M347225 八、新型說明： 【新型所屬之技術領域】 本創作係有關一種流體化浮動床溶劑回收裝置，尤指 一種於吸附塔增加非偶合定風量控制單元，使球狀吸附材 於吸附塔内部之浮動情形，不致產生低速不浮動、流體化 浮動不佳或是過速吹出吸附塔之情況；而於吸附塔上游端 串接冷凝吸收預處理單元，處理不適合球狀吸附材吸附之 有機物；另外可於下游端串並接固定床式溶劑回收單元，且 選用疏水性球狀吸附材，俾以提高吸附材性能與使用壽 命、提升有機溶劑回收穩定性與安全性及降低後續純化成 本之設計者。 【先前技術】 按，利用高孔隙率、高比表面積之吸附材，藉由吸附 作用去除揮發性有機氣體（Volati le Organic Compounds， VOCs)之吸附法淨化技術，一般多使用固定床的吸附系統； 而固定床吸附系統係以兩塔或多塔批式操作方式，進行廢 氣的吸附及吸附飽和後之吸附材料再生，唯在遇有高反應 性的VOCs處理時，常因被吸附之化學品於吸附時與吸附材 產生觸媒氧化放熱反應（例如酮類與活性碳吸附材），導致 固定床内部散熱不佳而大量熱聚集，進而發生碳床著火或 爆炸問題；於是，為了改善固定床吸附系統的缺點，而發 展出一種流體化浮動床的吸附系統。 次按，流體化浮動床吸附系統的吸附流程如第一圖所 示，廢氣以廢氣風機（14)自氣流入口（13)送入吸附塔（10) M347225 的底部，而廢氣氣流藉氣流分散板（12)分散後，乃與由上 落下的球狀吸附材（30)接觸，即可成為淨化氣體並從塔頂 之氣流出口（15)排放；其中，吸附塔（10)的内部以多孔板 (11)分隔成數層，球狀吸附材（30)由吸附塔（10)的頂端落 下，而在多孔板（11)的上方形成浮動層，並沿著多孔板（11) 一層一層的開口部落下，當球狀吸附材（30)與含有VOCs的 廢氣接觸時，將廢氣中的VOCs吸附於球狀吸附材（30)的孔 洞内，廢氣即變成淨化氣體排放；然而，吸附飽和的球狀 吸附材（30)落至吸附塔（10)底部的貯槽後，藉吸附材輸送 裝置（20)送至後續之脫附程序，進行脫附再生工作後送回 吸附塔（10)之頂端。 再按，流體化浮動床吸附系統的脫附流程如第二圖所 示，吸附飽和的球狀吸附材（30)落至吸附塔（10)底部的貯 槽後，並藉吸附材輸送裝置（20)之輸送氣源（22)，以所送 出之空氣或氮氣形成推送力，經出料管（21)、第一輸送轉 接器（23)、輸送管路（24)與第二輸送轉接器（25)送至脫附 塔（40)之頂端，進行脫附再生之工作；脫附再生後的球狀 吸附材（30)則以第三輸送轉接器（26)、第四輸送轉接器（27) 與進料管（28)送回吸附塔（10)的頂端。 接著，待再生之球狀吸附材（30)乃在脫附塔（40)之脫 附反應腔（41)慢慢往下流動，並經由脫附熱源（42)加熱， 再由脫附塔（40)下方之脫附氣源（43)吹入氮氣與球狀吸附 材（30)接觸，將球狀吸附材（30)中的VOCs脫附；脫附後的 球狀吸附材（30)經脫附塔（40)底部冷卻後，由前述之輸送 過程送回吸附塔（10)上端，再度吸收VOCs ;而脫附出來的 M347225 高濃度廢氣，則以氮氣流經脫附氣體管路（44)攜帶至冷凝 塔（50)冷凝，冷凝液體由回收槽（52)回收，冷凝氣體則自 氣體出口（53)排出。 此外，流體化浮動床吸附系統設計時，一般均以固定 之流體化浮動線速度設計（例如直徑0.6丽、比重0.6g/cc 的球狀活性碳吸附材的最佳流體化浮動線速度介於 0· 75〜1. 25m/s之間），以避免吸附材不浮動而直接掉落、流 體化浮動不佳或是過速吹出吸附塔，但吸附塔（10)内部多 孔板（11)之隔層數、球狀吸附材（30)的浮動分佈及再生的 速度，均影響VOCs去除的效率；因此，最好能充份掌握廢 氣的特性，例如溫度、溼度與VOCs的組成特性及濃度等， 而機動地以恰當之風量，讓球狀吸附材（30)不致產生低速 不浮動、流體化浮動不佳或是過速吹出吸附塔之情況；又， 如表一所示，由於待處理的VOCs分子大小不盡相同，沸 點、分子量、吸脫附特性及極性、分子徑等也各異，不同 的吸附材的吸脫附能力及吸脫附速度也不相同，最好能依 據待處理VOCs的類別，予以預先處理並選用適切之吸附材 與相應之吸附系統搭配，而最適切的進行廢氣淨化與溶劑 回收之工作。 廢氣中溶劑特性性質表（表一） 溶劑 學名 分子 量 沸點 (°c) 活性碳(吸附材） 脫附難度 蒸汽壓 (20°CmmHg) 水溶性 Toluene 甲苯 (C7H8) 92 111 容易 22.3 不溶於水 M347225 MEK 甲基乙基酮 (C4H80) 72 80 容易 77.5 27 〜29 g/100 g水 DMF 二曱基甲醯胺 (HCON(CH3)2) 73 153 困難 2.7 全溶於水 【新型内容】 本創作之主要目的，係具有大幅提高吸附材性能與使 用壽命、提升有機溶劑回收穩定性與安全性及降低後續純 化成本之功效。 本創作之另一目的，則欲解決先前技術流體化浮動床 吸附系統之吸附塔風量無法調整之問題，而具有吸附塔風 量得以機動調整之功效。 為達上述功效，本創作流體化浮動床溶劑回收裝置之 結構特徵，係包括有： 一吸附塔，選用疏水性之球狀吸附材於其内部吸附廢 氣； 一脫附塔，設置於該吸附塔之下游端，而藉吸附材輸送 裝置將吸附飽和之球狀吸附材，輸送至此脫附再生再送回吸 附塔； 一冷凝塔，設置於該脫附塔之下游端，而將脫附出來的 高濃度廢氣冷凝回收； 一冷凝吸收預處理單元，設置於該吸附塔上游產生廢 氣之任一製程機台排氣來源端，處理有機廢氣中難脫附之中 高沸點水溶性有機物，可包含一組以上之冷凝盤管、一除霧 器、一儲液槽及溶劑回收管，該冷凝盤管中以1至20°C之冰 一固定床溶劑回收單元，將複數個固定吸附床並聯連接 於該吸附^之氣流出σ ’該固定吸附床内部平鋪有吸附材， 外部連接有蒸氣源、排氣管及冷凝分離器，該冷凝分離器設 置有排水管與連接至回收槽之溶劑回收管者。M347225 VIII. New description: [New technical field] This is a fluidized floating bed solvent recovery device, especially a non-coupling constant air volume control unit in the adsorption tower, so that the spherical adsorption material is inside the adsorption tower. In the case of floating, it does not cause low-speed non-floating, fluid fluidity is not good, or the adsorption tower is blown out at an excessive speed; and the condensing absorption pretreatment unit is connected in series at the upstream end of the adsorption tower to treat organic matter that is not suitable for adsorption by the spherical adsorbing material; At the downstream end, a fixed bed type solvent recovery unit is connected in parallel, and a hydrophobic spherical adsorbing material is selected, which is used to improve the performance and service life of the adsorbent, improve the recovery stability and safety of the organic solvent, and reduce the subsequent purification cost. [Prior Art] According to the adsorption method for removing volatile organic compounds (VOCs) by adsorbing materials with high porosity and high specific surface area, a fixed bed adsorption system is generally used; The fixed bed adsorption system uses two-stage or multi-tower batch operation mode to carry out the adsorption of the exhaust gas and the regeneration of the adsorbed material after the adsorption is saturated. However, in the case of highly reactive VOCs, the adsorbed chemicals are often During the adsorption, the catalyst oxidative exothermic reaction with the adsorbent material (such as ketones and activated carbon adsorbing materials) leads to poor heat dissipation inside the fixed bed and a large amount of heat accumulation, which causes the carbon bed to ignite or explode; thus, in order to improve the adsorption of the fixed bed The shortcomings of the system have led to the development of a fluidized floating bed adsorption system. Sub-press, the adsorption process of the fluidized floating bed adsorption system is as shown in the first figure, the exhaust gas is sent from the gas inlet (13) to the bottom of the adsorption tower (10) M347225 by the exhaust fan (14), and the exhaust gas flow is dispersed by the gas flow dispersion plate. (12) After being dispersed, it is contacted with the spherical adsorbing material (30) which is dropped from above, and is discharged as a purge gas and discharged from the gas flow outlet (15) at the top of the column; wherein the inside of the adsorption tower (10) is a perforated plate (11) divided into several layers, the spherical adsorbing material (30) is dropped from the top end of the adsorption tower (10), and a floating layer is formed above the porous plate (11), and an open tribe is layered along the perforated plate (11). When the spherical adsorbing material (30) is in contact with the exhaust gas containing the VOCs, the VOCs in the exhaust gas are adsorbed into the pores of the spherical adsorbing material (30), and the exhaust gas is discharged into the purified gas; however, the saturated spherical shape is adsorbed. After the adsorption material (30) falls to the storage tank at the bottom of the adsorption tower (10), it is sent to the subsequent desorption procedure by the adsorption material conveying device (20), and is subjected to the desorption regeneration operation and sent back to the top of the adsorption tower (10). Pressing again, the desorption process of the fluidized floating bed adsorption system is as shown in the second figure, after the saturated spherical adsorbent material (30) falls to the storage tank at the bottom of the adsorption tower (10), and the adsorption material conveying device (20) The conveying gas source (22), forming a pushing force by the air or nitrogen sent out, through the discharging pipe (21), the first conveying adapter (23), the conveying pipe (24) and the second conveying transfer The device (25) is sent to the top of the desorption column (40) to perform the desorption regeneration operation; the desorbed and regenerated spherical adsorption material (30) is transferred to the third delivery adapter (26) and the fourth delivery device. The connector (27) and the feed tube (28) are returned to the top end of the adsorption tower (10). Next, the spherical adsorbent (30) to be regenerated is slowly flowed downward in the desorption reaction chamber (41) of the desorption column (40), heated by the desorption heat source (42), and then desorbed by the desorption column ( 40) The desorbed gas source (43) underneath is blown into contact with the spherical adsorbing material (30), and the VOCs in the spherical adsorbing material (30) are desorbed; the desorbed spherical adsorbing material (30) is subjected to desorption After the bottom of the desorption column (40) is cooled, it is sent back to the upper end of the adsorption tower (10) by the above-mentioned conveying process to absorb VOCs again; and the desorbed M347225 high-concentration exhaust gas flows through the desorbed gas line with nitrogen gas (44). Carrying to the condensation tower (50) for condensation, the condensed liquid is recovered by the recovery tank (52), and the condensed gas is discharged from the gas outlet (53). In addition, the fluidized floating bed adsorption system is designed with a fixed fluidized floating line speed (for example, the optimum fluidized floating line speed of a spherical activated carbon adsorbent with a diameter of 0.6 liter and a specific gravity of 0.6 g/cc is between 0·75~1. 25m/s), to avoid direct drop of the adsorbent material without floating, poor fluidization fluctuation or excessive speed blowing of the adsorption tower, but the inner porous plate (11) of the adsorption tower (10) The number of layers, the floating distribution of the spherical adsorbent (30) and the speed of regeneration all affect the efficiency of VOCs removal; therefore, it is better to fully grasp the characteristics of the exhaust gas, such as temperature, humidity and composition characteristics and concentration of VOCs. , and the right amount of air, so that the spherical adsorbent (30) does not produce low-speed non-floating, fluidized floating poor or excessive speed blowing out of the adsorption tower; and, as shown in Table 1, due to the pending The molecular size of VOCs is not the same, the boiling point, molecular weight, adsorption and desorption characteristics, polarity, molecular diameter, etc. are also different. The adsorption and desorption capacity and adsorption and desorption speed of different adsorption materials are also different, preferably based on the VOCs to be treated. Category First selection process and the relevance of the adsorbing material of the adsorption system with a corresponding, but the most appropriate work of exhaust gas purification and solvent recovery. Table of solvent properties in exhaust gas (Table 1) Solvent name Molecular weight Boiling point (°c) Activated carbon (adsorbed material) Desorption difficulty Vapor pressure (20°CmmHg) Water-soluble Toluene Toluene (C7H8) 92 111 Easy 22.3 Insoluble in water M347225 MEK Methyl ethyl ketone (C4H80) 72 80 Easy 77.5 27 ~ 29 g / 100 g water DMF Dimethyl carbamide (HCON (CH3) 2) 73 153 Difficult 2.7 fully soluble in water [new content] The main The purpose is to greatly improve the performance and service life of the adsorbent, improve the stability and safety of organic solvent recovery, and reduce the cost of subsequent purification. Another object of the present invention is to solve the problem that the adsorption tower air volume of the prior art fluidized floating bed adsorption system cannot be adjusted, and the adsorption tower air volume can be maneuvered. In order to achieve the above effects, the structural characteristics of the fluidized floating bed solvent recovery device of the present invention include: an adsorption tower that uses a hydrophobic spherical adsorbent material to adsorb exhaust gas therein; a desorption tower disposed in the adsorption tower At the downstream end, the spheroidal adsorption material adsorbed by the adsorption material is transported to the desorption regeneration and sent back to the adsorption tower; a condensation tower is disposed at the downstream end of the desorption tower, and will be desorbed high. Concentration exhaust gas condensation recovery; a condensation absorption pretreatment unit, disposed at the exhaust source end of any process machine that generates exhaust gas upstream of the adsorption tower, and is capable of decomposing high-boiling water-soluble organic matter in the organic waste gas, which may include more than one set a condensing coil, a defogger, a liquid storage tank and a solvent recovery tube, wherein the condensing coil has a fixed bed solvent recovery unit of 1 to 20 ° C, and a plurality of fixed adsorption beds are connected in parallel to the adsorption ^The air flow out σ 'The fixed adsorption bed is internally laid with an adsorbent material, and the external connection is connected with a vapor source, an exhaust pipe and a condensing separator, and the condensing separator is provided with a drain pipe and a connection A solvent recovery pipe to the recovery of those grooves.
M347225 冷凝盤管壁面產生水份凝結之液膜，藉由冷凝進 核包覆作用，包覆氣流中較高彿點有機物微霧， ^後液、_相平衡之液膜吸收機制，可對氣流中水 =生_職進行極為有效的吸收預處理機制；設置於該冷 及下游端之除霧器’可將氣流中經冷凝吸收作用後之水 S微霧滴有效去除，並收集於儲液槽中回收處理；以及 然而，該疏水性之球狀吸附材可為活性碳、沸石、活性 碳分子篩、樹脂等多孔性吸附材，尤其是石油瀝青基球形活 性碳（PSAC)、聚苯乙烯樹脂與高矽疏水性沸石其中之一種。 該冷凝吸收預處理單元預處理有機廢氣之淨化過程 中，其上下游可設置一熱管式(Heat pipe type)或盤管式(Run around type ; coil to coil type)熱回收熱交換器，可將冷凝吸 收預處理單元下游端所排出之冷氣流’經由熱回收熱交換器 管線内之流體，導引至該熱回收熱交換器與上游端之進氣氣 流熱交換，以冷卻進氣氣流之溫度，增加冷凝吸收效率並節 省能源；而其進氣風速約為2.5m/s以下，較佳約為h〇〜15 m/s之間。 此外，該吸附塔係於内部中段以數多孔板分隔成數 層，内部底端設置一氣流分散板，底部設置一氣流入口且 連接一廢氣風機，頂部設置一氣流出口；另於廢氣風機與 氣流入口之間設置一流I計’並令廢氣風機連接一變頻 M347225 器，且於該流量計與變頻器間設置一流量控制器；並進一 步將一非偶合平衡管之一端連接於該氣流出口，而非偶合 平衡管之另端連接於廢氣風機與製程機台風機排氣口之 間；因此，吸附塔内部多孔板之孔徑不限定必須小於球狀吸 附材之直徑（習知吸附塔之多孔板孔徑必須小於球狀吸附材 之直徑，球狀吸附材才不致自多孔板之孔洞落下）。 【實施方式】 首先，請參閱第三圖所示，本創作之吸附塔（10)，係 ρ 較第一圖所示之習知技術，加設一非偶合定風量控制單元 (60)，而該非偶合定風量控制單元（60)，乃於廢氣風機（14) 與吸附塔（10)之氣流入口（13)間設置一流量計（61)，並令 廢氣風機（14)連接一變頻器（63)，且於流量計（61)與變頻 器（63)間設置一流量控制器（62)，藉以機動調整該廢氣風 機（14)送入吸附塔（10)之風量，而以吸附塔風量得以機動 調整之功效，致使吸附塔（10)之球狀吸附材（30)穩定浮 動，不致產生低速不浮動而直接掉落、流體化浮動不佳或 _ 是過速吹出吸附塔之情況。 . 此外，將一非偶合平衡管（64)之一端連接於吸附塔（10) 之氣流出口（15)，而非偶合平衡管（64)之另端連接於廢氣 風機（14)與製程機台風機（65)之排氣口間，用以穩定開停機 之風量，且使吸附塔（10)内之球狀吸附材（30)，可維持穩定 之最低流體化浮動速度（Minimum fluidized velocity)， 不致因為風速過低而低速不浮動，甚至直接掉落至吸附塔 (10)下方；因此，如第五圖所示，吸附塔（10)内部多孔板（11) 之孔徑D不限定必須小於球狀吸附材（30)之直徑0 (0 = -10· M347225 0·8 〜3D)〇 再者，請參閱第四圖所示，本創作之實施例，係較第 二圖所示之習知技術’加設一冷凝吸收預處理單元（8〇)， 設置於該吸附塔（10)之上游端，處理製程機台有機廢氣中若 含有難脫附之較咼沸點水溶性有機物（如表一所示之Dmf)， 可包含一組以上之冷凝盤管（81)，該冷凝盤管（81)中以i至 20°C之冰水循環，使冷凝盤管（81)壁面產生水份凝結之液 膜，藉由冷凝進行中之凝結核包覆作用，包覆氣流中較高沸 點有機物微霧（如DMF)，以及冷凝後液、氣間相平衡之液膜 吸收機制，可對廢氣中水溶性V0Cs進行極為有效的吸收預處 理機制；設置於該冷凝盤管下游端之除霧器（82)可將廢氣中 之水及VOCs微霧滴有效去除後，收集於儲液回收槽（83)中經 溶劑回收管（84)回收處理。 再者，該吸附塔（10)之下游端加設一固定床式溶劑回收 單元（70)，而該固定床式溶劑回收單元（7〇)，乃將複數個固 定吸附床（71)並聯連接於吸附塔（1〇)之氣流出口（15)，該固 定吸附床（71)内部平鋪有吸附材（72)，外部連接有蒸氣源 (73)、排氣管（74)及冷凝分離器（75)，該冷凝分離器（75)設 置有排水管（77)與連接至回收槽（78)之溶劑回收管（76);於 是’當吸附塔（1〇)選用疏水性之球狀吸附材（3〇)，則可由 球狀吸附材（3〇)針對水溶性有機溶劑予以吸附，再藉後續 脫附塔（40)與冷凝塔（5〇)進行回收之工作，而對於其他溶 水丨生低之物質（如表一所示之甲苯，Toluene)，則由該固定 床式溶劑回收單元（70)予以回收，故具有大幅提高吸附材性 能與使用壽命、提升有機溶劑回收穩定性與安全性及降低 -11 - M347225 後續純化成本之功效。 基於如是之構成，請參閱表二所示，本創作於吸附塔 (10)增加非偶合定風量控制單元（60)控制風量之設計，係 使吸附性肖b維持在85〜95%之穩定狀態，而球狀吸附材（3〇) 之浮動情形，乃不致產生低速不浮動、流體化浮動不佳或 是過速吹出吸附塔之情況；又請參閱表三所示，本創作於 實施例增加冷凝吸收預處理單元（80)，可使回收效率達到 90%以上，含水率低於1%，大幅延長吸附材壽命；另外， . 增加固定床式溶劑回收單元（70)，且選用對酮類有機物不具 ，觸媒放熱反應之^^本乙稀樹脂類疏水性球狀吸附材（3〇)之 吞又计’可使回收效率達到90%以上，含水率低於3%，並將 安全性提咼且回收成本降低，確具大幅提高吸附材性能與 使用壽命、提升有機溶劑回收穩定性與安全性及降低後續 純化成本之功效。 500NCMM ;來源風量 200〜600NCMM.(表二） 風速（量） 控制 流體化浮動床 風量範圍 活性碳（吸附 材）吸附處理性 能 活性碳（吸 附材）浮動 情形 活性碳（吸附 材）吹出浮動床 本體情形 無非偶合 定風速 (量）控制 200〜600NCMM 25〜95% (不穩定） 不佳 嚴重 有非偶合 定風速 (量）控制 450〜550NCMM 85-95% (穩定） 佳 無 -12- M347225 500NCMM ;溶劑：MEK(丁酮）35 kgs/hr，Toluene(甲苯）35 kgs/hr ; DMF(二 甲基甲醯胺）10kgs/hr ;入風溫度25〜40°C，入風相對溼度35〜75% RH(表三） 溶劑回收吸 球狀吸附 BET比 平均 流体化浮 回收溶劑 回收效 安全性 回收運轉 附床型式 材 表面積 微孔 動床吸附 含水率(％ 率（%) 成本(含 (m2/g) 徑(A) 材壽命 wt) 純化，以 第一項為 基準） 單獨雙槽固 柱狀活性 800〜 10 〜15 —— 30-90% 50% ΐ 不佳 1.0 定吸附床 碳 1000 單獨流體化 0 0· 6mm 活 800〜 6〜10 短 3-20% 85% Τ 可 0.5 浮動床 性碳 1300 (數月即 需活化 再生） 流體化浮動 0 0· 6mm 活 800〜 6〜10 數年 1% i 90% Τ 佳 0. 15 床搭配冷凝 性碳 1300 (數年才 吸收預處理 需活化 單元 再生） 流體化浮動 0 0. 6mm 疏 400〜 5. 6 X 中 3°/〇 i 90% Τ 佳 0.2 床搭配雙槽 水性高破彿 500 5.8 (數季需 固定吸附床 石（流體化 (高梦 活化再 浮動床）土 沸石） 生） 01醒疏水 土 性樹脂（固 1100( 定吸附床） 樹脂） -13- M347225 综上所述，本創作所揭示之構造，為昔所無，且確能 達到預期之功效，並具可供產業利用性，完全符合新型專 利要件，祈請貴審查委員核賜專利，以勵創新，無任德感。 惟，上述所揭露之圖式、說明，僅為本創作之較佳實 施例，大凡熟悉此項技藝人士，依本案㈣料所作之修 飾或等效變化，仍應包括在本案申請專利範圍内。M347225 condensed coil wall surface produces a liquid film of moisture condensation. By condensing into the core coating, it coats the micro-fog of the higher organic point in the gas stream, and the liquid film absorption mechanism of the liquid and _ phase balance can be used for the air flow. The medium water = raw _ job carries out an extremely effective absorption pretreatment mechanism; the defogger set at the cold and downstream end can effectively remove the water S micro mist droplets after condensation absorption in the gas stream, and collect it in the liquid storage And the hydrophobic spherical adsorbing material may be a porous adsorbing material such as activated carbon, zeolite, activated carbon molecular sieve, or resin, especially petroleum pitch-based spherical activated carbon (PSAC), polystyrene resin. One of the hydrophobic zeolites with sorghum. In the process of purifying the organic waste gas by the condensing absorption pretreatment unit, a heat pipe type or a coil to coil type heat recovery heat exchanger may be disposed upstream and downstream. The cold gas stream discharged from the downstream end of the condensation absorption pretreatment unit passes through the fluid in the heat recovery heat exchanger line, and is guided to the heat recovery heat exchanger to exchange heat with the inlet gas stream at the upstream end to cool the temperature of the inlet gas stream. The condensing absorption efficiency is increased and the energy is saved; and the inlet air velocity is about 2.5 m/s or less, preferably about h 〇 15 m/s. In addition, the adsorption tower is divided into several layers in the inner middle section by a plurality of perforated plates, an inner flow end is provided with a gas flow dispersion plate, a gas flow inlet is arranged at the bottom and an exhaust gas fan is connected, and an air flow outlet is arranged at the top; and the exhaust gas fan and the air flow inlet are provided. Set a first-class I meter between 'and make the exhaust fan connected to a frequency conversion M347225, and set a flow controller between the flowmeter and the inverter; and further connect one end of a non-coupled balance tube to the air outlet, instead The other end of the coupling balance tube is connected between the exhaust fan and the exhaust port of the process machine fan; therefore, the diameter of the porous plate inside the adsorption tower is not limited to be smaller than the diameter of the spherical adsorption material (the aperture of the porous plate of the adsorption tower must be Less than the diameter of the spherical adsorbing material, the spherical adsorbing material does not fall from the pores of the perforated plate). [Embodiment] First, as shown in the third figure, the adsorption tower (10) of the present invention is ρ added a non-coupling constant air volume control unit (60) than the conventional technique shown in the first figure. The non-coupling constant air volume control unit (60) is provided with a flow meter (61) between the exhaust air fan (14) and the air flow inlet (13) of the adsorption tower (10), and the exhaust air fan (14) is connected to a frequency converter ( 63), and a flow controller (62) is disposed between the flow meter (61) and the frequency converter (63), thereby maneuvering the air volume of the exhaust fan (14) into the adsorption tower (10), and the air volume of the adsorption tower The effect of the maneuver adjustment makes the spherical adsorbing material (30) of the adsorption tower (10) stably float, and does not cause a low speed to float without falling, a fluidization floating poorly, or a condition that the adsorption tower is blown out at an excessive speed. In addition, one end of a non-coupling balance tube (64) is connected to the air outlet (15) of the adsorption tower (10), and the other end of the non-coupling balance tube (64) is connected to the exhaust fan (14) and the processing machine. The exhaust port of the fan (65) is used to stabilize the air volume of the shutdown, and the spherical adsorbent (30) in the adsorption tower (10) can maintain a stable minimum fluidized velocity (Minimum fluidized velocity). Not because the wind speed is too low, the low speed does not float, and even falls directly below the adsorption tower (10); therefore, as shown in the fifth figure, the aperture D of the inner porous plate (11) of the adsorption tower (10) is not limited to be smaller than the ball. The diameter of the adsorbing material (30) is 0 (0 = -10· M347225 0·8 ~ 3D). Further, please refer to the fourth figure. The embodiment of the present invention is a conventional example shown in the second figure. The technology 'adds a condensing absorption pretreatment unit (8〇), which is disposed at the upstream end of the adsorption tower (10), and processes the organic waste gas of the processing machine to contain water-soluble organic matter which is difficult to desorb and is more difficult to desorb (such as Table 1). The Dmf) shown may comprise more than one set of condensing coils (81) in the condensing coil (81) The ice water circulation of i to 20 °C causes the liquid film of water condensation to be formed on the wall of the condensing coil (81), and the high-boiling organic matter micro-mist (such as DMF) is coated in the airflow by the condensation of the condensation tube in the middle of condensation. ), and the liquid film absorption mechanism of the liquid and gas phase equilibrium after condensation, can effectively absorb the water-soluble V0Cs in the exhaust gas; the mist eliminator (82) disposed at the downstream end of the condensation coil can After the water and the VOCs micro-mist droplets in the exhaust gas are effectively removed, they are collected and collected in the liquid recovery tank (83) and recovered by the solvent recovery tube (84). Furthermore, a fixed bed solvent recovery unit (70) is added to the downstream end of the adsorption tower (10), and the fixed bed solvent recovery unit (7〇) connects a plurality of fixed adsorption beds (71) in parallel. At the gas outlet (15) of the adsorption tower (1〇), the fixed adsorption bed (71) is internally laid with an adsorbent material (72), and a vapor source (73), an exhaust pipe (74) and a condensation separator are externally connected. (75), the condensing separator (75) is provided with a drain pipe (77) and a solvent recovery pipe (76) connected to the recovery tank (78); then 'when the adsorption tower (1〇) selects a hydrophobic spherical adsorption The material (3〇) can be adsorbed by the spherical adsorbent (3〇) for the water-soluble organic solvent, and then recovered by the subsequent desorption tower (40) and the condensation tower (5〇), and for other dissolved water. The low-lying substances (such as toluene shown in Table 1) are recovered by the fixed-bed solvent recovery unit (70), so that the performance and service life of the adsorbent are greatly improved, and the recovery stability of the organic solvent is improved. Safety and reduction of the efficacy of -11 - M347225 subsequent purification costs. Based on the composition of this, please refer to Table 2, the design of the non-coupling constant air volume control unit (60) to control the air volume in the adsorption tower (10) is to maintain the adsorption stability b at a steady state of 85 to 95%. However, the floating condition of the spherical adsorbing material (3〇) does not cause low-speed non-floating, fluidizing floating, or excessively blowing out of the adsorption tower; see also Table 3, the creation is increased in the embodiment. The condensing absorption pretreatment unit (80) can achieve a recovery efficiency of more than 90%, a water content of less than 1%, and greatly prolong the life of the adsorbent; in addition, a fixed bed solvent recovery unit (70) is added, and a ketone is selected. Organic matter does not have, the catalyst exothermic reaction ^^ This etheric resin type hydrophobic spherical adsorbent (3〇) can be recycled to achieve more than 90% recovery efficiency, moisture content less than 3%, and safety The improvement and recovery cost are reduced, which has the effect of greatly improving the performance and service life of the adsorbent, improving the stability and safety of organic solvent recovery and reducing the subsequent purification cost. 500NCMM; source air volume 200~600NCMM. (Table 2) Wind speed (quantity) Control fluidized floating bed air volume range Activated carbon (adsorbed material) adsorption treatment performance Activated carbon (adsorbed material) floating situation Activated carbon (adsorbed material) blown floating bed body The situation is nothing more than the coincidence of the wind speed (quantity) control 200~600NCMM 25~95% (unstable) poorly severe with non-coupling constant wind speed (quantity) control 450~550NCMM 85-95% (stable) Jiawu -12- M347225 500NCMM; Solvent: MEK (butanone) 35 kgs / hr, Toluene (toluene) 35 kgs / hr; DMF (dimethylformamide) 10 kgs / hr; inlet air temperature 25 ~ 40 ° C, inlet air relative humidity 35 ~ 75 % RH (Table 3) Solvent recovery suction spheroidal adsorption BET ratio average fluidization float recovery solvent recovery efficiency safety recovery operation bed type surface area microporous moving bed adsorption moisture content (% rate (%) cost (including (m2/ g) Diameter (A) Material life wt) Purification, based on the first item) Separate double tank solid columnar activity 800~ 10 〜15 —— 30-90% 50% ΐ Poor 1.0 Fixed adsorbent bed Carbon 1000 Separate fluid 0 0·6mm live 800~ 6~10 Short 3-20% 85% Τ 0.5 floating bed carbon 1300 (requires activation regeneration in a few months) Fluidized floating 0 0·6mm Live 800~ 6~10 Years 1% i 90% Τ Good 0. 15 Beds Condensed carbon 1300 (regeneration pretreatment requires activation unit regeneration for several years) Fluidization float 0 0. 6mm Sparse 400~ 5. 6 X Medium 3°/〇i 90% 佳 Good 0.2 bed with double-slot water-based high-breaking Buddha 500 5.8 (Several seasons need to fix the adsorbed bed stone (fluidization (high dream activation re-floating bed) soil zeolite) raw) 01 wake hydrophobic resin (solid 1100 (fixed bed) resin) -13- M347225 In summary, The structure revealed by this creation is unprecedented, and it can achieve the expected effect, and it can be used for industrial utilization. It fully complies with the new patent requirements, and invites the reviewing committee to grant a patent to encourage innovation and no morality. sense. However, the drawings and descriptions disclosed above are only preferred embodiments of the present invention. Those who are familiar with the art, and the modifications or equivalent changes made in accordance with the provisions of this case (4) shall still be included in the scope of patent application in this case.
-14- M347225 【圖式簡單說明】 第一圖係習用流體化浮動床吸附系統之結構示意圖（說 明吸附流程）。 第二圖係習用流體化浮動床吸附系統之結構示意圖（說 明脫附流程）。 第三圖係本創作吸附塔加設非偶合定風量控制單元之 _ 結構示意圖。 第四圖係本創作實施例之結構示意圖。 p 第五圖A、B係本創作球狀吸附材與多孔板之尺寸相對 關係不意圖。 【主要元件符號說明】 (10)吸附塔 (28)進料管 (11)多孔板 (30)球狀吸附材 (12)氣流分散板 (40)脫附塔 (13)氣流入口 (41)脫附反應腔 (14)廢氣風機 (42)脫附熱源 (15)氣流出口 (43)脫附氣源 (20)吸附材輸送裝置 (44)脫附氣體管路 (21)出料管 (5 0 )冷凝塔 (22)輸送氣源 (52)回收槽 (23)第一輸送轉接器 (53)氣體出口 (24)輸送管路 (60)非偶合定風量控制單元 (25)第二輸送轉接器 (61)流量計 (26)第三輸送轉接器 (62)流量控制器 (27)第四輸送轉接器 (63)變頻器 -15- M347225 (64)非偶合平衡管 (76)溶劑回收管 (65)製程機台風機 (77)排水管 (70)固定床式溶劑回收單元 (78)回收槽 (71)固定吸附床 (80)冷凝吸收預處理單元 (72)吸附材 (81)冷凝盤管 (73)蒸氣源 (82)除霧器 (74)排氣管 (83)回收槽 (75)冷凝分離器 (84)溶劑回收管 -16--14- M347225 [Simple description of the diagram] The first diagram is a schematic diagram of the structure of a fluidized floating bed adsorption system (indicating the adsorption process). The second figure is a schematic diagram of the structure of a conventional fluidized floating bed adsorption system (description of the desorption process). The third figure is a schematic diagram of the structure of the non-coupling constant air volume control unit of the creation adsorption tower. The fourth figure is a schematic structural view of the present embodiment. p Figure 5, Figure A, B is not intended to be a relative relationship between the size of the spherical adsorbent and the perforated plate. [Explanation of main component symbols] (10) Adsorption tower (28) Feeding pipe (11) Perforated plate (30) Spherical adsorbent (12) Air flow dispersion plate (40) Desorption tower (13) Air flow inlet (41) With reaction chamber (14) exhaust fan (42) desorption heat source (15) air flow outlet (43) desorption gas source (20) adsorption material delivery device (44) desorption gas pipeline (21) discharge pipe (5 0 Condensation tower (22) conveying gas source (52) recovery tank (23) first conveying adapter (53) gas outlet (24) conveying line (60) non-coupling constant air volume control unit (25) second conveying Connector (61) Flowmeter (26) Third Delivery Adapter (62) Flow Controller (27) Fourth Delivery Adapter (63) Inverter -15- M347225 (64) Non-coupling Balance Tube (76) Solvent recovery tube (65) Process machine fan (77) Drain pipe (70) Fixed bed solvent recovery unit (78) Recovery tank (71) Fixed adsorption bed (80) Condensation absorption pretreatment unit (72) Adsorption material (81 Condensing coil (73) vapor source (82) defogger (74) exhaust pipe (83) recovery tank (75) condensing separator (84) solvent recovery tube - 16-