201103622 六、發明說明： 【發明所屬之技術領域】 本發明關於一種吸收空氣中二氧化碳之裝置，尤指一種利 用一全新設計旋轉填充床取代傳統填充塔，以進行化學吸收法 回收二氧化碳之裝置。 【先前技術】 >凰至氣體造成全球暖化的問題日益嚴重，溫室氣體之中以 二氧化碳（c〇2)的含量最多，佔有最大比例，約為55%，對 於溫室氣體的減量控制與處理技術的研發，儼然已成為世界趨 勢。因此，如何有效率的吸收空氣中的二氧化碳，為本發明主 要討論之主題。 目前已有化學吸收法來回收二氧化碳。而化學吸收法是以 吸收劑與一氧化碳發生化學反應來達到回收二氧化碳的目 的，並且利用其逆反應進行吸收劑再生。 化學吸收法為目前最有效率的回收二氧化碳方法，其能獲 得較高的二氧化碳去除率，且適合於處理二氧化碳分壓低的混 合氣體。此法可得到純度較高的二氧化碳，並且吸收速度快、 可處理較大量的氣體。 但是化學吸收法缺點有以下三點：丨.溶劑與其他氣體(如 〇2、S〇x或COS)發生不可逆的化學反應，使吸收劑之再生次 數減少，因而增加操作成本；2·由於吸收劑多為鹼性溶液，會 對吸收塔、再生塔及周邊管線造成腐蝕作用；3操作變數較 多，因此操作較為繁瑣。 在現有成熟的技術中’ 一般使用傳統填充塔進行二氧化碳 201103622 的吸收。在此傳統填充塔中，若欲增加吸收效率，通常都需要 龐大的設備或增加吸收劑量才能達到需求，這將使得成 提高，不符合經濟效益，不利市場的競爭。 不馮 在現有的技術中，於西元1981年，自從英國ICI公司之 Ramshaw與Mallinson成功地開發高效率氣液質傳技術以來， 引起工業界的密切關注。他們所開發之設備常被稱為旋轉填充 床(Rotating Packed Bed) ’其主要是利用高速旋轉的填充床産生 強大的離心力（或超重力），大幅地提高氣液之相對流速及填充 ^效比，面積’液體在高分散、強滿動以及界面急速更新的 情況下與氣體以極高的相對速度在彎曲流道中接觸，極大地強❿ 化氣液質傳效率。 此新賴技術具有低液泛、高處理量、較小空間需求、高質 傳效率、低能源耗用及低投資與操作成本等優點。此技術可廣 ^地應用於論、魏、氣提及具㈣散控獅氣液反應等程 ，，所以不僅能適用於化學工業，更能應用於其他產業相關之 程序如環保產業等。 式旋充床分為兩種類型，即逆流式旋轉填充床和錯流 逆流式旋轉填充床，如第一圖所示，係在一封閉的外殼9 —側面設有-氣體入口 9 2、頂面+心設有—氣體出口 9 3及 2體入σ 9 4、且底面設有-液體出口 9 5;外殼91内設 二以轉軸9 6趨動旋轉的轉筒97，哺筒9 7以填充物9 8填充。 =體自液體入口 9 4經管線末端的液體分佈器9 9而送 入轉筒9 7的中心；氣體自氣體入口9 2經填充物9 8而進入 4 201103622 轉筒9 7之中心。使液體與氣體在轉筒9 7之 化學吸收程序。 此種逆流式旋轉填充床的内外環流體通道，由於截面積差 、大以致氣體速度變化過大，如此將使氣體所受阻力提升， 不適合用於氣體流量高之氣液質傳交換程序如吸收等。 爲了在氣體流量高的氣液質傳交換程序中引入離心力場 ^化質傳，一些研究者開始研發不同於逆流式的錯流式旋轉填 床，其結構如第二圖所示，其係在一密封的外殼8丄底面設 有多個氣體入口 8 2及一液體出口 8 3，而頂面中心設有一氣 2出口 8 4及一液體入口 8 5 ;而外殼8 1内設有一以轉軸8 趨動％轉的填充物8 7，而填充物8 7上方設有一氣體封轴 8 8 〇 液體自液體入口 8 5經管線末端的液體分佈器8 9而送 入填充物8 7的中心；氣體自氣體入口 8 2經填充物8 7而進 入中心。使液體與氣體在填充物8 7之中心交匯以進行化學吸 收程序。 、 錯流式旋轉填充床中由於氣體流道截面積固定，因此氣體 ，度恒定’且氣體沿旋轉床軸向流動，無需克服離心阻力，故 氣體阻力遠比於逆流式小，適合氣體流量高之氣液接觸程序， 且可改善目前常使用洗滌塔壓損過高之缺點，如此可大幅地減 少操作過程中所使用之能源耗用。 >若能妥善利用此二種旋轉填充床設備的優點，將其應用於 空氣中二氧化碳的吸收，可大幅增加吸收效率。 【發明内容】 201103622 緣此’本發明主要目的係提供了一種空氣中二氧化碳吸收 裝置，主要利用此全新設計的旋轉填充床取代傳統填充塔進行 化學吸收法以回收二氧化碳。 本發明所提供的一種空氣中二氧化碳吸收裝置，主要係由 一全新設計旋轉填充床、空氣泵、一吸收劑儲槽及一抽水泵所 構成。此旋轉填充床具有一密封外殼’該外殼上設有一空氣入 口及一吸收劑出口，且頂面中心設有一空氣出口及一吸收劑入 口’而内部設有一以一馬達帶高速旋轉之填充物，而該填充物 中心設有一與該吸收劑入口連通的液體分佈器。空氣泵將空氣 自該空氣入口打入外殼内。吸收劑儲槽則用以儲存自該吸收劑 出口流出的吸收劑。抽水泵將吸收劑儲槽中的吸收劑自吸收劑 入口打入外殼内。吸收劑自吸收劑入口經管線末端的液體分佈 器而送入填充物的中心；而空氣自空氣入口經填充物而進入中 心；吸收劑經高速旋轉於100G以上的超重場受離心力喷射而 出與空氣中的二氧化碳於填充物之中心交匯，以進行化學吸收 程序，將空氣中的二氧化碳吸收，並使剩餘氣體自空氣出口排 出，而吸收二氧化碳之吸收劑回收至吸收劑儲槽中。 藉由本發明所提供的一種空氣中二氧化碳吸收裝置，利用 此旋轉填充床進行化學吸收程序，將可以縮減設備大小，降低 傳統填充塔内吸收劑輸送至塔頂所需能源；而利用此旋轉填充 床之耗能減量，使其在應用上更具競爭力，進而大幅地降低成 本’故以經濟觀點來看，此旋轉填充床將會是高效率的二氧化 碳去除設備。 以下將依據圖式所示，詳細說明本發明之結構特點及使用 功效。 【實施方式】 201103622 請參照第三圖所示，本發明係提供一種空氣中二氧化碳吸 收之裝置’主要係由一旋轉填充床1、空氣泵2、一吸收劑儲 槽3及一抽水泵4所構成。 &本發明的旋轉填充床1具有一密封外殼11，該外殼1 1 上设有一空氣入口 1 2及一吸收劑出口 1 3，且頂面中心設有 空氣出口 1 4及一吸收劑入口 1 5，而内部設有一以一馬達 j 6帶高速旋轉之填充物1 7，而該填充物1 7中心設有一與 該吸收劑入口15連通的液體分佈器18。 空氣泵2將空氣自該空氣入口12打入外殼11内。吸收 劑儲槽3則用以儲存自該吸收劑出口13流出的吸收劑。抽水 栗4將吸收劑儲槽3中的吸收劑自吸收劑入口15打入外殼 1 1内。201103622 VI. Description of the Invention: [Technical Field] The present invention relates to a device for absorbing carbon dioxide in air, and more particularly to a device for recycling carbon dioxide by a chemical absorption method by replacing a conventional packed column with a newly designed rotary packed bed. [Prior Art] > The problem of global warming caused by phoenix to gas is becoming more and more serious. The content of carbon dioxide (c〇2) in greenhouse gases is the largest, accounting for the largest proportion, about 55%, for the control and treatment of greenhouse gas reduction. The research and development of technology has become a world trend. Therefore, how to efficiently absorb carbon dioxide in the air is the subject of the main discussion of the present invention. There are currently chemical absorption methods to recover carbon dioxide. The chemical absorption method is a chemical reaction of an absorbent with carbon monoxide to achieve the purpose of recovering carbon dioxide, and the reverse reaction is used for regeneration of the absorbent. The chemical absorption method is currently the most efficient method for recovering carbon dioxide, which can achieve a high carbon dioxide removal rate and is suitable for treating a mixed gas having a low partial pressure of carbon dioxide. This method can obtain high purity carbon dioxide, and the absorption speed is fast, and a relatively large amount of gas can be processed. However, the chemical absorption method has the following three disadvantages: 丨. The solvent undergoes an irreversible chemical reaction with other gases (such as 〇2, S〇x or COS), which reduces the number of regenerations of the absorbent, thereby increasing the operating cost; Most of the agents are alkaline solutions, which will cause corrosion to the absorption tower, the regeneration tower and the surrounding pipelines; 3 the operation variables are more, so the operation is more complicated. In the existing mature technology, the absorption of carbon dioxide 201103622 is generally carried out using a conventional packed tower. In this conventional packed tower, if the absorption efficiency is to be increased, it usually requires a large amount of equipment or an increased absorbed dose to meet the demand, which will result in an increase, which is not economical and unfavorable for market competition. In the existing technology, in 1981, since the British ICI company Ramshaw and Mallinson successfully developed high-efficiency gas-liquid mass transfer technology, it has attracted close attention from the industry. The equipment they developed is often referred to as the Rotating Packed Bed. It uses a high-speed rotating packed bed to generate powerful centrifugal force (or super-gravity), which greatly increases the relative flow rate and filling efficiency of gas and liquid. The area 'liquid is in contact with the gas at a very high relative speed in the curved flow path under the condition of high dispersion, strong full movement and rapid interface update, which greatly enhances the efficiency of liquid gas liquid transfer. This new technology has the advantages of low liquid flooding, high throughput, low space requirements, high mass transfer efficiency, low energy consumption and low investment and operating costs. This technology can be widely applied to the theory, Wei, and Qi mentioned (four) scattered control lion gas-liquid reaction process, so it can be applied not only to the chemical industry, but also to other industry-related procedures such as environmental protection industries. The rotary charging bed is divided into two types, namely a counter-flow rotating packed bed and a cross-flow counter-flow rotating packed bed. As shown in the first figure, it is provided on a side of a closed casing 9 - a gas inlet 9 2 The surface + the core is provided - the gas outlets 9 3 and 2 are in the σ 9 4, and the bottom surface is provided with a liquid outlet 9 5; the outer casing 91 is provided with two rotating cylinders 97 which are rotated by the rotating shaft 96, and the feeding cylinders 97 are Filler 9 is filled. The body is supplied from the liquid inlet 9 to the center of the drum 97 via the liquid distributor 9 9 at the end of the line; the gas enters the center of the drum 9 7 from the gas inlet 9 2 through the packing 98. The chemical absorption procedure for the liquid and gas in the drum 97. The inner and outer ring fluid passages of such a counter-flow rotary packed bed are too large in cross-sectional area to change the gas velocity, which will increase the resistance of the gas, and is not suitable for gas-liquid mass transfer procedures such as absorption, etc. with high gas flow rate. . In order to introduce the centrifugal force field into the gas-liquid mass transfer program with high gas flow rate, some researchers began to develop a cross-flow rotary-filling machine different from the counter-flow type. The structure is as shown in the second figure. A sealed outer casing 8 has a plurality of gas inlets 8 2 and a liquid outlet 8 3 at the bottom surface, and a gas 2 outlet 8 4 and a liquid inlet 8 5 at the center of the top surface; and a shaft 8 is provided in the outer casing 8 1 a % of the filler 8 7 is driven, and a gas seal shaft 8 8 is provided above the filler 8 7 . The liquid is fed from the liquid inlet 8 5 to the center of the filler 87 through the liquid distributor 8 9 at the end of the line; From the gas inlet 8 2 through the fill 87 into the center. The liquid and gas are brought together at the center of the packing 87 for a chemical absorption procedure. In the cross-flow rotary packed bed, since the cross-sectional area of the gas flow passage is fixed, the gas is constant, and the gas flows along the axial direction of the rotating bed, and the centrifugal resistance is not required to be overcome, so the gas resistance is much smaller than that of the counterflow type, and the gas flow rate is high. The gas-liquid contact procedure can improve the disadvantages of the current high pressure loss of the scrubbing tower, which can greatly reduce the energy consumption used in the operation. > If the advantages of these two kinds of rotary packed bed equipment can be properly utilized, it can be applied to the absorption of carbon dioxide in the air, which can greatly increase the absorption efficiency. SUMMARY OF THE INVENTION 201103622 Therefore, the main object of the present invention is to provide an air carbon dioxide absorption device, which mainly uses this newly designed rotating packed bed to replace the conventional packed column for chemical absorption to recover carbon dioxide. The air carbon dioxide absorption device provided by the invention is mainly composed of a newly designed rotary packed bed, an air pump, an absorbent reservoir and a pump. The rotary packed bed has a sealed outer casing. The outer casing is provided with an air inlet and an absorbent outlet, and an air outlet and an absorbent inlet are disposed in the center of the top surface, and a filling device with a motor belt rotating at a high speed is disposed inside. The center of the filling is provided with a liquid distributor in communication with the absorbent inlet. An air pump pumps air from the air inlet into the housing. The absorbent reservoir is used to store the absorbent flowing from the absorbent outlet. The pump draws the absorbent from the absorbent reservoir into the housing from the absorbent inlet. The absorbent is sent from the inlet of the absorbent to the center of the filler through the liquid distributor at the end of the pipeline; and the air enters the center through the filler from the air inlet; the absorbent is sprayed by the centrifugal force by the high-speed rotation of the super-weight field above 100G. The carbon dioxide in the air meets at the center of the filler for a chemical absorption process that absorbs carbon dioxide from the air and allows the remaining gas to exit the air outlet, while the carbon dioxide-absorbing absorbent is recovered into the absorbent reservoir. By using the air-carbon dioxide absorption device provided by the present invention, the chemical absorption process using the rotary packed bed can reduce the size of the device and reduce the energy required for the absorption of the absorbent in the conventional packed tower to the top of the tower; The energy consumption reduction makes it more competitive in application, which in turn greatly reduces the cost. Therefore, from the economic point of view, this rotating packed bed will be a highly efficient carbon dioxide removal device. The structural features and the efficacy of the present invention will be described in detail below based on the drawings. [Embodiment] 201103622 Please refer to the third figure, the present invention provides a device for carbon dioxide absorption in air 'mainly by a rotating packed bed 1, an air pump 2, an absorbent reservoir 3 and a pump 4 Composition. The rotary packed bed 1 of the present invention has a sealed casing 11 having an air inlet 12 and an absorbent outlet 13 and an air outlet 14 and an absorbent inlet 1 in the center of the top surface. 5, while a filler 17 is provided with a motor j 6 at a high speed, and a center of the filler 17 is provided with a liquid distributor 18 in communication with the absorbent inlet 15. The air pump 2 draws air from the air inlet 12 into the outer casing 11. The absorbent reservoir 3 is used to store the absorbent flowing from the absorbent outlet 13. The pumping pump 4 pumps the absorbent in the absorbent reservoir 3 from the absorbent inlet 15 into the outer casing 11.
實際操作的過程中’吸收劑自吸收劑入口 1 5經管線末端 的液體:佈器18而送入填充物17的中心；而空氣自空氣入 口 1 2經填充物1 7而進入中心；吸收劑與空氣在填充物工7 之中心交匯以進行化學吸收程序，將空氣中的二氧化碳吸收， 並使剩餘氣體自該空氣出口 i 5排出，而吸收二氧化碳之吸收 劑回流至該吸收劑儲槽3中。 、本發明中的旋轉填充床1可以是逆流式旋轉填充床，也可 以疋錯流式旋轉填充床。 範圍 表1為本發明中以逆流式旋轉填充床實作之規格及操作 ------------- j_，》,、’、 ~ 逆流式旋轉填充床 操作參數 填充物内半徑Ri(cm) 2.0 201103622 填充物外半徑R〇(cm) 一 —. 8.0 軸向高度Zb(cm) 2.9 液體分佈器孔洞數 ------ 8 吸收劑濃度(mol/L) ----— 〇.2~ 10 馬達轉速（rpm) 500 ~ 3000 液體流量QL(L/min) 0.1' 10 空氣流量QG(L/min) 10' 100 本發明中，旋轉填充床1之填充物17於高速旋轉下，在其 心産生強大的離心力，而增加重力場強度，大幅提升空氣&吸 收劑的流速及接觸面積，在液體界面急速更新的情況下與氣體 以極高的相對速度在填充物中接觸，達到強化質傳的效 使吸收效率提升。 由於二氧化碳為酸性氣體，故一般選用具有鹼性之吸收 劑，常使用吸收劑之比較如表2，並將常用之方法簡述如下： (1)碳酸鉀吸收法： 此法最初是在美國開發利用煤合成液體燃料方案中的一 部分發展而起的，主要是利用碳酸鉀溶液吸收二氧化碳反應產 生碳酸氫鉀。再生方面’將已吸收二氧化碳的碳酸卸溶液加埶 到碳酸氫鉀的分解即可發生逆反應，產生二氧化碳並將反應^ 成的碳酸鉀再使用。此法發展為活化熱碳酸鉀法，即將吸收二 氧化碳的溫度提升至1〇5~ 120°C及壓力提高至2.3MPa，且在 同溫度下採用降壓的方法來再生吸收劑，其結果是增加反應速 率及吸收容量，但吸收速率仍慢，而且由於溫度的提升會造成 嚴重的腐蝕，故加入活性劑來提高吸收與再生速率並減輕腐 蝕，因而稱為活化熱碳酸鉀法。常用的活性劑有無機活性劑(石申 201103622 酸鹽、硼酸鹽和磷酸鹽)和有機活性劑(有機胺和醛、_類有機 物）。 、 (2)醇胺吸收法： 一般常用之醇胺類有一級醇胺(如MEA)、二級醇胺(如 DEA、DIPA)及三級醇胺(如MDEA、TEA)。一級醇胺和二級 醇胺具有強的驗性，故其與一氧化碳反應具有較快的速率，但 由於反應形成的產物為carbamate，使得其吸收容量限制於 0.5mol-C〇2/mol-醇胺。三級醇胺因鹼性較弱而降低與二氧化碳 反應的速率’然而其吸收容量卻能達到l.〇m〇l_c〇2/m〇1_醇胺。 近來，立體障礙醇胺(如AMP)被使用來代替傳統醇胺作為吸收 劑’因其具有較快之吸收速率且能如三級醇胺具有 lOmol-C〇2/mol·醇胺的高吸收容量。另外，混合醇胺也是目前 研究方向之一’因混合醇胺是溶液中混有兩種以上之醇胺溶 液’綜合各級醇胺的優點，故具有快吸收速率與高吸收容量之 特性，常使用之混合醇胺有MEA-MDEA、MEA-TEA、 DEA-MDEA ' DEA-TEA ' DEA-AMP、MEA-AMP & DEA-TEA-AMP 等。 (3)氫氧化鈉吸收法： 利用強鹼溶液作為吸收劑，氫氧化鈉是常使用的化學溶 劑’已有相當多的研究探討氫氧化鈉濃度對C02吸收效率的影 響’並也常以此系統比較不同氣液接觸吸收器之效能。除了氫 201103622 氧化鈉，LiOH及KOH也能被使用於吸收二氧化碳。 表2各種吸收劑優缺點之比較 吸收劑種類 優點 缺點 一級醇胺 MEA 吸收速率快 價格便宜 對碳氫化合物吸收極 小 吸收容量低 不適用於含有cos及cs2之 廢氣 較具腐蝕性 熱容量高 容易被煙道中的so2、o2毒化 二級醇胺 DEA ' DIPA 吸收速率快 較不具腐钱性 適用於含有cos及 cs2之廢氣 熱容量低 吸收容量低 三級醇胺 MDEA、TEA 吸收容量高 熱容量低 對H2S具有選擇性吸 收 汽提特性佳 吸收速率慢 201103622 立體障礙醇胺 ' ------- 吸收容量高 熱容量高 AMP、PZ 吸收速率快 汽提特性佳 對Hj具有高選擇性 吸收 ~~~~-- 強驗 去除效率佳 昂貴 NaOH、 KOH、LiOH 溶劑無法再生 弱鹼 氨水(NH4〇H) 價格低廉 吸收效率效低 化學吸收法可利用所使用的吸收劑種類不同或者搭配一 些增加吸收一氧化碳速率的活化劑，增加二氧化碳吸收效率。 以下是本發明中，以醇胺水溶液為吸收劑來吸收二氧化碳 之實驗說明。 口首先，將配製適當的醇胺溶液(02~ 10m〇]/L)濃度，在正 韦操作下’空氣經由空氣泵2推入逆流式旋轉填充床1内，從 填充物1 7外緣流動進入填充物！ 7内，最後由填充物丄7上 方空氣出口 14排出，以二氧化碳分析儀測得出口濃度。 #之後，打開馬達16轉動旋轉填充床丄内之填充物i 7， 接著將醇胺溶液經由抽水泵4打入填充物丄γ上方吸收劑入 口 1 5，液體再經由液體分佈器i 8開孔喷入填充物丄7之中 心，液體藉由旋轉產生的離心力作用向外殼i i甩出流動(於 11 201103622 100G以上的超重力場），最後由下方開口流出至吸收劑儲槽 3，醇胺溶液持續以循環模式吸收空氣中之二氧化碳氣體。曰 醇胺溶液與二氧化碳氣體在填充物丄7中以逆流的方式 接觸進行質傳，在超重力場内旋轉甩出過程中，液體經過填充 物被切割成細小液滴與液膜，同時，氣體從填充物1 7下方向 士流入與液體接觸，以達到吸收二氧化碳的目的最後量測空 氣入口 1 3與出口 1 5濃度，經由計算後可求得二氧化碳去除 率。 本實驗以不同濃度之醇胺水溶液吸收空氣中的二氧化碳 ^體(濃度約40(T1〇〇〇 ppm)，在+同的操作變因之下(吸收劑 轉速、液體流量、氣驗*) ’在*_作範圍測 1進出口處c〇2濃度的變化情形。 •^营操作(如表1 )下’量測C〇2進出σ濃度，㈣ et^求侍c〇2去除率，探討不同的操作 吸收效率。表3為本發明之—實驗結果：Μ敢㈣⑷2During the actual operation, the absorbent is fed from the absorbent inlet 15 through the liquid at the end of the line: the cloth 18 to the center of the filler 17; and the air enters the center from the air inlet 12 through the filler 17; Communicating with air at the center of the filling worker 7 for a chemical absorption process, absorbing carbon dioxide in the air, and discharging the remaining gas from the air outlet i 5, and returning the absorbent absorbing carbon dioxide to the absorbent reservoir 3 . The rotary packed bed 1 of the present invention may be a counter-flow rotary packed bed or a counter-flow rotating packed bed. Scope Table 1 is the specification and operation of the counter-flow rotary packed bed in the present invention ------------- j_, ",, ', ~ counter-flow rotary packed bed operating parameter filling Radius Ri(cm) 2.0 201103622 Filler outer radius R〇(cm) I—. 8.0 Axial height Zb(cm) 2.9 Number of liquid distributor holes □ 8 Absorbent concentration (mol/L) -- --— 〇.2~ 10 Motor speed (rpm) 500 ~ 3000 Liquid flow rate QL(L/min) 0.1' 10 Air flow rate QG(L/min) 10' 100 In the present invention, the filling of the packed bed 1 is 17 At high speeds, it produces strong centrifugal force in its heart, increases the strength of the gravitational field, greatly increases the flow rate and contact area of the air & absorbent, and fills the gas at a very high relative speed in the case of a rapid update of the liquid interface. In contact with the material, the effect of enhancing the quality transmission is enhanced, and the absorption efficiency is improved. Since carbon dioxide is an acid gas, it is generally used as an alkaline absorbent. The comparison of commonly used absorbents is shown in Table 2, and the commonly used methods are briefly described as follows: (1) Potassium carbonate absorption method: This method was originally developed in the United States. The development of a part of the coal synthetic liquid fuel scheme is mainly to use potassium carbonate solution to absorb carbon dioxide to produce potassium bicarbonate. In the aspect of regeneration, a carbonic acid-removing carbonic acid-removing solution is added to the decomposition of potassium hydrogencarbonate to cause a reverse reaction, and carbon dioxide is generated and the reacted potassium carbonate is reused. This method is developed to activate the hot potassium carbonate method, that is, the temperature of absorbing carbon dioxide is raised to 1〇5~120°C and the pressure is increased to 2.3MPa, and the pressure reducing method is used to regenerate the absorbent at the same temperature, and the result is an increase. The reaction rate and absorption capacity, but the absorption rate is still slow, and the corrosion is caused by the increase in temperature, so the active agent is added to increase the absorption and regeneration rate and reduce the corrosion, which is called the activated hot potassium carbonate method. Commonly used active agents are inorganic active agents (Shishen 201103622 acid salt, borate and phosphate) and organic active agents (organic amines and aldehydes, organic compounds). (2) Alcohol amine absorption method: Commonly used alcohol amines are primary alcohol amines (such as MEA), secondary alcohol amines (such as DEA, DIPA) and tertiary alcohol amines (such as MDEA, TEA). The primary alcohol amine and the secondary alcohol amine have strong testability, so they have a faster rate of reaction with carbon monoxide, but the product formed by the reaction is carbamate, so that the absorption capacity is limited to 0.5 mol-C〇2/mol-alcohol. amine. Tertiary alcohol amines reduce the rate of reaction with carbon dioxide due to weaker basicity. However, their absorption capacity can reach 1. 〇m〇l_c〇2/m〇1_alcoholamine. Recently, sterically hindered alkanolamines (such as AMP) have been used in place of conventional alkanolamines as absorbents because of their faster absorption rates and high absorption of lOmol-C〇2/mol·alkanolamines such as tertiary alcohol amines. capacity. In addition, mixed alcohol amines are also one of the current research directions 'Because mixed alcohol amines are mixed with two or more alcohol amine solutions in solution', which combines the advantages of various alcoholamines, so it has the characteristics of fast absorption rate and high absorption capacity. The mixed alcohol amines used are MEA-MDEA, MEA-TEA, DEA-MDEA 'DEA-TEA ' DEA-AMP, MEA-AMP & DEA-TEA-AMP and the like. (3) Sodium hydroxide absorption method: Using a strong alkali solution as an absorbent, sodium hydroxide is a commonly used chemical solvent. There have been quite a lot of studies to investigate the effect of sodium hydroxide concentration on the absorption efficiency of CO 2 'and often The system compares the performance of different gas-liquid contact absorbers. In addition to hydrogen 201103622 sodium oxide, LiOH and KOH can also be used to absorb carbon dioxide. Table 2 Comparison of Advantages and Disadvantages of Various Absorbents Absorber Type Advantages Disadvantages First-Organic Amine MEA Absorption Rate Fast Price Low To Hydrocarbon Absorption Very Low Absorption Capacity Unsuitable For Exhaust Gas Containing Cos and Cs2 Corrosive Heat Capacity High Easy to Smoke So2, o2 poisoning secondary alcohol amine DEA ' DIPA absorption rate is faster than non-corrosive. Applicable to cos and cs2 exhaust gas heat capacity low absorption capacity low tertiary alcohol amine MDEA, TEA absorption capacity high heat capacity low choice for H2S Sucking stripping characteristics, good absorption rate, slow 201103822 steric hindrance alcohol amine '------- absorption capacity, high heat capacity, high AMP, PZ, fast absorption rate, good stripping characteristics, good selective absorption for Hj~~~~-- Strong removal efficiency, expensive NaOH, KOH, LiOH solvent can not regenerate weak alkali ammonia (NH4〇H) Low cost, low efficiency, low efficiency, chemical absorption method can use different types of absorbents or with some activators that increase the rate of absorption of carbon monoxide Increase the efficiency of carbon dioxide absorption. The following is an experimental description of the present invention in which an aqueous alcohol amine solution is used as an absorbent to absorb carbon dioxide. First, the concentration of the appropriate alcoholamine solution (02~10m〇]/L) will be prepared. Under the operation of Zhengwei, the air is pushed into the counter-flow rotary packed bed 1 via the air pump 2, and flows from the outer edge of the filler 17. Enter the filler! In the seventh, it is finally discharged from the upper air outlet 14 of the filler 丄7, and the outlet concentration is measured by a carbon dioxide analyzer. After #, the motor 16 is turned to rotate the filler i7 in the packed bed, and then the alcoholamine solution is pumped into the absorbent inlet 1-5 via the pump 44, and the liquid is then opened through the liquid distributor i8. Sprayed into the center of the filler crucible 7, the liquid flows to the outer casing ii by the centrifugal force generated by the rotation (the supergravity field above 11 201103622 100G), and finally flows out from the lower opening to the absorbent reservoir 3, the alcoholamine solution Continuously absorbs carbon dioxide gas in the air in a cyclical mode. The sterol amine solution and the carbon dioxide gas are contacted in a countercurrent manner in the filler crucible 7 for mass transfer. During the rotation in the supergravity field, the liquid is cut into fine droplets and a liquid film through the filler, and at the same time, the gas is removed from the liquid. The filling material is in contact with the liquid in the lower direction of the filler to achieve the purpose of absorbing carbon dioxide. Finally, the concentration of the air inlet 13 and the outlet 15 is measured, and the carbon dioxide removal rate can be obtained by calculation. In this experiment, the carbon dioxide in the air is absorbed by different concentrations of aqueous alcoholamine solution (concentration is about 40 (T1〇〇〇ppm), under the same operating action of + (absorbent speed, liquid flow, gas test*)' In the range of *_ for the measurement of the change in the concentration of c〇2 at the entrance and exit. 1. The operation of the operation (as shown in Table 1) is to measure the concentration of Cσ2 in and out of σ, (4) et ^ seek the removal rate of c〇2, Different operating absorption efficiencies. Table 3 is the result of the present invention - experimental results: Μ (4) (4) 2
操作壓力：1 atm 吸收液'— 空氣氣體流~ 吸收液液體'ϊϊ''~- C〇2 濃度：470ppm 0.1 mol/L _ 10 L/min__ 0 9 1 7mir» 轉速 …—- — 认么 ι>νιπιπ _ C〇2吸收效率 1800 rpm 由上實驗數據結果，可得知本發 故本發贼錄要件，功心 12 201103622 【圖式簡單說明】 第一圖代表一種逆流式旋轉填充床簡圖， 第二圖代表一種錯流式旋轉填充床簡圖， 第三圖代表本發明之結構示意圖。 【主要元件符號說明】 旋轉填充床1 :密封外殼11 空氣入口12 吸收劑出口13 * 空氣出口14 吸收劑入口15 馬達1 6 填充物1 7 液體分佈器18 空氣泵2 吸收劑儲槽3 抽水泵4 籲外殼8 1 氣體入口 8 2 液體出口8 3 氣體出口 8 4 液體入口 8 5 轉軸8 6 填充物8 7 氣體封轴8 8 液體分佈器8 9 外殼9 1 氣體入口 9 2 13 201103622 氣體出口 9 3 液體入口 9 4 液體出口 9 5 轉軸9 6 轉筒9 7 填充物9 8 液體分佈器9 9Operating pressure: 1 atm Absorbent' - Air gas flow ~ Absorbent liquid 'ϊϊ''~- C〇2 Concentration: 470ppm 0.1 mol/L _ 10 L/min__ 0 9 1 7mir» Rotating speed...--- Recognize ι> ;νιπιπ _ C〇2 absorption efficiency 1800 rpm From the results of the above experimental data, you can know the origin of the thief record, Gongxin 12 201103622 [Simple diagram of the diagram] The first diagram represents a counterflow rotary packed bed diagram The second diagram represents a schematic diagram of a cross-flow rotary packed bed, and the third diagram represents a schematic view of the structure of the present invention. [Main component symbol description] Rotating packed bed 1: sealed casing 11 air inlet 12 absorbent outlet 13 * air outlet 14 absorbent inlet 15 motor 1 6 filling 1 7 liquid distributor 18 air pump 2 absorbent tank 3 pump 4 Capsule 8 1 Gas inlet 8 2 Liquid outlet 8 3 Gas outlet 8 4 Liquid inlet 8 5 Rotary shaft 8 6 Filler 8 7 Gas seal shaft 8 8 Liquid distributor 8 9 Housing 9 1 Gas inlet 9 2 13 201103622 Gas outlet 9 3 Liquid inlet 9 4 Liquid outlet 9 5 Rotary shaft 9 6 Rotary 9 7 Filler 9 8 Liquid distributor 9 9