%)
Runl Run2 1.527 0.520 0.039 0.075 97.4 85.6 綜上所述，本發明之方法所製作之臭氧/氧化鐵觸媒系 • 統，確實具有於低溫狀態（約1〇〇。〇150。(：）下分解戴奥辛 之特性。相較於先前技藝（參照表四），由於使用轉化能力 車父強、不會造成污染且反應溫度低之Fe〇〇H，除了能有效 將戴奥辛分解以外，還可節省能量並解決製程污染問題。 ^__查發明與先前技術之戴奧辛分解觸媒比較 技術類別 觸媒種類 反應器 形式 操作溫度 (°〇 技術來源 選擇性觸媒還原系統(SCR) V2O5/M0O3/T1 oxidant honeycomb >200 NIPPON SHOKUBAI Co., Ltd. Shell戴奥辛破壞系統(SDDS) Ti/V oxidant 侧流式反應 器 160-380 SHELL 觸媒分解濾袋 (REMEDIA® Catalytic Filtration Systems) V2〇5/W03/Ti〇2 濾袋 180-260 W. L. Gore & Associates, Inc., 本發明之臭氧/氧化鐵觸媒系 統 FeOOH 固定床 60-150 工研院 其他實施態樣 13 P1094〇022TW(本所案號 05P0450) 1310699 本發明之實施方法已詳述於前述實施例中，任何熟悉 本技術領域之人士皆可依本發明之說明，在不背離本發明 之精神與範圍内視需要更動、修飾本發明，因此，其他實 施態樣亦包含在本發明之申請專利範圍中。 雖然本發明已以較佳實施例揭露如上，然其並非用以 限定本發明，任何熟悉此技藝者，在不脫離本發明之精神 和範圍内，當可作各種之更動與潤飾，因此，本發明之保 •護範圍，當視後附之申請專利範圍所界定者為準。 •【圖式簡單說明】 第一圖係為本發明中臭氧/氧化鐵觸媒分解戴奥辛之反 應機制示意圖。 第二A圖係為本發明之分解戴奥辛裝置之一實施態樣 不意圖。 ' 第二B圖係為本發明之分解戴奥辛裝置之另一實施態 樣示意圖。 【主要元件符號對照說明】 Φ 1臭氧產生機 Γ臭氧產生機 2觸媒反應槽 2’觸媒反應槽 3引風機 3’引風機 4’廢氣進氣管線 10分解戴奥辛的裝置 10’分解戴奥辛的裝置 P10940022TW(本所案號 05P0450) 14Runl Run2 1.527 0.520 0.039 0.075 97.4 85.6 In summary, the ozone/iron oxide catalyst system produced by the method of the present invention does have a low temperature state (about 1 〇〇. 〇 150. (:) decomposition of dioxin Compared with the previous technology (refer to Table 4), due to the use of conversion ability, the parent is strong, does not cause pollution and the reaction temperature is low, Fe〇〇H, in addition to effectively decomposing dioxin, it can save energy and solve Process contamination problem. ^__Check invention and prior art dioxin decomposition catalyst comparison technology category catalyst type reactor form operating temperature (°〇 technology source selective catalyst reduction system (SCR) V2O5/M0O3/T1 oxidant honeycomb > 200 NIPPON SHOKUBAI Co., Ltd. Shell Dioxin Damage System (SDDS) Ti/V oxidant Sidestream Reactor 160-380 SHELL Catalytic Filtration Systems V2〇5/W03/Ti〇2 Filter Bag 180-260 WL Gore & Associates, Inc., Ozone/Iron Oxide Catalyst System FeOOH Fixed Bed 60-150 of the Invention Other Practices of the Institute of Technology 13 P1094〇022TW No. 05P0450) 1310699 The method of the present invention has been described in detail in the foregoing embodiments, and those skilled in the art can make modifications and modifications of the present invention as needed without departing from the spirit and scope of the invention. Therefore, other embodiments are also included in the scope of the present invention. Although the present invention has been disclosed in the above preferred embodiments, it is not intended to limit the invention, and In the spirit and scope, the various modifications and refinements can be made. Therefore, the scope of protection of the present invention is subject to the definition of the patent application scope. The schematic diagram of the reaction mechanism of the decomposition of dioxin by the ozone/iron oxide catalyst in the present invention. The second A diagram is not intended to be an embodiment of the decomposed dioxin device of the present invention. 'The second B diagram is the decomposition of the dioxin device of the present invention. Schematic diagram of another embodiment. [Main component symbol comparison description] Φ 1 ozone generator Γ ozone generator 2 catalyst reaction tank 2 'catalyst reaction tank 3 Machine 3 'primers fan 4' exhaust gas intake line 10 dioxin decomposition apparatus 10 'P10940022TW dioxin decomposition apparatus (the present Docket No. 05P0450) 14