TWI558667B - Apparatus and method for the production of solution by concentrating volatile substances from steam stripping of wastewater - Google Patents
Apparatus and method for the production of solution by concentrating volatile substances from steam stripping of wastewater Download PDFInfo
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本發明涉及一種利用蒸汽汽提回收水中揮發性物質之質量傳送系統,該系統可使用一般旋轉填充床或夾層式旋轉填充床進行一種多階段(級)式蒸汽-溶液的質量傳送程序,以回收廢水中揮發性物質而轉製成包含該揮發性物質之高濃度溶液。 The invention relates to a mass transfer system for recovering volatile substances in water by steam stripping, which can perform a multi-stage (stage) steam-solution mass transfer process using a general rotary packed bed or a sandwich rotary packed bed to recover The volatile matter in the wastewater is converted into a high concentration solution containing the volatile material.
工業廢水或民生污水中常含有大量的揮發性物質,例如氨氮、氯化氫與揮發性有機化合物(Volatile Organic Compounds,VOCs)等,常見的揮發性有機化合物包含甲醇、乙醇、異丙醇、甲醛、乙醛、丙酮、甲酸和乙酸等。對於去除這些揮發性物質常見的處理方法,包括吸附法、生物處理、空氣吹脫和氧化法等,但是這些方法通常存在著操作成本高或是去除效果不好等缺點。其中,空氣吹脫為物理法,其係將揮發性物質由水相傳輸到氣相中,再使用其它溶液進行吸收濃縮,操作成本相對較低,但是可能會產生二次污染物;可以使用蒸汽來代替空氣來進行汽提,冷凝後可得到含有揮發性物質的濃縮溶液,但是若使用傳統的氣提塔或蒸餾塔都需要很高的蒸汽使用量,而且用以處理含揮發性物質濃度較低的廢水,不易獲得高濃度有經濟價值的回收溶液。 Industrial wastewater or residential sewage often contains a large amount of volatile substances, such as ammonia nitrogen, hydrogen chloride and volatile organic compounds (VOCs). Common volatile organic compounds include methanol, ethanol, isopropanol, formaldehyde, and acetaldehyde. , acetone, formic acid and acetic acid. Common treatment methods for removing these volatile substances include adsorption, biological treatment, air blowing and oxidation, but these methods usually have disadvantages such as high operating cost or poor removal effect. Among them, air blowing is a physical method, which transfers volatile substances from the aqueous phase to the gas phase, and then uses other solutions for absorption and concentration. The operating cost is relatively low, but secondary pollutants may be generated; steam may be used. Instead of air for stripping, a concentrated solution containing volatile substances can be obtained after condensation, but if a conventional stripper or distillation column is used, high steam usage is required, and the concentration of volatile substances is treated. Low wastewater, it is not easy to obtain high concentration and economic value of the recovery solution.
通常會以亨利常數(Henry's law,H)來表示揮發性污染物質的揮發度,亨利常數越高表示越容易揮發,通常可以下列方程式來表示:Pi=HiCL,i The volatility of volatile pollutants is usually expressed by Henry's law (H). The higher the Henry's constant, the more volatile it is. It is usually expressed by the following equation: P i =H i C L,i
其中,Pi為i物質的氣相分壓(atm),CL,i為i物質在溶液中的濃度(mol/m3),Hi(atm.m3/mol)為i物質的亨利常數。 Where P i is the gas phase partial pressure (atm) of the substance i , C L,i is the concentration of the substance i in the solution (mol/m 3 ), and H i (atm.m 3 /mol) is the substance of Henry constant.
i物質的亨利常數另一種形式為HC,i:CG,i=HC,iCL,i The other form of the Henry's constant of substance i is H C,i :C G,i =H C,i C L,i
其中,CG,i為i物質在氣相中的濃度(mol/m3),HC,i的單位為(mol.m3)/(mol.m3)。 Wherein C G,i is the concentration (mol/m 3 ) of the substance i in the gas phase, and the unit of H C,i is (mol.m 3 )/(mol.m 3 ).
HC,i=Hi/(RT) H C,i =H i /(RT)
其中,R為理想氣體常數,T為絕對溫度。 Where R is the ideal gas constant and T is the absolute temperature.
假設廢水流量為QL(m3/s),要將i物質完全從廢水移除至氣相,所需要理論最小氣體總流量QG(m3/s)為QL/HC。假設i物質完全由廢水傳輸至氣相且氣相只有蒸汽與i物質,根據理想氣體方程式,理論上蒸汽所需的最小莫爾流率(,mol/s)可計算得到如下
其中,P為氣相的壓力(atm)。 Where P is the pressure (atm) of the gas phase.
若原廢水中i物質的濃度不高,廢水中水的莫爾流率(,mol/s)約為QLρw/Mw,其中ρw和Mw分別為水的密度(約為1000kg/m3)與分子量(1.8 x 10-2kg/mol)。若i物質可完全從廢水傳輸至蒸汽相,其濃縮倍數理論上與/成正比。 If the concentration of substance i in the raw wastewater is not high, the Mohr flow rate of water in the wastewater ( , mol/s) is approximately Q L ρ w /M w , where ρ w and M w are the density of water (about 1000 kg/m 3 ) and the molecular weight (1.8 x 10 -2 kg/mol), respectively. If the substance i can be completely transported from the wastewater to the vapor phase, the concentration factor is theoretically / In direct proportion.
通常操作環境的P值接近1atm與溫度約為100℃,由上式可知當i物質在100℃時的H值若大於1.8x10-5atm.m3/mol,理論上即具有蒸汽 濃縮的可行性。表一係表示常見的揮發性物質在25℃左右時,其H值與水中溶解度的數值,然而100℃時的H值通常為25℃時的10到20倍左右,因此可知許多揮發性物質都具有進行蒸汽濃縮的可行性。 Generally, the P value of the operating environment is close to 1 atm and the temperature is about 100 ° C. From the above formula, the H value of the substance i at 100 ° C is greater than 1.8 x 10 -5 atm. m 3 /mol, in theory, has the feasibility of steam concentration. Table 1 shows the values of the H value and the solubility in water of a common volatile substance at around 25 ° C. However, the H value at 100 ° C is usually about 10 to 20 times that at 25 ° C. Therefore, many volatile substances are known. It has the feasibility of carrying out steam concentration.
一般工業生產和農業包含養殖畜牧等行業皆可能會產生氨氮廢水,根據台灣的工業技術研究院針對高科技產業所排放之氨氮廢水的水量及濃度分析,半導體產業12吋晶圓廠所排放之氨氮廢水的水量約為1000 CMD(m3/day)與濃度約為0.2wt.%,發光二極體(Light-Emitting Diode,LED)工廠之氨氮廢水的水量約為30 CMD與濃度約為2wt.%,印刷電路板(Printed Circuit Board,PCB)產業的氨銅製程之氨氮廢水的水量約為5 CMD與濃度約為7wt.%,太陽能光電產業的相關製 程之氨氮廢水的水量約為50 CMD與濃度約為1wt.%。總合而言,台灣高科技產業的氨氮廢水排放量接近每年一百萬噸與濃度約為1wt.%。 General industrial production and agriculture, including aquaculture and animal husbandry, may produce ammonia nitrogen wastewater. According to the analysis of the amount and concentration of ammonia nitrogen wastewater emitted by the Taiwan Industrial Technology Research Institute for high-tech industries, the ammonia nitrogen emitted by the semiconductor industry's 12-inch wafer fab. The water volume of the wastewater is about 1000 CMD (m 3 /day) and the concentration is about 0.2 wt.%, and the ammonia nitrogen wastewater of the Light-Emitting Diode (LED) factory has a water volume of about 30 CMD and a concentration of about 2 wt. %, the amount of ammonia nitrogen wastewater in the ammonia-copper process of the Printed Circuit Board (PCB) industry is about 5 CMD and the concentration is about 7 wt.%, and the amount of ammonia-nitrogen wastewater in the solar photovoltaic industry is about 50 CMD. The concentration is about 1 wt.%. In summary, Taiwan's high-tech industry's ammonia nitrogen wastewater discharge is close to 1 million tons per year and the concentration is about 1wt.%.
廢水中的氨氮是指以氨(NH3)或銨離子(NH4 +)形式存在的化合物,氨氮對水生生物會產生毒害,氨氮也會被微生物分解而消耗水體中的溶氧,而導致水體發黑或發臭。氨氮在氧氣充足的情況下,可被微生物氧化成亞硝酸鹽氮,進而分解為硝酸鹽氮。在自然的環境中,亞硝酸鹽氮可能會與蛋白質結合生成具有致癌和致畸作用的亞硝胺,而危害人體健康。另一方面,氨氮可為藻類及水草的生長提供氮營養源,可導致某些水生植物如海藻及水草的大量繁殖而產生優養化現象。此外,氨氮廢水亦會對某些工業設備產生危害,如會腐蝕某些金屬如銅及促使微生物在輸水管道和用水設備中大量繁殖而形成生物垢,導致管道和設備的堵塞。由此可知氨氮對水環境會造成嚴重的危害,要如何有效處理含氨氮廢水以降低其對水環境的影響已經是當前的重要課題。 The ammonia nitrogen in the wastewater refers to a compound in the form of ammonia (NH 3 ) or ammonium ion (NH 4 + ). The ammonia nitrogen is toxic to aquatic organisms, and the ammonia nitrogen is also decomposed by microorganisms to consume dissolved oxygen in the water body, resulting in water body. Black or stinky. Ammonia nitrogen can be oxidized by microorganisms to nitrite nitrogen in the presence of sufficient oxygen to decompose into nitrate nitrogen. In a natural environment, nitrite nitrogen may combine with proteins to form nitrosamines that are carcinogenic and teratogenic, and endanger human health. On the other hand, ammonia nitrogen can provide a nitrogen nutrient source for the growth of algae and aquatic plants, which can lead to the proliferation of certain aquatic plants such as seaweed and aquatic plants. In addition, ammonia-nitrogen wastewater can also cause damage to certain industrial equipment, such as corrosion of certain metals such as copper and the proliferation of microorganisms in water pipelines and water equipment to form bioscale, leading to blockage of pipelines and equipment. It can be seen that ammonia nitrogen can cause serious harm to the water environment. How to effectively treat ammonia-containing wastewater to reduce its impact on the water environment has become an important issue at present.
目前已有數種方法用於去除廢水中的氨氮,包含有(一)氣提法:是在鹼性水質(高pH值)下利用氣液質量傳送效應,將空氣通入含氨氮之廢水中,將氨由水相中氣提出來。一般會使用氣提塔來進行,分離出來之氣態氨可用酸來進行吸收,但可能會衍生出二次污染物的問題;(二)化學沉澱法:在一定的pH條件下,添加鎂離子(Mg2+)、磷酸根(HPO4 3-)和NH4 +可以生成磷酸銨鎂(MgNH4PO4)的沉澱,而使銨離子從水中分離出來。化學沉澱法的主要問題是沉澱劑的用量大、鎂鹽費用高,另外所生成的沉澱顆粒細小或是產生絮狀體,在進行固液分離時具有一定困難度;(三)離子交換法:主要是利用離子交換程序將廢水中之銨離子進行置換去除,但廢水中若含有具氧化性物質,可能會傷害離子交換樹脂而造成處理效率降低,此外後續還有離子交換樹脂再 生及廢棄等問題,使得處理成本增加;(四)逆滲透法:利用逆滲透膜將氨離子濃縮,逆滲透膜可將氨離子阻絕而產出低濃度氨氮產出水,但設置成本較高且逆滲透膜孔徑小易因廢水中雜質或有機物造成堵塞而降低產水率,也可能因廢水中其他化學物質破壞逆滲透膜,而增加操作困難度與提高處理成本;(五)生物處理:於廢水中培養適當之微生物,藉由微生物之代謝作用將氨氮去除。生物處理除氮方法主要包含二個步驟,先藉由氨氧化菌與亞硝酸氧化菌將氨氮氧化成硝酸氮,之後再由脫氮菌將硝酸氮還原成氮氣而達到去除的效果。雖然生物脫氮是目前常用的方法之一,但是佔地面積大而且對高濃度或間斷性的氨氮廢水會有操作上的困難,也有後續污泥處理的問題與費用;及(六)薄膜蒸餾技術:薄膜蒸餾技術為提高廢水溫度後流經多孔且疏水性薄膜一側,薄膜另一側以低溫酸性溶液進行循環,以薄膜兩側流體接觸面之氨氮蒸氣壓差為趨動力,使氨氮蒸氣分子通過薄膜孔洞,由高溫廢水側傳輸到低溫酸性溶液側而被吸收成含銨鹽液體,但同樣地可能會有衍生出二次污染物的問題。 At present, there are several methods for removing ammonia nitrogen from wastewater, including (1) stripping method: using the gas-liquid mass transfer effect under alkaline water quality (high pH value), the air is introduced into the wastewater containing ammonia nitrogen. Ammonia is extracted from the gas in the aqueous phase. Generally, the stripping tower is used for the separation, and the separated gaseous ammonia can be absorbed by the acid, but the secondary pollutant may be derived; (2) the chemical precipitation method: adding magnesium ions under a certain pH condition ( Mg 2+ ), phosphate (HPO 4 3- ) and NH 4 + can form a precipitate of magnesium ammonium phosphate (MgNH 4 PO 4 ), which separates the ammonium ions from the water. The main problems of the chemical precipitation method are the large amount of precipitant and the high cost of magnesium salt. In addition, the precipitated particles formed are fine or floccules are formed, which has certain difficulty in solid-liquid separation; (3) Ion exchange method: It mainly uses the ion exchange program to replace and remove the ammonium ions in the wastewater. However, if the wastewater contains oxidizing substances, it may damage the ion exchange resin and cause the treatment efficiency to decrease. In addition, there are problems such as regeneration and disposal of the ion exchange resin. In order to increase the processing cost; (4) Reverse osmosis method: the reverse osmosis membrane is used to concentrate the ammonia ions, and the reverse osmosis membrane can block the ammonia ions to produce low-concentration ammonia nitrogen to produce water, but the installation cost is high and the reverse osmosis membrane pore size Xiaoyi reduces the water production rate due to clogging of impurities or organic matter in the wastewater, and may also damage the reverse osmosis membrane due to other chemical substances in the wastewater, thereby increasing the difficulty of operation and increasing the treatment cost; (5) Biological treatment: appropriate cultivation in wastewater The microorganism removes ammonia nitrogen by the metabolism of microorganisms. The biological treatment nitrogen removal method mainly comprises two steps. First, the ammonia nitrogen is oxidized to nitrogen nitrate by the ammonia oxidizing bacteria and the nitrous acid oxidizing bacteria, and then the nitrogen nitrogen is reduced to nitrogen by the denitrifying bacteria to achieve the removal effect. Although biological nitrogen removal is one of the commonly used methods, it has a large footprint and has operational difficulties for high-concentration or intermittent ammonia-nitrogen wastewater, as well as problems and costs of subsequent sludge treatment; and (6) thin film distillation Technology: The thin film distillation technology flows through the porous and hydrophobic film side after increasing the temperature of the wastewater, and the other side of the film is circulated with a low-temperature acidic solution, and the ammonia nitrogen vapor pressure difference between the fluid contact surfaces on both sides of the film is the driving force, so that the ammonia nitrogen vapor The molecules are absorbed into the ammonium salt-containing liquid through the pores of the film and transported from the high-temperature wastewater side to the low-temperature acidic solution side, but similarly there may be a problem of secondary pollutants being derived.
異丙醇常用於油漆、稀釋劑、塗料、清潔劑、表面殺菌、食品加工廠等相關行業,異丙醇為目前半導體製程所排放最大宗的廢有機溶劑。在柔印、平版印刷和凹版印刷程序中,異丙醇亦作為溶劑與設備清潔劑。此外,光電產業在清洗段製程中也會產生大量含異丙醇的有機廢水。異丙醇的排放不但會污染環境,且因為異丙醇是一種光化學氧化劑,在受到陽光照射下會形成臭氧而刺激人的眼睛和呼吸系統,危害人類身體健康和植物生長。 Isopropanol is commonly used in paints, thinners, coatings, detergents, surface sterilization, food processing plants and other related industries. Isopropanol is the largest waste organic solvent in current semiconductor processes. Isopropanol is also used as a solvent and equipment cleaner in flexo, lithographic and gravure printing processes. In addition, the photovoltaic industry will also produce a large amount of organic wastewater containing isopropanol in the cleaning stage process. Isopropanol emissions not only pollute the environment, but because isopropyl alcohol is a photochemical oxidant that forms ozone when exposed to sunlight, irritating the eyes and respiratory system, endangering human health and plant growth.
超重力技術是強化氣體與液體之質量傳送程序之創新技術,主要特點是在為地球重力場之數十倍至數百倍的離心加速度環境下,液體會在填充物的表面與孔隙處分散成微小的液滴、液膜及液絲進行由內徑向外徑的流動,而增加了氣液接觸的比表面積。也因為氣液之間 的微觀劇烈混合作用,可提高氣液接觸的比表面積與降低氣液之間的質量傳送阻力,因此達到增加氣液質量傳送速率與減少反應器體積之目的。相較於傳統的蒸汽與液體的接觸裝置,例如汽提塔或蒸餾塔,超重力反應器單位體積的質量傳送速率可提高數十倍至數百倍,因而顯著減少反應器所需的設備體積與可用於處理較大流量的廢水,同時可以減少蒸汽使用量。 Hypergravity technology is an innovative technology that enhances the mass transfer process of gases and liquids. The main feature is that in the centrifugal acceleration environment of tens to hundreds of times the Earth's gravitational field, the liquid will be dispersed at the surface and pores of the filler. The tiny droplets, liquid film and liquid filament carry out the flow from the inner radial outer diameter, increasing the specific surface area of the gas-liquid contact. Also because of gas and liquid The micro-violent mixing effect can increase the specific surface area of the gas-liquid contact and reduce the mass transfer resistance between the gas and liquid, thereby achieving the purpose of increasing the gas-liquid mass transfer rate and reducing the reactor volume. Compared to conventional steam-liquid contact devices, such as stripping columns or distillation columns, the mass transfer rate per unit volume of a supergravity reactor can be increased by tens to hundreds of times, thus significantly reducing the equipment volume required for the reactor. It can be used to treat large volumes of wastewater while reducing steam usage.
含有揮發性物質的回收溶液一般必須達到較高濃度數值,才具有進行後續純化再利用的經濟價值。例如濃縮回收氨水濃度需在20wt.%以上,通常才適合進一步提純轉製成工業用的氨水。目前對於低濃度如數百或數千mg/L的氨氮廢水,要轉製成高濃度(>20wt.%)的氨水仍需要開發新穎的處理程序。相同道理,若要進行揮發性有機物質(如異丙醇)的回收利用,所回收的有機物質溶液亦需要達到數十個wt.%以上,才有再進行後續純化再利用的經濟效益。 The recovery solution containing volatile substances generally must reach a higher concentration value in order to have the economic value of subsequent purification and reuse. For example, the concentrated ammonia water concentration should be above 20 wt.%, and it is usually suitable for further purification of ammonia water for industrial conversion. At present, for ammonia nitrogen wastewater with low concentrations such as hundreds or thousands of mg/L, it is still necessary to develop a novel treatment process to convert to a high concentration (>20 wt.%) of ammonia water. By the same token, if the volatile organic substances (such as isopropyl alcohol) are to be recycled, the recovered organic matter solution needs to reach tens of wt.% or more, and the economic benefits of subsequent purification and reuse can be achieved.
本發明使用蒸汽汽提進行廢水中揮發性物質的回收,具有高回收效率、製程簡單及佔地面積小等優點,且可有效降低廢水中揮發性物質的含量以減輕環境負荷,同時達到資源循環再利用與提高回收溶液之經濟價值之目的。 The invention adopts steam stripping to recover volatile substances in waste water, has the advantages of high recovery efficiency, simple process and small occupied area, and can effectively reduce the content of volatile substances in waste water to reduce environmental load and achieve resource recycling. Reuse and increase the economic value of the recovered solution.
本發明係提供一種以蒸汽汽提廢水以濃縮製備揮發性物質之溶液之方法,其包含將蒸汽及含揮發性物質之廢水通入旋轉填充床裝置中,使該蒸汽及該廢水在該旋轉填充床裝置中進行汽液質量傳送程序;及將離開該旋轉填充床裝置的氣體冷凝收集成含揮發性物質之溶液。 The invention provides a method for preparing a volatile substance by steam stripping wastewater, which comprises introducing steam and volatile matter-containing wastewater into a rotary packed bed device, and the steam and the waste water are filled in the rotation The vapor-liquid mass transfer procedure is performed in the bed apparatus; and the gas leaving the rotating packed bed apparatus is condensed and collected into a solution containing a volatile substance.
本發明另提供一種夾層式旋轉填充床裝置,該夾層式旋轉填充床裝置可取代上述方法中所使用的旋轉填充床裝置,該裝置包括一內層殼體,其具有一氣體開口,並設有一蒸汽通入管及一液體排出管; 一外層殼體,其與該內層殼體之間隔界定出一外層中空腔體,該外層中空腔體與該氣體開口相連通,並設有一流體出口,該外層中空腔體包覆該內層殼體與該氣體開口;一旋轉填充床,其設於該內層殼體內,該旋轉填充床包括一腔體,該腔體內以固體填充件填充;一貫穿該內層殼體的旋轉心軸,其與該旋轉填充床耦合,使該旋轉填充床可相對於該內層殼體進行旋轉;及一液體通入管,該液體通入管穿過該氣體開口,且其具有噴液開口,該噴液開口設置於一中間通道中;所通入的蒸汽將依序通過該旋轉填充床、該氣體開口、該外層中空腔體、該流體出口連接到外部管線;其中,該蒸汽通入管、該液體排出管及該液體通入管穿過該外層殼體。 The present invention further provides a sandwich type rotating packed bed device which can replace the rotary packed bed device used in the above method, the device comprising an inner layer casing having a gas opening and provided with a a steam inlet pipe and a liquid discharge pipe; An outer casing defining a space between the outer casing and an outer casing, wherein the outer cavity is in communication with the gas opening and is provided with a fluid outlet, wherein the outer cavity covers the inner layer a housing and the gas opening; a rotating packed bed disposed in the inner casing, the rotating packed bed comprising a cavity filled with a solid filling member; a rotating mandrel extending through the inner casing Coupling with the rotating packed bed to rotate the rotating packed bed relative to the inner casing; and a liquid passage pipe passing through the gas opening and having a liquid discharge opening The liquid opening is disposed in an intermediate passage; the introduced steam will sequentially pass through the rotating packed bed, the gas opening, the outer cavity, and the fluid outlet connected to the external line; wherein the steam is passed into the tube, the liquid A discharge tube and the liquid passage tube pass through the outer casing.
在本發明中,揮發性物質回收製程的形式可根據廢水中揮發性物質的初始濃度與回收溶液的目標濃度而決定。 In the present invention, the form of the volatile matter recovery process can be determined based on the initial concentration of the volatile matter in the wastewater and the target concentration of the recovered solution.
本發明提供之夾層式旋轉填充床裝置及以蒸汽汽提廢水以濃縮製備含高濃度揮發性物質之溶液之方法,將可藉由下列實施方式說明及附圖而進一步瞭解。 The present invention provides a sandwich type rotary packed bed apparatus and a method for preparing a solution containing a high concentration of volatile substances by steam stripping wastewater, which will be further understood by the following description of the embodiments and the accompanying drawings.
本發明亦涵蓋其他方面及具體實施例。前述發明內容及以下實施方式並無意將本發明侷限於任何特定具體實施例,而係僅計畫描述本發明之一些具體實施例。 Other aspects and specific embodiments are also contemplated by the present invention. The above summary of the invention and the following embodiments are not intended to limit the invention to any particular embodiments.
A‧‧‧含揮發性物質廢水 A‧‧‧ Wastewater containing volatile substances
B‧‧‧調整藥劑 B‧‧‧Adjustment
C‧‧‧蒸汽 C‧‧‧Steam
D‧‧‧出流水 D‧‧‧Outflow
E‧‧‧回收溶液 E‧‧‧Recovery solution
F‧‧‧尾氣 F‧‧‧Exhaust
1‧‧‧旋轉填充床裝置 1‧‧‧Rotary packed bed device
2‧‧‧外殼 2‧‧‧ Shell
3‧‧‧旋轉填充床 3‧‧‧Rotary packed bed
4‧‧‧上蓋 4‧‧‧Upper cover
5‧‧‧殼體 5‧‧‧Shell
6‧‧‧底板 6‧‧‧floor
7‧‧‧旋轉心軸 7‧‧‧Rotating mandrel
8‧‧‧多孔內環 8‧‧‧Porous inner ring
9‧‧‧多孔外環 9‧‧‧Porous outer ring
10‧‧‧中空上蓋 10‧‧‧ hollow cover
11‧‧‧底盤 11‧‧‧Chassis
12‧‧‧固體填充件 12‧‧‧solid filling parts
13‧‧‧氣體排出管 13‧‧‧ gas discharge pipe
14‧‧‧液體通入管 14‧‧‧Liquid access tube
15‧‧‧噴液開口 15‧‧‧spray opening
16‧‧‧旋轉密封元件 16‧‧‧Rotary sealing element
17‧‧‧蒸汽通入管 17‧‧‧Steam access tube
18‧‧‧液體排出管 18‧‧‧Liquid drain
19‧‧‧中空腔體 19‧‧‧ hollow body
20‧‧‧夾層式旋轉填充床裝置 20‧‧‧Mezzanine rotary packed bed device
21‧‧‧外層殼體 21‧‧‧ outer shell
22‧‧‧內層殼體 22‧‧‧ Inner shell
23‧‧‧旋轉填充床 23‧‧‧Rotary packed bed
24‧‧‧多孔內環 24‧‧‧Porous inner ring
25‧‧‧多孔外環 25‧‧‧Porous outer ring
26‧‧‧中空上蓋 26‧‧‧ hollow cover
27‧‧‧底盤 27‧‧‧Chassis
28‧‧‧旋轉心軸 28‧‧‧Rotating mandrel
29‧‧‧固體填充件 29‧‧‧solid filling parts
30‧‧‧內上蓋 30‧‧‧With cover
31‧‧‧內殼體 31‧‧‧ inner casing
32‧‧‧內底板 32‧‧‧Inner backplane
33‧‧‧旋轉密封元件 33‧‧‧Rotary sealing element
34‧‧‧蒸汽通入管 34‧‧‧Steam access pipe
35‧‧‧液體排出管 35‧‧‧Liquid drain
36‧‧‧氣體開口 36‧‧‧ gas opening
37‧‧‧液體通入管 37‧‧‧Liquid access tube
38‧‧‧中間通道 38‧‧‧Intermediate passage
39‧‧‧噴液開口 39‧‧‧spray opening
40‧‧‧外上蓋 40‧‧‧Outer cover
41‧‧‧外殼體 41‧‧‧Outer casing
42‧‧‧外底板 42‧‧‧Outer floor
43‧‧‧流體出口 43‧‧‧ Fluid outlet
44‧‧‧外層中空腔體 44‧‧‧ Outer hollow body
45‧‧‧內層中空腔體 45‧‧‧Inner hollow body
100‧‧‧調整槽 100‧‧‧ adjustment slot
110‧‧‧泵浦 110‧‧‧ pump
120‧‧‧廢水熱交換器 120‧‧‧Waste water heat exchanger
130‧‧‧第一級旋轉填充床 130‧‧‧First-stage rotating packed bed
140‧‧‧第一級冷凝器 140‧‧‧First stage condenser
150‧‧‧第一級回收溶液儲槽 150‧‧‧First-stage recovery solution storage tank
160‧‧‧熱交換器 160‧‧‧ heat exchanger
170‧‧‧旋轉填充床 170‧‧‧Rotary packed bed
310‧‧‧第二級旋轉填充床 310‧‧‧Second stage rotating packed bed
320‧‧‧第二級冷凝器 320‧‧‧Second stage condenser
330‧‧‧第二級回收溶液儲槽 330‧‧‧Second grade recovery solution storage tank
410‧‧‧第三級旋轉填充床 410‧‧‧third-stage rotating packed bed
420‧‧‧第三級冷凝器 420‧‧‧third stage condenser
430‧‧‧第三級回收溶液儲槽 430‧‧‧ third-stage recovery solution storage tank
圖1是旋轉填充床之結構示意圖。 Figure 1 is a schematic view of the structure of a rotating packed bed.
圖2是一級式廢水回收製程之示意圖。 Figure 2 is a schematic diagram of a primary wastewater recovery process.
圖3是二級式廢水回收製程之示意圖。 Figure 3 is a schematic diagram of a two-stage wastewater recovery process.
圖4是三級式廢水回收製程之示意圖。 Figure 4 is a schematic diagram of a three-stage wastewater recovery process.
圖5是夾層式旋轉填充床之結構示意圖。 Figure 5 is a schematic view showing the structure of a sandwich type rotating packed bed.
本發明提出一種以蒸汽汽提廢水中揮發性物質來濃縮製備揮發 性物質溶液之回收系統,依照所處理廢水中的原始揮發性物質濃度,搭配合適的多階段(級)式程序設計,並可利用旋轉填充床裝置的高汽液質量傳送效率與保溫效果,來回收廢水中的揮發性物質而得到含高濃度揮發性物質的溶液。 The invention provides a method for preparing volatiles by concentrating volatile substances in steam stripping wastewater The recovery system of the substance solution is designed according to the concentration of the original volatile substances in the treated wastewater, combined with a suitable multi-stage (stage) program design, and can utilize the high vapor-liquid mass transfer efficiency and the heat preservation effect of the rotary packed bed device. The volatile matter in the wastewater is recovered to obtain a solution containing a high concentration of volatile matter.
圖1係顯示一種使用於本發明以蒸汽汽提廢水中揮發性物質來濃縮製備揮發性物質溶液之旋轉填充床裝置1,該旋轉填充床裝置1包括且較佳為圓柱形的外殼2;一個旋轉填充床3,其設於該外殼2內。該外殼2包括上蓋4、殼體5及底板6所構成;該上蓋4及該底板6分別與該殼體5之上緣、下緣結合,一旋轉心軸7貫穿該底板6中央。該旋轉心軸7係利用一馬達(未顯示)驅動進行旋轉,帶動該旋轉填充床3相對於該外殼2進行旋轉。該旋轉填充床3包括一個多孔內環8、一個多孔外環9、一個中空上蓋10、一個底盤11所組成,該多孔內環8及該多孔外環9則與該底盤11耦合、而該底盤11與該旋轉心軸7耦合。該旋轉填充床3具有一腔體,界定於該多孔內環8及該多孔外環9之間,該腔體內以固體填充件12填充,該固體填充件12的材質可選用不鏽鋼、纖維、氧化鋁、樹脂、塑膠、沸石、矽膠、活性炭、鐵氟龍等至少其中之一,其中以不鏽鋼材質較佳。該多孔內環8與該多孔外環9之間藉由若干孔洞相互連通。該旋轉填充床3的旋轉速度可視需要調整,較佳地,該旋轉填充床3的旋轉速度為150至3000rpm。該旋轉填充床3之該中空上蓋10設有一氣體排出管13,該氣體排出管13穿過該上蓋4,一液體通入管14進入到該氣體排出管13中,該液體通入管14的噴液開口15位於該旋轉填充床3的多孔內環8之內側。該旋轉填充床3的上方與該氣體排出管13之間有旋轉密封元件16,以避免進入該殼體5的蒸汽未通過該旋轉填充床3,而直接由該氣體排出管13排出。該旋轉填充床裝置1設有蒸汽通入管17和液體排出管18,該氣體排出管13、該蒸汽通入管17和該液體排出管18皆穿出該殼體5而與外界管線相連接,該液 體通入管14則穿出該氣體排出管13與外界管線相連接。該旋轉填充床裝置1包括一中空腔體19,該中空腔體介於該殼體5與該旋轉填充床3之間。 Figure 1 shows a rotary packed bed apparatus 1 for use in the present invention for concentrating a volatile matter solution in a steam stripping wastewater, the rotating packed bed apparatus 1 comprising and preferably a cylindrical outer casing 2; A packed bed 3 is rotated, which is disposed in the outer casing 2. The outer casing 2 comprises an upper cover 4, a casing 5 and a bottom plate 6; the upper cover 4 and the bottom plate 6 are respectively coupled with the upper edge and the lower edge of the casing 5, and a rotating mandrel 7 penetrates the center of the bottom plate 6. The rotary mandrel 7 is driven to rotate by a motor (not shown) to rotate the rotary packed bed 3 relative to the outer casing 2. The rotary packed bed 3 comprises a porous inner ring 8, a porous outer ring 9, a hollow upper cover 10, and a chassis 11, the porous inner ring 8 and the porous outer ring 9 being coupled to the chassis 11, and the chassis 11 is coupled to the rotating mandrel 7. The rotating packed bed 3 has a cavity defined between the porous inner ring 8 and the porous outer ring 9. The cavity is filled with a solid filling member 12, and the material of the solid filling member 12 can be selected from stainless steel, fiber, and oxidation. At least one of aluminum, resin, plastic, zeolite, silicone, activated carbon, Teflon, etc., of which stainless steel is preferred. The porous inner ring 8 and the porous outer ring 9 communicate with each other through a plurality of holes. The rotational speed of the rotary packed bed 3 can be adjusted as needed. Preferably, the rotational speed of the rotary packed bed 3 is 150 to 3000 rpm. The hollow upper cover 10 of the rotary packed bed 3 is provided with a gas discharge pipe 13 through which the gas discharge pipe 13 passes, and a liquid passage pipe 14 enters the gas discharge pipe 13, and the liquid discharge pipe 14 is sprayed. The opening 15 is located inside the porous inner ring 8 of the rotating packed bed 3. A rotary sealing member 16 is disposed between the upper portion of the rotary packed bed 3 and the gas discharge pipe 13 to prevent steam entering the casing 5 from passing through the rotary packed bed 3 and directly discharged from the gas discharge pipe 13. The rotary packed bed device 1 is provided with a steam inlet pipe 17 and a liquid discharge pipe 18, and the gas discharge pipe 13, the steam inlet pipe 17, and the liquid discharge pipe 18 are all passed out of the casing 5 to be connected to an external pipeline. liquid The body passage pipe 14 is passed through the gas discharge pipe 13 and connected to the outside line. The rotary packed bed apparatus 1 comprises a hollow body 19 interposed between the housing 5 and the rotating packed bed 3.
本發明以處理含氨氮或異丙醇的廢水作為實施例,說明濃縮製備高濃度氨水或異丙醇水溶液之方法及裝置,可參考圖2、3與4。在本發明的一種態樣中,係用一種多階段(級)式廢水中揮發性物質回收系統以獲得較高之溶液濃度,該系統包括二個以上的旋轉填充床、二個以上的熱交換器、一個以上的冷凝器、二個以上的液體泵浦與一個蒸汽供應系統。 The invention treats wastewater containing ammonia nitrogen or isopropanol as an example, and describes a method and a device for preparing a high concentration aqueous ammonia or isopropyl alcohol solution by concentration, and can refer to FIGS. 2, 3 and 4. In one aspect of the invention, a volatile matter recovery system in a multi-stage (stage) type of wastewater is used to obtain a higher solution concentration, the system comprising more than two rotating packed beds, more than two heat exchanges , more than one condenser, more than two liquid pumps and a steam supply system.
圖2是一級式含揮發性物質廢水回收製程之示意圖,含揮發性物質廢水A在調整槽100中進行性質調整(通入調整藥劑B),再利用液體泵浦110把含揮發性物質的廢水運輸通過一廢水熱交換器120提高廢水溫度後,從第一級旋轉填充床130的液體通入管中噴出,同時將蒸汽C導入第一級旋轉填充床130的蒸汽通入管中。經由該第一級旋轉填充床130的汽液質量傳送機制,將廢水中的揮發性物質傳送至蒸汽相,可顯著降低從該第一級旋轉填充床130排出的出流水D所含之揮發性物質濃度。含有揮發性物質的氣體離開該第一級旋轉填充床130後會連接到第一級冷凝器140(所使用的冷卻水未顯示,原始的廢水亦可作為冷卻水使用),將該氣體進行冷凝收集成一含揮發性物質的溶液儲存在第一級回收溶液儲槽150中。如果第一級冷凝器140有尚未被冷凝的氣體將導到一旋轉填充床170中,並將該第一級回收溶液儲槽150的溶液經過一熱交換器160進行冷卻後,導入該旋轉填充床170中來吸收該未被冷凝的氣體,而獲得一含揮發性物質之回收溶液E,並將尾氣F排出。 2 is a schematic diagram of a first-stage wastewater containing waste water recovery process, in which the volatile matter-containing wastewater A is adjusted in the conditioning tank 100 (passing the adjusting agent B), and then the liquid pump 110 is used to treat the volatile matter-containing wastewater. After the transportation is increased by the waste water heat exchanger 120 to raise the temperature of the wastewater, it is ejected from the liquid inlet pipe of the first stage rotating packed bed 130 while the steam C is introduced into the steam inlet pipe of the first stage rotating packed bed 130. By transferring the volatile matter in the wastewater to the vapor phase via the vapor-liquid mass transfer mechanism of the first-stage rotating packed bed 130, the volatility contained in the outflow D discharged from the first-stage rotating packed bed 130 can be significantly reduced. Substance concentration. After the volatile matter-containing gas leaves the first-stage rotating packed bed 130, it is connected to the first-stage condenser 140 (the cooling water used is not shown, and the original wastewater can also be used as cooling water), and the gas is condensed. The solution collected as a volatile substance is stored in the first stage recovery solution storage tank 150. If the first stage condenser 140 has a gas that has not been condensed, it will be led to a rotating packed bed 170, and the solution of the first stage recovery solution storage tank 150 is cooled by a heat exchanger 160, and then introduced into the rotary filling. The bed 170 absorbs the uncondensed gas to obtain a recovery solution E containing a volatile substance, and discharges the exhaust gas F.
若使用上述一級式廢水回收製程所得到含揮發性物質之回收溶液之濃度仍不夠高,將採用二級式(圖3)或三級式(圖4)含揮發性物質 廢水回收製程。相較於前述一級式廢水回收製程,二級式廢水回收製程是將該第一級回收溶液儲槽150的溶液導入第二級旋轉填充床310中(圖3),同時將新鮮蒸汽C導入該第二級旋轉填充床310中,使用新鮮蒸汽C可確保該第二級旋轉填充床310之高及穩定的氨氮去除效率。含有揮發性物質的氣體離開該第二級旋轉填充床310後會連接到第二級冷凝器320,將該氣體進行冷凝收集得到一更高濃度的揮發性物質溶液,並儲存在第二級回收溶液儲槽330中。從該第二級旋轉填充床310所流出的水溶液可直接放流或再導回該調整槽100中。如果該第一級冷凝器140與該第二級冷凝器320有尚未被冷凝的氣體將導到一旋轉填充床170中,並將該第二級回收溶液儲槽330的溶液經過一熱交換器160進行冷卻後,導入該旋轉填充床170中用來吸收該未被冷凝的氣體,而製備出比使用前述一級式廢水回收製程更高濃度揮發性物質之回收溶液E。 If the concentration of the volatile matter-containing recovery solution obtained by using the above-mentioned primary wastewater recovery process is still not high enough, the secondary (Fig. 3) or tertiary (Fig. 4) volatile substances will be used. Waste water recycling process. Compared with the first-stage wastewater recovery process, the secondary wastewater recovery process introduces the solution of the first-stage recovery solution storage tank 150 into the second-stage rotary packed bed 310 (Fig. 3), and introduces the fresh steam C into the In the second stage of rotating packed bed 310, the use of fresh steam C ensures high and stable ammonia nitrogen removal efficiency of the second stage rotating packed bed 310. After the volatile matter-containing gas leaves the second-stage rotating packed bed 310, it is connected to the second-stage condenser 320, and the gas is condensed and collected to obtain a higher concentration volatile matter solution, and stored in the second-stage recycling. In solution reservoir 330. The aqueous solution flowing out of the second stage rotating packed bed 310 can be directly discharged or redirected back into the conditioning tank 100. If the first stage condenser 140 and the second stage condenser 320 have gas that has not been condensed, the gas will be led to a rotating packed bed 170, and the solution of the second stage recovery solution storage tank 330 is passed through a heat exchanger. After cooling 160, it is introduced into the rotating packed bed 170 for absorbing the uncondensed gas to prepare a recovery solution E which is higher in concentration than the volatile matter used in the first-stage wastewater recovery process.
相較於上述二級式廢水回收製程,三級式廢水回收製程是將該第二級回收溶液儲槽330的溶液再導入第三級旋轉填充床410中(圖4),同時將新鮮蒸汽C導入該第三級旋轉填充床410中。含有氨氮的蒸汽離開該第三級旋轉填充床410後會連接到第三級冷凝器420,將該氣體進行冷凝收集得到一濃度更高的含揮發性物質溶液,並儲存在第三級回收溶液儲槽430中。從該第三級旋轉填充床410所流出的水溶液可直接放流或再導回該調整槽100或該第一級回收溶液儲槽150中。如果該第一級冷凝器140、該第二級冷凝器320與該第三級冷凝器420有尚未被冷凝的氣體將導到一旋轉填充床170中,並將該第三級回收溶液儲槽430的溶液經過該熱交換器160進行冷卻後,導入該旋轉填充床170中用來吸收該未被冷凝的氣體,而製備出比前述二級式廢水回收製程更高濃度揮發性物質之回收溶液E。 Compared with the above-mentioned two-stage waste water recovery process, the three-stage waste water recovery process re-introduces the solution of the second-stage recovery solution storage tank 330 into the third-stage rotary packed bed 410 (Fig. 4), and simultaneously fresh steam C. Introduced into the third stage rotating packed bed 410. After the ammonia-containing steam leaves the third-stage rotating packed bed 410, it is connected to the third-stage condenser 420, and the gas is condensed and collected to obtain a higher concentration volatile matter solution and stored in the third-stage recovery solution. In the tank 430. The aqueous solution flowing from the third stage rotating packed bed 410 can be directly discharged or re-conducted back into the conditioning tank 100 or the first stage recovery solution storage tank 150. If the first stage condenser 140, the second stage condenser 320 and the third stage condenser 420 have not yet condensed gas will be led to a rotating packed bed 170, and the third stage recovery solution storage tank After the solution of 430 is cooled by the heat exchanger 160, it is introduced into the rotating packed bed 170 for absorbing the uncondensed gas, thereby preparing a recovery solution of a higher concentration of volatile substances than the second-stage wastewater recovery process. E.
視需要,可使用超過三階段(級)之多級式廢水中揮發性物質回收 系統。 Volatile material recovery in multi-stage wastewater over three stages (grades), if required system.
此外,蒸汽的質量流率與廢水的質量流率之比值大小會影響廢水中污染物的去除效率及回收溶液中揮發性物質的濃度。該比值較大的時候(例如,大於0.25kg/kg),可以得到較高的廢水中揮發性物質去除效率,但是所得到回收溶液中揮發性物質的濃度會較低;該比值較小的時候(例如,小於0.25kg/kg),會得到較低的廢水中揮發性物質去除效率,但是所得到回收溶液中揮發性物質的濃度會較高。 In addition, the ratio of the mass flow rate of steam to the mass flow rate of wastewater affects the removal efficiency of pollutants in the wastewater and the concentration of volatiles in the recovered solution. When the ratio is large (for example, greater than 0.25 kg/kg), the removal efficiency of the volatile matter in the wastewater can be obtained, but the concentration of the volatile matter in the recovered solution is lower; when the ratio is small (for example, less than 0.25 kg/kg), the lower volatile matter removal efficiency in the wastewater is obtained, but the concentration of the volatile matter in the recovered solution is higher.
在本發明中,各階段(級)中蒸汽的質量流率與廢水的質量流率之比值約為0.01至0.5kg/kg,較佳係為0.05至0.4kg/kg。本發明建議對於含低濃度揮發性物質的廢水可使用較低蒸汽的質量流率與廢水的質量流率之比值,因為原本廢水中揮發性物質濃度低,不需要高的揮發性物質去除效率,而可以得到較高濃度揮發性物質的回收溶液。 In the present invention, the ratio of the mass flow rate of steam in each stage (stage) to the mass flow rate of the wastewater is about 0.01 to 0.5 kg/kg, preferably 0.05 to 0.4 kg/kg. The invention proposes that the ratio of the mass flow rate of the lower steam to the mass flow rate of the waste water can be used for the wastewater containing the low concentration volatile matter, because the concentration of the volatile matter in the original waste water is low, and high volatile matter removal efficiency is not required. A recovery solution of a higher concentration of volatile substances can be obtained.
圖5所示的夾層式旋轉填充床裝置係為本發明的一種態樣,夾層式旋轉填充床裝置20包括且較佳為圓柱形的外層殼體21和內層殼體22;一個旋轉填充床23,其設於該內層殼體22內,且可相對於該內層殼體22進行旋轉。該旋轉填充床23包括一個多孔內環24、一個多孔外環25、一個中空上蓋26、一個底盤27所組成,該多孔內環24及該多孔外環25則與該底盤27耦合、而該底盤27與一旋轉心軸28耦合。該旋轉填充床23具有一腔體,界定於該多孔內環24及該多孔外環25之間,該腔體內以固體填充件29填充,該固體填充件29的材質可選用不鏽鋼、纖維、氧化鋁、樹脂、塑膠、沸石、矽膠、活性炭、鐵氟龍等至少其中之一,其中以不鏽鋼材質較佳。該多孔內環24與該多孔外環25之間藉由若干孔洞相互連通。 The sandwich type rotating packed bed apparatus shown in FIG. 5 is an aspect of the present invention, and the sandwich type rotary packed bed apparatus 20 includes and preferably has a cylindrical outer casing 21 and an inner casing 22; a rotating packed bed 23, which is disposed in the inner casing 22 and rotatable relative to the inner casing 22. The rotating packed bed 23 includes a porous inner ring 24, a porous outer ring 25, a hollow upper cover 26, and a chassis 27, the porous inner ring 24 and the porous outer ring 25 being coupled to the chassis 27, and the chassis 27 is coupled to a rotating mandrel 28. The rotating packed bed 23 has a cavity defined between the porous inner ring 24 and the porous outer ring 25. The cavity is filled with a solid filling member 29, and the material of the solid filling member 29 can be selected from stainless steel, fiber, and oxidation. At least one of aluminum, resin, plastic, zeolite, silicone, activated carbon, Teflon, etc., of which stainless steel is preferred. The porous inner ring 24 and the porous outer ring 25 communicate with each other through a plurality of holes.
該內層殼體22包括內上蓋30、內殼體31及內底板32所構成;該內上蓋30及該內底板32分別與該內殼體31之上緣、下緣結合,該旋轉心軸28貫穿該內底板32中央。該旋轉心軸28係利用一馬達(未顯示)驅 動進行旋轉,帶動該旋轉填充床23相對於該內層殼體22進行旋轉。該旋轉填充床23的旋轉速度可視需要調整,較佳地,該旋轉填充床23的旋轉速度為150至3000rpm。該旋轉心軸28在通過該底板32處設有旋轉密封元件33,例如軸封。一蒸汽通入管34設於該內層殼體22的側壁上,該底板32設有一個液體排出管35。該內上蓋30設有一氣體開口36與有一液體通入管37進入到一中間通道38中,該液體通入管37的噴液開口39位於該旋轉填充床23的多孔內環24之內側。該旋轉填充床23的上方與該氣體開口36之間有旋轉密封元件33,以避免進入該內層殼體22的蒸汽未通過該旋轉填充床23,而直接由該氣體開口36排出。 The inner casing 22 includes an inner upper cover 30, an inner casing 31 and an inner bottom plate 32. The inner upper cover 30 and the inner bottom plate 32 are respectively coupled with an upper edge and a lower edge of the inner casing 31. The rotating mandrel 28 extends through the center of the inner bottom plate 32. The rotating mandrel 28 is driven by a motor (not shown) The rotation is performed to rotate the rotating packed bed 23 relative to the inner casing 22. The rotational speed of the rotary packed bed 23 can be adjusted as needed. Preferably, the rotational speed of the rotary packed bed 23 is 150 to 3000 rpm. The rotating mandrel 28 is provided with a rotary sealing element 33, such as a shaft seal, through the bottom plate 32. A steam inlet pipe 34 is provided on the side wall of the inner casing 22, and the bottom plate 32 is provided with a liquid discharge pipe 35. The inner upper cover 30 is provided with a gas opening 36 and a liquid inlet pipe 37 into an intermediate passage 38, and a liquid discharge opening 39 of the liquid inlet pipe 37 is located inside the porous inner ring 24 of the rotary packed bed 23. There is a rotary sealing member 33 between the upper portion of the rotating packed bed 23 and the gas opening 36 to prevent steam entering the inner casing 22 from passing through the rotating packed bed 23 and being directly discharged from the gas opening 36.
一外層殼體21具有一定的間隔包覆在該內層殼體22與該氣體開口36的外側並與該氣體開口36相通,該外層圓柱殼體21由外上蓋40、外殼體41及外底板42所構成,該外殼體41連接有一個流體出口43。該液體通入管37、液體排出管35和蒸汽通入管34,皆穿出該外層殼體21而與外界管線相連接。通過該旋轉填充床23的氣體經由該氣體開口36進入外層中空腔體44,部分的氣體會冷卻凝結而同時對內層中空腔體45產生保溫的效果,流體出口43設置於該外層殼體21下方可避免冷凝液體累積在該外層殼體21的情形。亦即,該外層中空腔體44具有流體通道的功能,同時該外層中空腔體44的存在可達到內部保溫的效果。在本發明的另一個實施例中(未繪示),流體出口可依照外部接管需求配置於外層殼體下方之對應位置。 An outer casing 21 is covered on the outer side of the inner casing 22 and the gas opening 36 at a certain interval, and communicates with the gas opening 36. The outer cylindrical casing 21 is composed of an outer upper cover 40, an outer casing 41 and an outer bottom plate. 42 is configured such that the outer casing 41 is connected to a fluid outlet 43. The liquid inlet pipe 37, the liquid discharge pipe 35, and the steam inlet pipe 34 are all passed through the outer casing 21 to be connected to the outside line. The gas passing through the rotating packed bed 23 enters the outer hollow cavity 44 via the gas opening 36, and part of the gas cools and condenses while simultaneously insulating the hollow body 45 in the inner layer, and the fluid outlet 43 is disposed in the outer casing 21 The case where condensed liquid accumulates in the outer casing 21 can be avoided below. That is, the outer hollow body 44 has the function of a fluid passage, and the presence of the hollow body 44 in the outer layer can achieve the effect of internal heat preservation. In another embodiment of the invention (not shown), the fluid outlets may be disposed at corresponding locations below the outer casing in accordance with external stub requirements.
依據本發明之一種態樣,在一級式廢水回收製程中,部分或全部旋轉填充床裝置可使用上述之夾層式旋轉填充床裝置;依據本發明之另一種態樣,在二級式廢水回收製程中,部分或全部旋轉填充床裝置可使用上述之夾層式旋轉填充床裝置;依據本發明之又一種態樣,在三級式廢水回收製程中,部分或全部旋轉填充床裝置可使用上述之夾層式旋轉填充床裝置。 According to one aspect of the present invention, in the primary waste water recovery process, the above-described sandwich type rotary packed bed apparatus can be used for part or all of the rotating packed bed apparatus; according to another aspect of the present invention, in the secondary type waste water recycling process In the middle, part or all of the rotating packed bed device, the above-mentioned sandwich type rotating packed bed device can be used; according to another aspect of the present invention, in the three-stage waste water recycling process, some or all of the rotating packed bed devices can use the above-mentioned interlayer Rotary packed bed device.
本發明使用蒸汽汽提進行廢水中揮發性物質的回收,特別地是,本發明針對含低濃度揮發性物質的廢水,提出多階段(級)式的旋轉填充床裝置之回收製程。如下列實施方式所示,本發明實施例的氨氮廢水濃度範圍為0.1至2.5wt.%,證明本發明可達到從含低濃度揮發性物質廢水中回收揮發性物質之目的。 The invention uses steam stripping to recover volatile substances in waste water. In particular, the present invention provides a multi-stage (stage) type rotary packed bed apparatus recovery process for waste water containing low concentration volatile substances. As shown in the following embodiments, the concentration of the ammonia nitrogen wastewater in the embodiment of the present invention ranges from 0.1 to 2.5 wt.%, which proves that the present invention can achieve the purpose of recovering volatile substances from waste water containing low concentrations of volatile materials.
根據本發明所提供之自廢水中濃縮回收揮發性物質之製程,可藉由下列較佳實施方式及附圖而進一步說明。但是本發明不限於所列出實施例。 The process for the concentration and recovery of volatile materials from wastewater according to the present invention can be further illustrated by the following preferred embodiments and the accompanying drawings. However, the invention is not limited to the listed embodiments.
使用本發明的一級式回收系統來汽提含有氨氮的廢水,廢水中氨氮濃度約為2.5wt.%。首先將廢水的pH值在調整槽中調整到約為12,並經過熱交換器將水溫調整到70℃左右,經由泵浦以約200kg/h的流量導入一台旋轉填充床中,同時通入溫度約為110℃與流量約為25kg/h的蒸汽,其蒸汽與廢水的比值約為0.125kg/kg,在該旋轉填充床中進行氨氮的汽液質量傳送程序,可得到出流水的氨氮濃度約為0.05wt.%(氨氮去除效率約為98%)。同時將從該旋轉填充床排出含氨氮的氣體進行冷凝收集於第一級回收溶液儲槽中,所回收氨水的濃度約為22wt.%。 The aqueous ammonia-containing wastewater is stripped using the primary recovery system of the present invention, and the ammonia nitrogen concentration in the wastewater is about 2.5 wt.%. Firstly, the pH value of the wastewater is adjusted to about 12 in the adjustment tank, and the water temperature is adjusted to about 70 ° C through a heat exchanger, and is introduced into a rotating packed bed by a pump at a flow rate of about 200 kg/h. The steam has a temperature of about 110 ° C and a flow rate of about 25 kg / h, the ratio of steam to wastewater is about 0.125 kg / kg, in the rotating packed bed to carry out the vapor-liquid mass transfer program of ammonia nitrogen, can obtain the ammonia nitrogen of the running water The concentration is about 0.05 wt.% (the ammonia nitrogen removal efficiency is about 98%). At the same time, the ammonia nitrogen-containing gas is discharged from the rotating packed bed and condensed and collected in the first-stage recovery solution storage tank, and the concentration of the recovered ammonia water is about 22 wt.%.
使用本發明的二級式回收系統來汽提含有氨氮的廢水,廢水中氨氮濃度約為1.2wt.%。首先將廢水的pH值在調整槽中調整到約為12,並經過熱交換器將水溫調整到70℃左右,經由泵浦以約140kg/h的流量導入第一台旋轉填充床中,同時通入溫度約為110℃與流量約為25kg/h的蒸汽,其蒸汽與廢水的比值約為0.18kg/kg,進行第一次氨氮的汽液質量傳送程序,可得到出流水的氨氮濃度約為0.01wt.% (氨氮去除效率約為99%)。從該旋轉填充床所排出含氨氮的氣體進行冷凝收集於第一級回收溶液儲槽中,所冷凝回收的氨水濃度約為7wt.%。再將該氨水經由泵浦以流量約為60kg/h導入第二台旋轉填充床中,同時通入溫度約為110℃與流量約為15kg/h的蒸汽,其蒸汽與廢水的比值約為0.25kg/kg,進行第二次氨氮的汽液質量傳送程序,出流廢水的氨氮濃度約為0.05wt.%(氨氮去除效率約為99%),可直接排放或導回該調整槽中,同時將從該第二台旋轉填充床排出含氨氮的氣體進行冷凝收集於第二級回收溶液儲槽中,所回收氨水的濃度約為25wt.%。 The wastewater containing ammonia nitrogen is stripped using the secondary recovery system of the present invention, and the ammonia nitrogen concentration in the wastewater is about 1.2 wt.%. First, the pH value of the wastewater is adjusted to about 12 in the adjustment tank, and the water temperature is adjusted to about 70 ° C through a heat exchanger, and is introduced into the first rotating packed bed by a pump at a flow rate of about 140 kg/h. The steam has a temperature of about 110 ° C and a flow rate of about 25 kg / h, the ratio of steam to wastewater is about 0.18 kg / kg, the first ammonia nitrogen vapor-liquid mass transfer procedure, the ammonia nitrogen concentration of the running water can be obtained 0.01wt.% (Ammonia nitrogen removal efficiency is about 99%). The ammonia nitrogen-containing gas discharged from the rotating packed bed is condensed and collected in the first-stage recovery solution storage tank, and the concentration of the ammonia water recovered by condensation is about 7 wt.%. The ammonia water is pumped into a second rotating packed bed at a flow rate of about 60 kg/h, and a steam having a temperature of about 110 ° C and a flow rate of about 15 kg / h is introduced, and the ratio of steam to wastewater is about 0.25. Kg/kg, the second ammonia-nitrogen vapor-liquid mass transfer program, the ammonia nitrogen concentration of the outflow wastewater is about 0.05wt.% (the ammonia nitrogen removal efficiency is about 99%), and can be directly discharged or returned to the adjustment tank. The ammonia nitrogen-containing gas is discharged from the second rotating packed bed and condensed and collected in the second-stage recovery solution storage tank, and the concentration of the recovered ammonia water is about 25 wt.%.
使用本發明的二級式回收系統來汽提含有氨氮的廢水,廢水中氨氮濃度約為0.6wt.%。首先將廢水的pH值在調整槽中調整到約為12,並經過熱交換器將水溫調整到70℃左右,經由泵浦以約140kg/h的流量導入第一台旋轉填充床中,同時通入溫度約為110℃與流量約為25kg/h的蒸汽,其蒸汽與廢水的比值約為0.18kg/kg,進行第一次氨氮的汽液質量傳送程序,可得到出流水的氨氮濃度約為0.005wt.%(氨氮去除效率約為99%)。從該旋轉填充床所排出含氨氮的氣體進行冷凝收集於第一級回收溶液儲槽中,所冷凝回收的氨水濃度約為3.5wt.%。再將該氨水經由泵浦以約為160kg/h的流量導入第二台旋轉填充床中,同時通入溫度約為110℃與流量約為20kg/h的蒸汽,其蒸汽與廢水的比值約為0.125kg/kg,進行第二次氨氮的汽液質量傳送程序,出流廢水的氨氮濃度約為0.08wt.%(氨氮去除效率約為98%),可直接排放或導回該調整槽中,同時將從該第二台旋轉填充床排出含氨氮的氣體進行冷凝收集於第二級回收溶液儲槽中,所回收氨水的濃度約為25wt.%。 The wastewater containing ammonia nitrogen is stripped using the secondary recovery system of the present invention, and the ammonia nitrogen concentration in the wastewater is about 0.6 wt.%. First, the pH value of the wastewater is adjusted to about 12 in the adjustment tank, and the water temperature is adjusted to about 70 ° C through a heat exchanger, and is introduced into the first rotating packed bed by a pump at a flow rate of about 140 kg/h. The steam has a temperature of about 110 ° C and a flow rate of about 25 kg / h, the ratio of steam to wastewater is about 0.18 kg / kg, the first ammonia nitrogen vapor-liquid mass transfer procedure, the ammonia nitrogen concentration of the running water can be obtained It is 0.005 wt.% (ammonia nitrogen removal efficiency is about 99%). The ammonia nitrogen-containing gas discharged from the rotating packed bed is condensed and collected in a first-stage recovery solution storage tank, and the concentration of the ammonia water recovered by condensation is about 3.5 wt.%. The ammonia water is pumped into the second rotating packed bed at a flow rate of about 160 kg/h, and a steam having a temperature of about 110 ° C and a flow rate of about 20 kg / h is introduced, and the ratio of steam to wastewater is about 0.125kg/kg, the second ammonia-nitrogen vapor-liquid mass transfer program, the ammonia nitrogen concentration of the outflow wastewater is about 0.08wt.% (the ammonia nitrogen removal efficiency is about 98%), and can be directly discharged or returned to the adjustment tank. At the same time, the ammonia nitrogen-containing gas is discharged from the second rotating packed bed for condensation and collected in the second-stage recovery solution storage tank, and the concentration of the recovered ammonia water is about 25 wt.%.
使用本發明的三級式回收系統來汽提含有氨氮的廢水,廢水中氨氮濃度約為0.1wt.%。首先將廢水的pH值在調整槽中調整到約為12,並經過熱交換器將水溫調整到70℃左右,經由泵浦以約200kg/h的流量導入第一台旋轉填充床中,同時通入溫度約為110℃與流量約為20kg/h的蒸汽,其蒸汽與廢水的比值約為0.1kg/kg,進行第一次氨氮的汽液質量傳送程序,可得到出流水的氨氮濃度約為0.003wt.%(氨氮去除效率約為97%)。從該旋轉填充床所排出含氨氮的氣體進行冷凝收集於第一級回收溶液儲槽中,所冷凝回收的氨水濃度約為1.3wt.%。再將該氨水經由泵浦以約150kg/h的流量導入第二台旋轉填充床中,同時通入溫度約為110℃與流量約為20kg/h的蒸汽,其蒸汽與廢水的比值約為0.13kg/kg,進行第二次氨氮的汽液質量傳送程序,出流廢水的氨氮濃度約為0.02wt.%(氨氮去除效率約為98%),可直接排放或導回該調整槽中,同時將從該第二台旋轉填充床排出含氨氮的氣體進行冷凝收集於第二級回收溶液儲槽中,所回收氨水的濃度約為8wt.%。再將該氨水經由泵浦以約60kg/h的流量導入第三台旋轉填充床中,同時通入溫度約為110℃與流量約為20kg/h的蒸汽,其蒸汽與廢水的比值約為0.33kg/kg,進行第三次氨氮的汽液質量傳送程序,出流廢水的氨氮濃度約為0.05wt.%(氨氮去除效率約為98%),可直接排放或導回該調整槽中,同時將從該第三台旋轉填充床排出含氨氮的氣體進行冷凝收集於第三級回收溶液儲槽中,所回收氨水的濃度約為23wt.%。 The ammonia-containing wastewater is stripped using the three-stage recovery system of the present invention, and the ammonia nitrogen concentration in the wastewater is about 0.1 wt.%. First, the pH value of the wastewater is adjusted to about 12 in the adjustment tank, and the water temperature is adjusted to about 70 ° C through a heat exchanger, and is introduced into the first rotating packed bed by a pump at a flow rate of about 200 kg/h. The steam has a temperature of about 110 ° C and a flow rate of about 20 kg / h, the steam to wastewater ratio of about 0.1 kg / kg, the first ammonia nitrogen vapor-liquid mass transfer program, the ammonia nitrogen concentration of the run-off water can be obtained It is 0.003 wt.% (ammonia nitrogen removal efficiency is about 97%). The ammonia nitrogen-containing gas discharged from the rotating packed bed is condensed and collected in the first-stage recovery solution storage tank, and the concentration of the ammonia water recovered by condensation is about 1.3 wt.%. The ammonia water is then pumped into a second rotating packed bed at a flow rate of about 150 kg/h, while a steam having a temperature of about 110 ° C and a flow rate of about 20 kg/h is introduced, and the ratio of steam to wastewater is about 0.13. Kg/kg, the second ammonia-nitrogen vapor-liquid mass transfer program, the ammonia nitrogen concentration of the outflow wastewater is about 0.02 wt.% (the ammonia nitrogen removal efficiency is about 98%), and can be directly discharged or returned to the adjustment tank, The ammonia-containing gas is discharged from the second rotating packed bed and condensed and collected in the second-stage recovery solution storage tank, and the concentration of the recovered ammonia water is about 8 wt.%. The ammonia water is pumped into a third rotating packed bed at a flow rate of about 60 kg/h, and a steam having a temperature of about 110 ° C and a flow rate of about 20 kg/h is introduced, and the ratio of steam to wastewater is about 0.33. Kg/kg, the third ammonia-nitrogen vapor-liquid mass transfer program, the ammonia nitrogen concentration of the outflow wastewater is about 0.05wt.% (the ammonia nitrogen removal efficiency is about 98%), and can be directly discharged or returned to the adjustment tank. The ammonia nitrogen-containing gas was discharged from the third rotating packed bed and condensed and collected in a third-stage recovery solution storage tank, and the concentration of the recovered ammonia water was about 23 wt.%.
使用本發明的一級式回收系統來汽提含有異丙醇的廢水,廢水中異丙醇濃度約為2wt.%。首先將廢水經過熱交換器將水溫調整到約80℃左右,再經由泵浦以約15kg/h的流量導入一台旋轉填充床中,同時通入溫度約為110℃與流量約為3.8kg/h的蒸汽,其蒸汽與廢水的 比值約為0.25kg/kg,在該旋轉填充床中進行異丙醇的汽液質量傳送程序,可得到出流水的異丙醇濃度約為0.08wt.%(異丙醇去除效率約為96%)。同時將從該旋轉填充床排出含異丙醇的氣體進行冷凝收集於第一級回收溶液儲槽中,所回收異丙醇溶液的濃度約為9wt.%。 The wastewater containing isopropyl alcohol is stripped using the primary recovery system of the present invention, and the isopropanol concentration in the wastewater is about 2 wt.%. First, the wastewater is adjusted to a temperature of about 80 ° C through a heat exchanger, and then introduced into a rotating packed bed by a pump at a flow rate of about 15 kg / h, while the inlet temperature is about 110 ° C and the flow rate is about 3.8 kg. /h of steam, its steam and wastewater The ratio is about 0.25 kg/kg, and the vapor-liquid mass transfer procedure of isopropanol is carried out in the rotating packed bed, and the isopropanol concentration of the produced water is about 0.08 wt.% (the isopropyl alcohol removal efficiency is about 96%). ). At the same time, the isopropanol-containing gas is discharged from the rotating packed bed and condensed and collected in the first-stage recovery solution storage tank, and the concentration of the recovered isopropanol solution is about 9 wt.%.
使用本發明的一級式回收系統來汽提含有異丙醇的廢水,廢水中異丙醇濃度約為2wt.%。首先將廢水經過熱交換器將水溫調整到約80℃左右,再經由泵浦以約25kg/h的流量導入一台旋轉填充床中,同時通入溫度約為120℃與流量約為1.65kg/h的蒸汽,其蒸汽與廢水的比值約為0.065kg/kg,在該旋轉填充床中進行異丙醇的汽液質量傳送程序,可得到出流水的異丙醇濃度約為0.2wt.%(異丙醇去除效率約為90%),同時將從該旋轉填充床排出含異丙醇的氣體進行冷凝收集於第一級回收溶液儲槽中,所回收異丙醇溶液的濃度約為25wt.%。 The wastewater containing isopropyl alcohol is stripped using the primary recovery system of the present invention, and the isopropanol concentration in the wastewater is about 2 wt.%. First, the wastewater is adjusted to a temperature of about 80 ° C through a heat exchanger, and then introduced into a rotating packed bed by a pump at a flow rate of about 25 kg / h, while the inlet temperature is about 120 ° C and the flow rate is about 1.65 kg. /h of steam, the ratio of steam to wastewater is about 0.065kg / kg, in the rotating packed bed to carry out the vapor-liquid mass transfer procedure of isopropanol, the isopropanol concentration of the produced water can be obtained is about 0.2wt.% (Isopropanol removal efficiency is about 90%), and the isopropyl alcohol-containing gas is discharged from the rotating packed bed for condensation and collected in the first-stage recovery solution storage tank, and the concentration of the recovered isopropanol solution is about 25 wt. .%.
使用本發明的二級式回收系統來汽提含有異丙醇的廢水,廢水中異丙醇濃度約為2wt.%。首先將廢水經過熱交換器將水溫調整到約80℃左右,經由泵浦以約20kg/h的流量導入第一台旋轉填充床中,同時通入溫度約為120℃與流量約為1.5kg/h的蒸汽,其蒸汽與廢水的比值約為0.08kg/kg,進行第一次異丙醇的汽液質量傳送程序,可得到出流水的異丙醇濃度約為0.17wt.%(異丙醇去除效率約為92%)。從該旋轉填充床所排出含異丙醇的氣體進行冷凝收集於第一級回收溶液儲槽中,所冷凝回收的異丙醇溶液濃度約為21wt.%。再將該冷凝回收的異丙醇溶液經由泵浦以約20kg/h的流量導入第二台旋轉填充床中,同時通入溫度約為120℃與流量約為1.6kg/h的蒸汽,其蒸汽與廢水的比值約為0.08kg/kg,進行第二次異丙醇的汽液質量傳送程序,出流廢水的異丙醇濃度約為3.2wt.%(異丙醇去除效率約為85%) 可導回調整槽中,同時將從該第二台旋轉填充床排出含異丙醇的氣體進行冷凝收集於第二級回收溶液儲槽中,所回收異丙醇溶液的濃度約為70wt.%。 The waste water containing isopropanol is stripped using the secondary recovery system of the present invention, and the isopropanol concentration in the wastewater is about 2 wt.%. First, the wastewater is adjusted to a temperature of about 80 ° C through a heat exchanger, and is introduced into the first rotating packed bed by a pump at a flow rate of about 20 kg/h, and the temperature is about 120 ° C and the flow rate is about 1.5 kg. /h steam, the ratio of steam to wastewater is about 0.08kg / kg, the first isopropyl alcohol vapor-liquid mass transfer procedure, the isopropanol concentration of the produced water can be obtained is about 0.17wt.% (isopropyl The alcohol removal efficiency is about 92%). The isopropyl alcohol-containing gas discharged from the rotating packed bed was condensed and collected in a first-stage recovery solution storage tank, and the concentration of the isopropyl alcohol solution recovered by condensation was about 21 wt.%. The condensed recovered isopropanol solution is then pumped into a second rotating packed bed at a flow rate of about 20 kg/h, while steam having a temperature of about 120 ° C and a flow rate of about 1.6 kg/h is introduced. The ratio of wastewater to wastewater is about 0.08 kg/kg, and the second isopropyl alcohol vapor-liquid mass transfer procedure is carried out. The isopropanol concentration of the outflow wastewater is about 3.2 wt.% (the isopropyl alcohol removal efficiency is about 85%). It can be guided back into the adjusting tank, and the isopropyl alcohol-containing gas is discharged from the second rotating packed bed for condensation and collected in the second-stage recovery solution storage tank, and the concentration of the recovered isopropanol solution is about 70 wt.%. .
A‧‧‧含揮發性物質廢水 A‧‧‧ Wastewater containing volatile substances
B‧‧‧調整藥劑 B‧‧‧Adjustment
C‧‧‧蒸汽 C‧‧‧Steam
D‧‧‧出流水 D‧‧‧Outflow
E‧‧‧回收溶液 E‧‧‧Recovery solution
F‧‧‧尾氣 F‧‧‧Exhaust
100‧‧‧調整槽 100‧‧‧ adjustment slot
110‧‧‧泵浦 110‧‧‧ pump
120‧‧‧廢水熱交換器 120‧‧‧Waste water heat exchanger
130‧‧‧第一級旋轉填充床 130‧‧‧First-stage rotating packed bed
140‧‧‧第一級冷凝器 140‧‧‧First stage condenser
150‧‧‧第一級回收溶液儲槽 150‧‧‧First-stage recovery solution storage tank
160‧‧‧熱交換器 160‧‧‧ heat exchanger
170‧‧‧旋轉填充床 170‧‧‧Rotary packed bed
310‧‧‧第二級旋轉填充床 310‧‧‧Second stage rotating packed bed
320‧‧‧第二級冷凝器 320‧‧‧Second stage condenser
330‧‧‧第二級回收溶液儲槽 330‧‧‧Second grade recovery solution storage tank
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