201034742 六、發明說明： 【發明所屬之技術領域】 本發明係有關一種揮發性有機物之淨化回收裝置及方 法，尤指一種由回收設備進行第一階段之淨化處理，搭配 上進行第二階段淨化處理之轉輪式或轉環式濃縮器，甚至 是構成部份循環式淨化處理之設計者。 【先前技術】201034742 VI. Description of the Invention: [Technical Field] The present invention relates to a purification and recovery device and method for volatile organic compounds, and more particularly to a purification process of a first stage by a recycling device, and a second stage purification treatment The rotary or rotary concentrator is even the designer of a part of the circulating purification process. [Prior Art]
按，生活和生産中廣泛應用的有機溶劑，在室溫下易 揮發成氣體，故又名揮發性有機物（V〇latile 〇rganic Compounds，VOCs)，而多數的VOCs對人體有一定毒性，必 須加以處理；另，由環保署空氣品質監測資料顯示，v〇Cs 及NOx等臭氣前驅物質與光反應所產生的臭氧，有取代懸 浮微粒成為影響空氣污染指數（psi)的主要污染物的現 象，故加強管制VOCs排放乃是改善空氣品質的當務之急； 因此，環保署在過去幾年陸續研訂各行業別之職排放標 準（包括半導體、光電、汽車塗裝，皮革、勝帶…等產業） 來管制其污染賊，以及包括未來的其他傳統行業別（印 刷、塗裝...），也都將陸續訂定管制標準。 麻^按’環保署於九十六年一月一日，依據空氣污染防 “眷I七條第二項公告訂定「固定污染源空氣污染防制 率J’自九十六年-月一日起至九十八年十二月三 十-日止，揮發性有機物費率及計費方式如下表： 201034742 污 染 適用 物 費率 之公 種 私場 _類 所 揮 — 發 性 12 it*/ 排放 有 公斤 VOCs 機 者 物 備註 1.揮發性有機物(Volatile Organic Compounds，VOCs)係指 在1大氣壓下，測量所得初始沸點在攝氏250度以下有機化 合物之空氣污染物總稱。但不包括甲烷、一氧化碳、二氧化 ^、二硫化碳、碳酸、碳酸鹽、碳酸兹、氰化物、硫氰化物 ^化^物。以非甲烧碳氫化合物(NMHC)為計費基準。 Ο 而自九十九年一月一日起，揮發性有機物費率及計費 下表，其中，揮發性有機物總收費費額=揮發性有收費費額: ^ 率According to the widely used organic solvents in life and production, they are easily volatilized into gases at room temperature, so they are also known as V〇latile 〇rganic compounds (VOCs). Most VOCs are toxic to human body and must be In addition, the EPA's air quality monitoring data show that ozone generated by the reaction of odor precursors such as v〇Cs and NOx with light has replaced the suspended particles as a major pollutant affecting the air pollution index (psi). Therefore, strengthening the control of VOCs emissions is a top priority for improving air quality. Therefore, the EPA has been studying emission standards for various industries (including semiconductors, optoelectronics, automotive coatings, leather, winning belts, etc.) in the past few years. Controlling its polluting thieves, as well as other traditional industries (printing, painting, etc.), will also set regulatory standards. Ma ^ according to the 'EPD on January 1, 1996, based on the air pollution prevention ""I, the second bulletin of the seven articles, "fixed pollution source air pollution prevention rate J' from the 1996-Monday As of December 30, 1998, the VOC rates and billing methods are as follows: 201034742 The public interest rate of the applicable rate of pollution _ class is volatility 12 it* / emissions Volatile Organic Compounds (VOCs) are general term for air pollutants of organic compounds with an initial boiling point below 250 ° C measured at 1 atmosphere, but excluding methane, carbon monoxide, and Oxidation, carbon disulfide, carbonic acid, carbonate, carbonate, cyanide, thiocyanide, based on non-carbonated hydrocarbons (NMHC). Ο From January 1, 1999 From the table below, VOC rates and billing, where VOC total charges = volatility fees: ^ rate
〇 揮發性有機物 2〇元/ 公斤 25元/ 公斤 第一級： 季排放量扣除 起徵量後>49 公嘲 第二級： 6.5公嘲 < 季 排放量扣除起 徵量後各49公 噸 坨元/ 公斤 20元/ 公斤 個 物 種 窠三級 季排放量扣除 起徵量後g、 6.5公喝 .防制區等級係以臭氣 分級為基準。 2. 起徵量：每季一公噸 3. 揮發性有機物收費費 額=【（第一級排放量X 第一級費率）+(第二級 排放量X第二級费率）Η (第三級排放量X第三級 費率）】X優惠係數 (Α，）。 甲苯、二甲苯 元/公斤 排放揮發性 有機物中含 本項個別物 種者，加計 個別物種收費費額=個別 物種排放量X費率 -4- 201034742 笨、乙苯、苯乙烯、 二氣甲烷、1，1-二氯 乙烷、1，2二氣乙烷、 三氣甲燒（氣仿）、 1，1，1-三氣乙烧、四 氣化碳、三氣乙稀、 四氣乙烯 本項空氣污 染防制費 30 元/公斤 另’對於硫氳化物 污染物種 類〇Volatile Organic Compounds 2 / / kg 25 yuan / kg First Level: Seasonal emissions after deducting the levy >49 public ridicule second level: 6.5 public ridiculous < ** emissions minus 49 metric tons after the levy坨 yuan / kg 20 yuan / kg of species 窠 three seasons emissions after deducting the amount of levy g, 6.5 public drinking. The control zone level is based on odor classification. 2. Amount of levy: one metric ton per quarter 3. VOC charge = [(first level emissions X first rate) + (second level emissions X second rate) Η ( The third-level emission X third-rate rate)] X discount coefficient (Α,). Toluene, xylene/kg emissions of volatile organic compounds containing this individual species, plus individual species fees = individual species emissions X rate -4- 201034742 stupid, ethylbenzene, styrene, di-methane, 1 , 1-dichloroethane, 1,2 di-ethane, tri-gas (gas-like), 1,1,1-three-gas, four-carbonized, tri-ethylene, tetra-ethylene Air pollution control costs 30 yuan / kg and another 'for sulphur telluride pollutant types
適用之公私 場 所 元/公斤 8.5 元/公斤 氮氧化物費率及計費方式如下 備 註 Ο 硫氧化物 450 8元/公斤 元/公斤 第一級： 季排放量> 14公噸 第二級： 1公噸 <季 排放量$ 14 公噸 450 元/季 第三級： 季排放量S1 公噸 〇 氮氧化物 450 10元/公斤 7.5 第一級： 季排放量> 24公噸 第二級： 公峨 < 季 排放量客24 公噸 45〇 第三級： 季排放量彡 公噸 1. 硫氧化物、氮氧化物收 費費額=【（第一級排 放量X第一級費率）+ (第二級排放量X第二 級費率）+第三級費 額】X全廠優惠係數 ⑻。 2. 使用天然氣或其他經 中央主管機關認可之 低污染性氣體燃料 者，適用零費率。 3. 低污染性氣體燃料係 指符合下列二項條件 之氣體燃料： (1) 含四個碳原子以下 之碳氫化合物佔 總氣體體積百分 比百分之九十五 以上者。 (2) 每千立方公尺（攝 氏十五.五六度， 一大氣壓下）熱值 為六、六三五、〇 〇〇仟卡以上且 含硫量在百萬分 之五百以下者。 201034742 然而’以膠帶製造業為例，根據『膠帶製造業揮發性 有機物空氣污染管制及排放標準』第五條之規定：膠帶製 造業者應設置揮發性有機物污染防制設備，依規定將收集 之廢氣導入污染防制設備處理，且其揮發性有機物之處理 效率應達百分之九十以上始得排放；而有下列情形者，除 應符合前項規定外，其單一排放管道之揮發性有機物排放 量不得大於每小時三•八公斤；一、新設製程；二、全廠 〇 含揮發性有機物原（物）料年許可用量達四百公噸以上者。 因此，若處理效率以VOCs產生量為200kg/hr而言，防制 設備處理效率（消減率）須>98.1%，並非>90%。 此外，由於過去產業的快速發展與著重於削減率的環 保政策，造成產業在處理VOCs時，並未著重資源回收再利 用’而是以燃燒處理為主（焚化爐之處理效率約g〇〜gg %)，卻常伴隨產生大量的二次污染物（如氮氧化物及其他 有害之氧化物）；於是，隨著揮發性有機物之排放規定曰趨 ο 嚴格’除了考量處理效率以及二次污染物之外，另因原物 料價格不斷上漲’故採用活性碳吸脫附回收設備，將有機 溶劑回收之應用例將越來越普遍；而常見之活性碳吸脫附 回收設備，其特性比較如下表，可見其處理效率並無法滿 足現階段之環保要求; 固定床式 回收設備 流動床式 回收設備 碳纖維筒 回收設備 吸附材料 粒狀活性碳 球狀活性碳 織維狀活性 碳 吸附方式 填充層 空中浮游式 圓筒形單體 201034742 (固定床式） (固定床式） 脫附媒體 蒸汽（大量） 氮氣（少量） 蒸汽（中量） 脫附溫度（°c) 80 〜100 150〜Ϊ60 100〜110 吸脫循環時間（分鐘） 60 〜120 30 〜60 10 〜12 處理效率（％) 80 〜95 50 〜95 80 〜95 回收品中酸分（分解 物） 高 低 低 分離水量（廢水）kg水 /kg溶劑 1〜7 0〜0. 2(原廢氣 中濕分凝結） 1〜5 因此，由前述之VOCs處理設備而言，無論是回收後燃 燒處理之焚化爐，或是回收後凝結再利用之固定床式回收 設備、流動床式回收設備以及碳纖維筒回收設備，都逐漸 難以滿足日後之VOCs排放規定。 【發明内容】 本發明之主要目的’係欲提供一種揮發性有機物之淨 化回收裝置，而具有確保最終所排放氣體濃度符合規定之 功效。 本發明之另一目的，則具有大幅提高揮發性有機物回 收再利用且降低二次污染物產生之功效。 本發明之又一目的，乃具有設備簡單之功效。 為達上述功效，本發明之結構特徵，係包括有： 一回收設備，由設置於抽氣管之風機，將待淨化氣體 送入吸脫附單元予以濃縮淨化處理，符合排放標準之淨化 氣體由排放管排出，濃縮氣體藉回收管送入終處理單元進 行回收處理；以及 一濃縮器，至少被區隔成一吸附區及一再生區，而將 連接於吸附區入口側之吸附進氣管，叉接於該吸脫附單元 之排放管，讓經該回收設備淨化但未符合排放標準之一次 201034742 濃縮氣體於吸附區再度淨化，再度淨化氣體由連接於吸附 區出口側之吸附排氣管排出，而再生區入口侧連接有脫附 進氣管，另把連接於再生區出口侧之脫附排氣管，又接於 該風機上游之抽氣管，將自再生區脫附之揮發性有機物氣 體送回該回收設備者。 此外，該脫附進氣管設置有脫附加熱器與脫附氣源， 且進一步令該吸附排氣管或進氣管以叉管又接於該脫附加 熱器上游之脫附進氣管，並可加設有： 一控制器’藉由设置於該抽氣管之第一濃度偵測器、 設置於該排放管之第二濃度偵測器與設置於該吸附排氣管 之第二濃度伯測器，摘測淨化前後之揮發性有機物濃度， 而根據所偵測到之濃度訊號及排放標準，控制設置於該排 放管之第一控制閥與設置於該吸附進氣管之第二控制閥之 比例開度，俾以確保由回收設備或濃縮器排出之淨化氣體 符合排放標準。 大再者，該吸脫附單元為固定床式、流動床式或碳纖維 筒式，而該吸脫附單元之吸附材為活性碳、沸石、矽膠、 碳分子篩、多孔性樹脂或活性氧化鋁；該終處理單元為冷 凝器或焚化爐；該濃縮器為轉輪式或轉環式濃縮器；該濃 縮器吸附材為浠石、卿、活性碳、碳分子_、多孔性樹 脂或活性氧化銘；該濃、縮器進—步於再生區與吸附區間增 設-隔離區；該濃縮器濃縮倍率較佳為5〜刚倍，最佳為 8〜20倍；該脫附排氣管進—步可設置有脫附風機。 另外’本發明之方法特徵，係包括下列步驟： a.利用回收設備將揮發性有機物濃縮淨化，並進行回 201034742 收處理； b.债測回收設備淨化前後 觥签π-τα -會命> *愧 貫丨有機物濃度，而判 斷淨化前後纽之處理效率是否符合排放標準，_ 進至步驟e，若否，則進行下一步驟； 右疋則 c.將經回收設備濃縮後之揮發性有機物全部或依比 ===縮器，用濃縮器將揮發性有機物再度 Ο 〇 d·將經漠縮器濃縮後之揮發性有機物部份導引至回 收設備入口側㈣並進行步驟a，而構成部㈣ 處理； e.將符合排放標準之淨化氣體排放。 另者，步驟c可進一步增加下列程序： 伯測濃縮器及回收設備淨化前後之揮發性有機物濃 度，而判斷淨化前後濃度之總處理效率是否符合排放標 準’若是’義至步驟e ’❹’壯大分流至濃縮器之風 量比例，直到總處理效率符合排放標準。 【實施方式】 首先，請參閱第-、二圖所示，本發明之淨化回收裝 置係包括有： 一回收設備（10)，由設置於抽氣管（11)之風機（12)， 將含有揮發性有機物之待淨化氣體，送入吸脫附單元（13) 予以濃縮淨化處理，符合排放標準之淨化氣體由排放管（14) 排出，濃縮之揮發性有機物氣體藉回收管（15)，送入冷凝 器或焚化爐之終處理單元（16)進行回收處理；其中，該吸 201034742 脫附單元（13)為固定床式、流動床式或碳纖維筒式（圖示以 流動床式代表），而其吸附材為活性碳、沸石、矽膠、碳分 子篩、多孔性樹脂或活性氧化鋁；以及 一轉輪式或轉環式濃縮器（2〇a或20b) ’其吸附材為沸 石、矽膠、活性碳、碳分子篩、多孔性樹脂或活性氧化鋁， 利用風量變小濃度變高之濃縮效果，將揮發性有機物氣體 予以濃縮，而區隔成至少一吸附區（21)及一再生區（22)， 亦可於再生區（22)與吸附區（21)之間增設一隔離區（圖未 示），並將連接於吸附區（21)入口側之吸附進氣管（23)，叉 接於該吸脫附單元（13)之排放管（14)，讓經該回收設備（10) 淨化但未符合排放標準之一次濃縮氣體於吸附區（21)再度 淨化，再度淨化氣體由連接於吸附區（21)出口側之吸附排 氣管（24)排出，而再生區（22)入口側連接有脫附進氣管 (25)，另把連接於再生區（22)出口側之脫附排氣管（26)， 叉接於該風機（12)上游之抽氣管（11)，將自再生區（22)脫 附之揮發性有機物氣體送回該回收設備（10);其中，該脫 附進氣管（25)設置有脫附加熱器（27)與脫附氣源（28)，而 該吸附排氣管（24)或吸附進氣管（23)得以叉管（241)叉接 於該脫附加熱器（27)上游之脫附進氣營（25)，可用以取代 脫附氣源（28)且形成部份循環管路，該脫附排氣管（26)得 設置有脫附風機（29)者。 此外’揮發性有機物之排放規定’除了排放濃度外， 有時亦根據排放口之有機物質量流率（另稱總排放量），或 是排放消減率來規範’而不同之製造業別也有不同之規 定；於是，為了精準控制揮發性有機物之處理效能，俾以 -10- 201034742 符合揮發性有機物之排放規定，本發明之淨化回收裝置進 一步包括有： 一控制器（30)，藉由設置於該抽氣管（11)之第一濃度 偵測器（31)、設置於該排放管（14)之第二濃度偵測器（32) 與設置於該吸附排氣管（24)之第三濃度偵測器（33)，偵測 淨化前後之揮發性有機物濃度，而根據所偵測到之濃度訊 號及排放標準，控制設置於該排放管（14)之第一控制閥（34) 與設置於該吸附進氣管（23)之第二控制閥（35)之比例開 度，俾以確保由回收設備（10)或濃縮器（20)排出之淨化氣 體符合排放標準；其中，以循環淨化之實施例說明控制閥 之比例開度，當該排放管（14)之揮發性有機物濃度未達排 放標準，第一控制閥（34)關閉且第二控制閥（35)開啟，讓 經該回收設備（10)淨化之氣體，再藉由該濃縮器（20a或20b) 二度淨化，並自該吸附排氣管（24)排放，又若設置有叉管 (241)，則可進一步迫使部份二度淨化後之氣體經由該叉管 (241)、脫附進氣管（25)與脫附排氣管（26)，回到該回收設 備（10)而循環淨化。 此外，該轉輪式或轉環式濃縮器（2〇a或20b)之吸附氣 流與脫附氣流，其氣流方向不限定為逆向流或順向流；其 中第一圖為逆向流（吸附氣流與脫附氣流之流向相反），第 二圖為順向流（吸附氣流與脫附氣流均自環外流向環内）之 示意。 基於如是之構成，本發明之淨化回收裝置，係將含有 揮發性有機物之待淨化氣體，先藉該回收設備（10)進行第 一階段之淨化處理，再由濃縮器（20a或20b)進行第二階段 -11 - 201034742 之淨化處理，而舉出三個實施例與先前技術單一階段之淨 化處理比較，其操作結果如下表所示： 第一階段淨 化處理效率 V 1 第二階段淨 化處理效率 V2 總淨化處 理效率 τ?3 二次污染物衍 生 系統 穩定 度 比較例一 流動床式活性 碳吸脫附裝置 50-95% (不穩定） 無 50-95% (不穩定） 少 效率 不穩 定 比較例二 焚化爐 90-99% (不穩定） 無 90-99% (不穩定） Nox、Sox、氣 化物等二次污 染物衍生 過溫 跳機 機率 大 實施例一 流動床式活性 碳吸脫附裝置 搭配轉環式濃 縮器 50-95% (不穩定） 95-99% (穩定） 95-99% (穩定） 少 效率 高且 穩定 實施例二 流動床式活性 碳吸脫附裝置 搭配轉輪式濃 縮器 50-95% (不穩定） 95-99% (穩定） 95-99% (穩定） 少 效率 高且 穩定 實施例三 固定床式活性 碳吸脫附裝置 搭配轉輪式濃 縮器 80-95% (尚穩定） 95-99% (穩定） 97-99% (穩定） 適中 (廢水） 效率 高且 穩定 7?1 =(第一濃度一第二濃度)/第一濃度 ??2 =(第二濃度一第三濃度)/第二濃度 η 3= η ! + (!00%— η\)/ η 2 是以，本發明係由回收設備（10)進行第一階段之淨化 處理，搭配上進行第二階段淨化處理之轉輪式或轉環式濃 -12- 201034742 縮器（20a或20b)，甚至是構成循環式之淨化處理；因此， 具有不必採用複雜之處理設備，即得以確保最終所排放之 氣體符合規定，且將揮發性有機物回收再利用之功效。 綜上所述，本發明所揭示之技術手段，確具「新穎性」、 「進步性」及「可供產業利用」等發明專利要件，祈請鈞 局惠賜專利，以勵發明，無任德感。 惟，上述所揭露之圖式、說明，僅為本發明之較佳實 施例，大凡熟悉此項技藝人士，依本案精神範疇所作之修 飾或等效變化，仍應包括本案申請專利範圍内。Applicable public and private places/kg 8.5 yuan/kg NOx rate and billing method as follows Remarks Ο Sulfur oxides 450 8 yuan / kg yuan / kg First level: Seasonal emissions > 14 metric tons Second level: 1 Metric tons <quarter emissions: $14 metric tons 450 yuan/quarter third level: Quarterly emissions S1 metric tons 〇NOx 450450 10 yuan/kg 7.5 First level: Seasonal emissions> 24 metric tons Level 2: 峨<lt Seasonal emissions of 24 metric tons 45 〇 Level 3: Seasonal emissions 彡 metric tons 1. Sulfur oxides, nitrogen oxides charge fees = [(first level emissions X first rate) + (second level Emissions X second rate) + third level fee] X factory discount factor (8). 2. For use with natural gas or other low-pollution gas fuels approved by the central authority, zero rates apply. 3. Low-pollution gas fuels are gas fuels that meet the following two conditions: (1) Hydrocarbons containing less than four carbon atoms account for more than 95% of the total gas volume. (2) For every thousand cubic meters (15.56 degrees Celsius, at atmospheric pressure), the calorific value is six, six, three, five, and more than five hundredths of a million sulphur. 201034742 However, taking the tape manufacturing industry as an example, according to Article 5 of the “Volatile Organic Compounds Air Pollution Control and Emission Standards for Tape Manufacturing Industry”: tape manufacturers should set up volatile organic pollutant pollution control equipment and collect the exhaust gas according to regulations. Introduced into the pollution prevention equipment, and the treatment efficiency of volatile organic compounds should be more than 90%. In the following cases, in addition to the provisions of the preceding paragraph, the volatile organic emissions of the single discharge pipeline It shall not be more than three or eight kilograms per hour; first, a new process; second, the whole plant shall contain more than 400 metric tons of volatile organic compounds (materials). Therefore, if the treatment efficiency is 200 kg/hr in terms of the amount of VOCs produced, the treatment efficiency (rate reduction rate) of the control equipment must be >98.1%, not >90%. In addition, due to the rapid development of the industry in the past and the environmental protection policy focusing on the reduction rate, the industry did not focus on resource recycling when dealing with VOCs, but mainly based on combustion treatment (the efficiency of incinerator treatment is about g〇~gg %), but often accompanied by the production of a large number of secondary pollutants (such as nitrogen oxides and other harmful oxides); therefore, with the emission regulations of volatile organic compounds, rigorously 'except for consideration of treatment efficiency and secondary pollutants In addition, due to the rising price of raw materials, the use of activated carbon adsorption and desorption equipment, the application of organic solvent recovery will become more and more common; and the common activated carbon adsorption and desorption equipment, its characteristics are compared as follows, It can be seen that the processing efficiency can not meet the current environmental protection requirements; Fixed bed type recycling equipment, fluidized bed type recycling equipment, carbon fiber tube recycling equipment, adsorbent material, granular activated carbon, spherical activated carbon, woven viable, activated carbon, adsorption method, filled layer, floating float Tubular monomer 201034742 (fixed bed type) (fixed bed type) desorption medium steam (large amount) nitrogen (small amount) ) Steam (medium amount) Desorption temperature (°c) 80 to 100 150~Ϊ60 100~110 Suction and removal cycle time (minutes) 60 to 120 30 to 60 10 to 12 Treatment efficiency (%) 80 to 95 50 to 95 80 ~95 Recycled acid (decomposition) High and low separation water volume (waste water) kg water / kg solvent 1~7 0~0. 2 (the original exhaust gas moisture condensation) 1~5 Therefore, the aforementioned VOCs processing equipment In terms of incinerators after recycling, or fixed bed recycling equipment, fluidized bed recycling equipment, and carbon fiber cylinder recycling equipment after recycling, it is difficult to meet future VOC emission regulations. SUMMARY OF THE INVENTION The main object of the present invention is to provide a purification apparatus for volatile organic compounds, which has the effect of ensuring that the concentration of the finally discharged gas is in compliance with the regulations. Another object of the present invention is to greatly improve the recovery and reuse of volatile organic compounds and to reduce the effects of secondary pollutants. Another object of the present invention is to have a simple device. In order to achieve the above-mentioned effects, the structural features of the present invention include: a recycling device, which is sent to the suction and desorption unit by a fan disposed in the exhaust pipe to be concentrated and purified, and the purified gas complying with the discharge standard is discharged. The tube is discharged, and the concentrated gas is sent to the final processing unit for recovery by the recovery tube; and a concentrator is at least divided into an adsorption zone and a regeneration zone, and the adsorption inlet pipe connected to the inlet side of the adsorption zone is forked. The discharge pipe of the suction and desorption unit allows the 201034742 concentrated gas purified by the recovery device but does not meet the discharge standard to be purified again in the adsorption zone, and the purified gas is discharged by the adsorption exhaust pipe connected to the outlet side of the adsorption zone. A desorption inlet pipe is connected to the inlet side of the regeneration zone, and a desorption exhaust pipe connected to the outlet side of the regeneration zone is connected to an exhaust pipe upstream of the fan to return the volatile organic matter gas desorbed from the regeneration zone. The recycling equipment. In addition, the desorption intake pipe is provided with a desorption heater and a desorption air source, and further, the adsorption exhaust pipe or the intake pipe is further connected to the desorption air inlet pipe upstream of the desorption heater by a fork pipe. And a controller: a first concentration detector disposed on the exhaust pipe, a second concentration detector disposed on the discharge pipe, and a second concentration disposed on the adsorption exhaust pipe a detector for measuring the concentration of volatile organic compounds before and after purification, and controlling a first control valve disposed on the discharge pipe and a second control disposed on the adsorption intake pipe according to the detected concentration signal and emission standard The proportional opening of the valve is to ensure that the purge gas discharged from the recovery equipment or concentrator meets the emission standards. In addition, the suction and desorption unit is a fixed bed type, a fluidized bed type or a carbon fiber cylinder type, and the adsorbing material of the suction and desorption unit is activated carbon, zeolite, tannin, carbon molecular sieve, porous resin or activated alumina; The final treatment unit is a condenser or an incinerator; the concentrator is a rotary or rotary concentrator; the concentrator adsorbent is vermiculite, qing, activated carbon, carbon molecule _, porous resin or active oxidation The thickening and shrinking device is stepped in the regeneration zone and the adsorption zone is added-isolated zone; the concentration ratio of the concentrator is preferably 5 to just double, preferably 8 to 20 times; the desorption exhaust pipe is further advanced A desorption fan can be provided. In addition, the method features of the present invention include the following steps: a. using a recycling device to concentrate and purify volatile organic compounds, and returning to 201034742 for processing; b. testing and recycling equipment for purification before and after purification of π-τα-fighting > * 愧 丨 丨 organic matter concentration, and determine whether the treatment efficiency before and after purification meets the emission standards, _ proceed to step e, if not, proceed to the next step; right 疋 c. All or the ratio === reducer, the volatile organic substance is again 用 用 · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · Department (4) Disposal; e. Emissions of purified gas that meets emission standards. In addition, step c can further increase the following procedures: The concentration of volatile organic compounds before and after purification by the concentrator and the recovery equipment, and whether the total processing efficiency of the concentration before and after purification meets the emission standard 'if yes' to the step e '❹' The proportion of air flow diverted to the concentrator until the total treatment efficiency meets the emission standards. [Embodiment] First, as shown in the first and second figures, the purification and recovery apparatus of the present invention includes: a recovery device (10), which is provided by a fan (12) disposed in the exhaust pipe (11), and contains a volatilization The gas to be purified of the organic matter is sent to the suction and desorption unit (13) for concentration and purification treatment, and the purified gas complying with the discharge standard is discharged from the discharge pipe (14), and the concentrated volatile organic gas is fed through the recovery pipe (15). The final treatment unit (16) of the condenser or incinerator is subjected to recovery treatment; wherein the suction 201034742 desorption unit (13) is a fixed bed type, a fluidized bed type or a carbon fiber cylinder type (represented by a fluidized bed type), and The adsorbent material is activated carbon, zeolite, tannin, carbon molecular sieve, porous resin or activated alumina; and a rotary or rotary concentrator (2〇a or 20b) 'the adsorbent is zeolite, tannin, active Carbon, carbon molecular sieve, porous resin or activated alumina, the volatile organic gas is concentrated by using a concentration effect in which the air volume becomes smaller, and is partitioned into at least one adsorption zone (21) and a regeneration zone (22). ), an isolation zone (not shown) may be added between the regeneration zone (22) and the adsorption zone (21), and the adsorption intake pipe (23) connected to the inlet side of the adsorption zone (21) may be forked. The discharge pipe (14) of the suction and removal unit (13) allows the primary concentrated gas purified by the recovery device (10) but does not meet the discharge standard to be re-purified in the adsorption zone (21), and the purified gas is connected to the adsorption again. The adsorption exhaust pipe (24) on the outlet side of the zone (21) is discharged, and the desorption inlet pipe (25) is connected to the inlet side of the regeneration zone (22), and the desorption row connected to the outlet side of the regeneration zone (22) is additionally connected. a gas pipe (26), which is forked to an exhaust pipe (11) upstream of the fan (12), and returns volatile organic compounds desorbed from the regeneration zone (22) to the recovery device (10); wherein the desorption The intake pipe (25) is provided with a desorption heater (27) and a desorption air source (28), and the adsorption exhaust pipe (24) or the adsorption intake pipe (23) is forked by the fork pipe (241) The desorption air inlet (25) upstream of the desorption heater (27) can be used instead of the desorption air source (28) and form a partial circulation line, and the desorption exhaust pipe (26) is provided with Attaching the fan (29) persons. In addition to the emission concentration of volatile organic compounds, in addition to the emission concentration, it is sometimes regulated according to the organic matter mass flow rate (also known as total emissions) or the emission reduction rate of the discharge port, and the manufacturing industries are different. Therefore, in order to accurately control the treatment efficiency of the volatile organic compounds, the purification recovery device of the present invention further includes: a controller (30), provided by the a first concentration detector (31) of the exhaust pipe (11), a second concentration detector (32) disposed in the discharge pipe (14), and a third concentration detection disposed on the adsorption exhaust pipe (24) a detector (33) for detecting a concentration of volatile organic compounds before and after purification, and controlling a first control valve (34) disposed on the discharge pipe (14) according to the detected concentration signal and emission standard The proportional opening degree of the second control valve (35) of the intake pipe (23) is adsorbed to ensure that the purge gas discharged from the recovery device (10) or the concentrator (20) meets the discharge standard; wherein, the implementation of the cycle purification Example description Control valve proportional opening, when the concentration of volatile organic compounds in the discharge pipe (14) does not reach the discharge standard, the first control valve (34) is closed and the second control valve (35) is opened, allowing the recovery device (10) The purified gas is secondarily purified by the concentrator (20a or 20b) and discharged from the adsorption exhaust pipe (24), and if a fork pipe (241) is provided, the partial second purification can be further forced. The latter gas is circulated and purified by returning to the recovery device (10) via the fork pipe (241), the desorption intake pipe (25), and the desorption exhaust pipe (26). In addition, the adsorption gas flow and the desorption gas flow of the rotary or rotary concentrator (2〇a or 20b) are not limited to a reverse flow or a forward flow; wherein the first figure is a reverse flow (adsorption flow) The opposite is to the flow of the desorbed gas stream. The second plot is a schematic representation of the forward flow (both adsorption and desorption flows from the outer ring to the inner ring). Based on the configuration, the purification and recovery device of the present invention firstly purifies the gas to be purified containing volatile organic compounds, and first performs the purification treatment of the first stage by the recovery device (10), and then performs the first step by the concentrator (20a or 20b). The purification treatment of the two stages -11 - 201034742, and the three examples compared with the purification process of the prior art single stage, the operation results are shown in the following table: The first stage purification treatment efficiency V 1 The second stage purification treatment efficiency V2 Total purification treatment efficiency τ?3 Secondary pollutant derivation system stability comparison Example 1 Flow bed type activated carbon adsorption and desorption device 50-95% (unstable) No 50-95% (unstable) Less efficiency instability Comparative example Second incinerator 90-99% (unstable) No 90-99% (unstable) Nox, Sox, vapor and other secondary pollutants derived from the temperature jump machine. Example 1 Flow bed type activated carbon adsorption and desorption device 50-95% with a rotary concentrator (unstable) 95-99% (stable) 95-99% (stable) Less efficient and stable Example 2 Flow-bed activated carbon suction and desorption device with a wheel-type thick 50-95% (unstable) 95-99% (stable) 95-99% (stable) less efficient and stable Example 3 fixed bed activated carbon adsorption and desorption device with rotary concentrator 80-95% (Stilled) 95-99% (stable) 97-99% (stable) Moderate (waste water) High efficiency and stable 7?1 = (first concentration - second concentration) / first concentration ?? 2 = (second Concentration - third concentration) / second concentration η 3 = η ! + (!00% - η\) / η 2 Therefore, the present invention is carried out by the recycling device (10) for the first stage of purification treatment The second-stage purification treatment of the rotary or rotary ring -12-201034742 reducer (20a or 20b), even constitutes a circular purification treatment; therefore, without having to use complex processing equipment, that is to ensure the final The emitted gas meets the requirements and the effect of recycling volatile organic compounds. In summary, the technical means disclosed in the present invention have the invention patents such as "novelty", "progressiveness" and "available for industrial use", and pray for the patent to be invented by the bureau. German sense. The drawings and descriptions disclosed above are only preferred embodiments of the present invention, and those skilled in the art, which are subject to the spirit of the present invention, should be included in the scope of the patent application.
-13- 201034742 【圖式簡單說明】 第一圖係本發明採用轉輪式濃縮器之結構說明圖。 第二圖係本發明採用轉環式濃縮器之結構說明圖。-13- 201034742 [Simplified description of the drawings] The first figure is a structural explanatory diagram of the invention using a rotary concentrator. The second drawing is a structural explanatory diagram of the present invention using a rotary ring concentrator.
【主要元件符號說明】 (10) 回收設備 (11) 抽氣管 (12) 風機 (13) 吸脫附單元 (14) 排放管 (15) 回收管 (16) 終處理單元 (20a、20b)濃縮器 (21) 吸附區 (22) 再生區 (23) 吸附進氣管 (24) 吸附排氣管 (241)叉管 (25) 脫附進氣管 (26) 脫附排氣管 (27) 脫附加熱器 (28) 脫附氣源 (29) 脫附風機 (30) 控制器 (31) 第一濃度偵測器 (32) 第二濃度偵測器 (33) 第三濃度偵測器 (34) 第一控制閥 (35) 第二控制閥 -14-[Explanation of main component symbols] (10) Recycling equipment (11) Exhaust pipe (12) Fan (13) Suction and removal unit (14) Discharge pipe (15) Recovery pipe (16) Final treatment unit (20a, 20b) concentrator (21) Adsorption zone (22) Regeneration zone (23) Adsorption intake pipe (24) Adsorption exhaust pipe (241) Fork pipe (25) Desorption intake pipe (26) Desorption exhaust pipe (27) De-attachment Heater (28) Desorbed air source (29) Desorber (30) Controller (31) First concentration detector (32) Second concentration detector (33) Third concentration detector (34) First control valve (35) second control valve -14-