TW201540654A - Ammonia recycling system - Google Patents
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本發明是有關於一種氨回收系統，其係利用預熱、催化劑及氨吸收器使得廢水中的銨有效地轉化成氨水。The present invention relates to an ammonia recovery system that utilizes preheating, a catalyst, and an ammonia absorber to efficiently convert ammonium in wastewater to ammonia.
含氨廢水廣泛存在於人們的日常生活和各個行業中，近年來，隨著對氮、磷等有機污染的重視，各種含氨廢水的脫氮技術便成為相當重要的課題。Ammonia-containing wastewater is widely used in people's daily life and various industries. In recent years, with the emphasis on organic pollution such as nitrogen and phosphorus, various nitrogen-containing wastewater denitrification technologies have become an important issue.
亞硝酸鹽是氨轉化為硝酸鹽過程中的中間產物，對魚蝦等水生動物具有一定的毒性。若含氨廢水排放至池塘或河川中，亞硝酸鹽含量偏高現象便相當嚴重，進而導致魚蝦的突然死亡，因而造成養殖者嚴重的經濟損失。即使達不到致死濃度，但由於亞硝酸鹽含量超過Nitrite is an intermediate product in the conversion of ammonia to nitrate and has certain toxicity to aquatic animals such as fish and shrimp. If ammonia-containing wastewater is discharged into ponds or rivers, the high nitrite content is quite serious, leading to sudden death of fish and shrimp, thus causing serious economic losses for farmers. Even if the lethal concentration is not reached, the nitrite content exceeds
然而，習知去除廢水中氨氮的方法如折點氯化法由於運行費用高，且副產物氯胺和氯化有機物更會造成環境二次汙染，因此只適用於處理低濃度氨氮廢水。此外，習知之空氣吹脫法及生物法則各別具有水溫低時吹脫效率低及站地面積大等缺點，因此皆無法有效率地去除廢水中的氨氮。However, the conventional method for removing ammonia nitrogen from waste water, such as the chlorination method, is high in operation cost, and the by-product chloramine and chlorinated organic matter cause secondary pollution to the environment, and therefore is only suitable for treating low-concentration ammonia nitrogen wastewater. In addition, the conventional air blowing method and the biological method have the disadvantages of low blowing efficiency and large station area when the water temperature is low, so that the ammonia nitrogen in the wastewater cannot be efficiently removed.
有鑑於上述習知技藝之問題，本發明之其中之一目的在於提供一種氨回收系統，其係藉由預熱及催化使得廢水中的銨(固定 銨；fixed ammoni um)有效地脫離廢水成為氨氣(游離氨；free ammonia)，並且藉由氨吸收器而轉化成氨水。In view of the above problems of the prior art, it is an object of the present invention to provide an ammonia recovery system which is capable of effectively removing ammonia (fixed ammoni um) from waste water into ammonia by preheating and catalysis. Gas (free ammonia) and converted to ammonia by an ammonia absorber.
本發明之另一目的在於提供一種氨回收系統，其係藉由添加催化劑及滲析作用，以達到回收廢水中的氨之目的。Another object of the present invention is to provide an ammonia recovery system for the purpose of recovering ammonia in wastewater by adding a catalyst and dialysis.
緣是，本發明提出一種氨回收系統，至少包含第一廢水槽、第一熱交換器、反應槽及第一氨吸收器。第一廢水槽內設置有含有銨之廢水。第一熱交換器係連通第一廢水槽，以預熱廢水至第一溫度。反應槽係連通第一熱交換器，且令第一催化劑與經第一熱交換器預熱之廢水反應而得氨氣。第一氨吸收器係連通反應槽，並藉由第二熱交換器以冷卻第一氨吸收器至第二溫度，並藉由噴灑純水使得氨氣溶於純水中以轉化成氨水。Accordingly, the present invention provides an ammonia recovery system comprising at least a first wastewater tank, a first heat exchanger, a reaction tank, and a first ammonia absorber. Waste water containing ammonium is disposed in the first wastewater tank. The first heat exchanger is in communication with the first wastewater tank to preheat the wastewater to a first temperature. The reaction tank is connected to the first heat exchanger, and the first catalyst is reacted with the waste water preheated by the first heat exchanger to obtain ammonia gas. The first ammonia absorber is connected to the reaction tank, and is cooled by the second heat exchanger to cool the first ammonia absorber to the second temperature, and the ammonia gas is dissolved in pure water by spraying pure water to be converted into ammonia water.
此外，本發明之氨回收系統更包含第二氨吸收器，其係連通第一氨吸收器。第二氨吸收器係藉由第二熱交換器以冷卻第二氨吸收器至第二溫度，並藉由噴灑純水使得部分未被第一氨吸收器轉化成氨水之氨氣溶於純水中而轉化成氨水。此外，氨回收系統更包含設置有硫酸之洗滌塔，且洗滌塔連通第二氨吸收器。其中，第一溫度為70℃，第二溫度之溫度範圍為-30℃至30℃。Further, the ammonia recovery system of the present invention further comprises a second ammonia absorber that is in communication with the first ammonia absorber. The second ammonia absorber cools the second ammonia absorber to the second temperature by the second heat exchanger, and dissolves the ammonia gas which is not converted into the ammonia water by the first ammonia absorber by spraying the pure water into the pure water. It is converted into ammonia water. Further, the ammonia recovery system further comprises a scrubber equipped with sulfuric acid, and the scrubber is connected to the second ammonia absorber. Wherein, the first temperature is 70 ° C, and the second temperature has a temperature ranging from -30 ° C to 30 ° C.
此外，本發明之氨回收系統更包含氨水槽連通第一氨吸收器及第二氨吸收器，以儲存第一氨吸收器及第二氨吸收器所轉化而得之氨水，並且藉由第二熱交換器使得氨水槽內之氨水的溫度維持在第二溫度。In addition, the ammonia recovery system of the present invention further comprises an ammonia water tank connected to the first ammonia absorber and the second ammonia absorber for storing the ammonia water converted by the first ammonia absorber and the second ammonia absorber, and by the second The heat exchanger maintains the temperature of the ammonia water in the ammonia tank at a second temperature.
除此之外，本發明之氨回收系統更包含第二廢水槽、催化槽、第一氨滲析模組及硫酸槽。第二廢水槽連通反應槽，以容納反應槽中未被第一催化劑催化之廢水。催化槽設置有第二催化劑且連通第二廢水槽，用以將第二廢水槽內之廢水中的銨催化成氨氣。第一氨滲析模組包含至少一滲析膜，並藉由滲析膜滲析已被第二催化劑催化之氨氣。硫酸槽內設置有硫酸，用以與已被第一氨滲析模組滲析之氨氣反應而得硫酸銨。其中，未被第二催化劑催化之廢水中的銨係藉由第三催化劑催化成氨氣，且氨回收系統更包含第二氨滲析模組。第二氨滲析模組包含至少一滲析膜，並藉由滲析膜滲析已被第三催化劑催化之氨氣。其中，已被第二氨滲析模組滲析之氨氣與硫酸反應而得硫酸銨。其中，第三催化劑係來自於催化槽，且硫酸係來自於硫酸槽。其中，第一催化劑、第二催化劑及第三催化劑係分別為氧化鈣或氫氧化鈉且其pH值範圍為10至12。其中，第一氨滲析模組及第二氨滲析模組中的滲析膜為透氣式滲析膜。In addition, the ammonia recovery system of the present invention further comprises a second wastewater tank, a catalytic tank, a first ammonia dialysis module and a sulfuric acid tank. The second wastewater tank is connected to the reaction tank to accommodate the wastewater in the reaction tank that is not catalyzed by the first catalyst. The catalytic tank is provided with a second catalyst and communicates with the second wastewater tank for catalyzing the ammonium in the wastewater in the second wastewater tank to ammonia gas. The first ammonia dialysis module comprises at least one dialysis membrane and dialysis of the ammonia gas that has been catalyzed by the second catalyst by the dialysis membrane. Sulfuric acid is disposed in the sulfuric acid tank for reacting with the ammonia gas which has been dialyzed by the first ammonia dialysis module to obtain ammonium sulfate. The ammonium in the wastewater not catalyzed by the second catalyst is catalyzed into ammonia by the third catalyst, and the ammonia recovery system further comprises a second ammonia dialysis module. The second ammonia dialysis module comprises at least one dialysis membrane and dialysis of the ammonia gas that has been catalyzed by the third catalyst by the dialysis membrane. Among them, the ammonia gas which has been dialyzed by the second ammonia dialysis module reacts with sulfuric acid to obtain ammonium sulfate. Wherein, the third catalyst is derived from the catalytic tank, and the sulfuric acid is derived from the sulfuric acid tank. Wherein, the first catalyst, the second catalyst and the third catalyst are respectively calcium oxide or sodium hydroxide and have a pH ranging from 10 to 12. The dialysis membrane in the first ammonia dialysis module and the second ammonia dialysis module is a gas permeable dialysis membrane.
承上所述，依據本發明之氨回收系統，其可具有一或多個下述優點：As described above, the ammonia recovery system according to the present invention may have one or more of the following advantages:
(1) 本發明之氨回收系統，藉由添加催化劑可有效率地將廢水中的銨催化成氨氣，再藉由氨吸收器滲析模組滲析氨氣，以達到將廢水中的氨提取出來之目的。(1) The ammonia recovery system of the present invention can efficiently catalyze the ammonium in the wastewater into ammonia gas by adding a catalyst, and then dialysis ammonia gas through the ammonia absorber dialysis module to extract the ammonia in the wastewater. The purpose.
(2) 本發明之氨回收系統，藉由將經由催化及滲析作用後之氨氣與硫酸反應，可得硫酸銨。(2) The ammonia recovery system of the present invention can obtain ammonium sulfate by reacting ammonia gas after catalytic and dialysis with sulfuric acid.
(3) 本發明之氨回收系統，藉由預熱及催化，可將硫酸銨預熱並催化反應而得氨氣，再藉由氨吸收器進而可將氨氣轉化成氨水回收再利用。(3) The ammonia recovery system of the present invention can preheat and catalyze the reaction to obtain ammonia gas by preheating and catalysis, and then convert the ammonia gas into ammonia water for recycling by the ammonia absorber.
(4) 在本發明之氨回收系統中，催化劑(例如為氧化鈣)與銨反應後的生成物更可作為水泥添加物而不會造成環境二次汙染。(4) In the ammonia recovery system of the present invention, the product obtained by reacting a catalyst (for example, calcium oxide) with ammonium can be used as a cement additive without causing secondary environmental pollution.
10‧‧‧第一廢水槽10‧‧‧First Wastewater Tank
12‧‧‧第一熱交換器12‧‧‧First heat exchanger
14‧‧‧反應槽14‧‧‧Reaction tank
16‧‧‧第一氨吸收器16‧‧‧First ammonia absorber
18‧‧‧第二氨吸收器18‧‧‧Second ammonia absorber
20、20’‧‧‧純水20, 20’‧‧‧ pure water
22‧‧‧洗滌塔22‧‧‧ Washing tower
24‧‧‧氨水槽24‧‧‧Ammonia sink
26、26’‧‧‧第二熱交換器26, 26' ‧ ‧ second heat exchanger
28‧‧‧第二廢水槽28‧‧‧Second wastewater tank
30‧‧‧催化槽30‧‧‧catalytic tank
32‧‧‧第一氨滲析模組32‧‧‧First ammonia dialysis module
34‧‧‧第二氨滲析模組34‧‧‧Second ammonia dialysis module
36、36’‧‧‧硫酸槽36, 36'‧‧‧ sulfuric acid tank
38‧‧‧硫酸銨槽38‧‧‧Ammonium sulphate tank
40‧‧‧第一催化劑40‧‧‧First Catalyst
42‧‧‧第三廢水槽42‧‧‧ Third Wastewater Tank
第1圖 係為本發明之氨回收系統之第一實施例之示意圖。Figure 1 is a schematic illustration of a first embodiment of an ammonia recovery system of the present invention.
第2圖 係為本發明之氨回收系統之第二實施例之示意圖。Figure 2 is a schematic illustration of a second embodiment of the ammonia recovery system of the present invention.
以下將參照相關圖式，說明依本發明之氨回收系統之實施例，為使便於理解，下述實施例中之相同元件係以相同之符號標示來說明。The embodiments of the ammonia recovery system according to the present invention will be described below with reference to the related drawings. For ease of understanding, the same elements in the following embodiments are denoted by the same reference numerals.
請參閱第1圖，其係為本發明之氨回收系統之第一實施例之示意圖。本發明之氨回收系統至少包含第一廢水槽10、第一熱交換器12、反應槽14及第一氨吸收器16。第一廢水槽10內設置有含有銨(NH4 + ) 之廢水。第一熱交換器12係連通第一廢水槽10，以預熱廢水至第一溫度。其中，第一溫度可例如為70℃，但不限定於此。反應槽14係連通第一熱交換器12，且令第一催化劑40與經第一熱交換器12預熱之廢水反應而得氨氣(NH3 )。其中，如第1圖所示，使用者可視實際需求在廢水於第一熱交換器12中進行預熱之前加入第一催化劑40。並且，反應槽14的溫度範圍可例如為70至90℃。此外，反應槽14之槽壁更可開設有至少一孔洞(圖式中未繪示)，使得外界環境與反應槽14連通，以藉由外界環境之大氣壓力促進反應槽14中流體的流動速率，提高反應槽14的反應效率。並且，反應槽14更可設置與上述孔洞相對應之一曝氣盤(圖式中未繪示)，此曝氣盤為具有複數個孔隙之盤狀物，可均勻分散從外界環境進入反應槽14中的空氣，以更有效率地提高反應槽14之反應效率。此外，也可以在第一氨吸收器16設置一抽真空系統，以抽取第一氨吸收器16的空氣並提高反應槽14的反應速率。詳細來說，由於第一氨吸收器16是與反應槽14相互連通的，因此，在對第一氨吸收器16抽取空氣時，反應槽14中會產生氣泡，這些氣泡的產生會帶動反應槽14中的反應物(即第一催化劑40與廢水)更快速地進行化學反應而提高製得氨氣的反應速率。Please refer to Fig. 1, which is a schematic view of a first embodiment of the ammonia recovery system of the present invention. The ammonia recovery system of the present invention comprises at least a first wastewater tank 10, a first heat exchanger 12, a reaction tank 14, and a first ammonia absorber 16. Waste water containing ammonium (NH 4 + ) is disposed in the first wastewater tank 10. The first heat exchanger 12 is in communication with the first wastewater tank 10 to preheat the wastewater to a first temperature. The first temperature may be, for example, 70 ° C, but is not limited thereto. The reaction tank 14 communicates with the first heat exchanger 12, and reacts the first catalyst 40 with the wastewater preheated by the first heat exchanger 12 to obtain ammonia gas (NH 3 ). As shown in FIG. 1, the user may add the first catalyst 40 before the wastewater is preheated in the first heat exchanger 12 according to actual needs. Also, the temperature range of the reaction tank 14 may be, for example, 70 to 90 °C. In addition, the groove wall of the reaction tank 14 can be opened with at least one hole (not shown), so that the external environment communicates with the reaction tank 14 to promote the flow rate of the fluid in the reaction tank 14 by the atmospheric pressure of the external environment. The reaction efficiency of the reaction tank 14 is increased. Moreover, the reaction tank 14 can further be provided with an aeration disc (not shown) corresponding to the hole, and the aeration disc is a disc having a plurality of pores, and can be uniformly dispersed into the reaction tank from the external environment. The air in 14 is used to more efficiently increase the reaction efficiency of the reaction tank 14. Further, an evacuation system may be provided in the first ammonia absorber 16 to extract the air of the first ammonia absorber 16 and increase the reaction rate of the reaction tank 14. In detail, since the first ammonia absorber 16 is in communication with the reaction tank 14, when the first ammonia absorber 16 is evacuated, bubbles are generated in the reaction tank 14, and the generation of these bubbles drives the reaction tank. The reactants in 14 (i.e., the first catalyst 40 and the wastewater) undergo a chemical reaction more rapidly to increase the reaction rate of the ammonia gas produced.
續言之，第一氨吸收器16係連通反應槽14，並藉由第二熱交換器26以冷卻第一氨吸收器16至第二溫度，並藉由噴灑純水20使得氨氣溶於純水中以轉化成氨水。如第1圖所示，所得之氨水可儲存於氨水槽24中，並可例如藉由氨水槽24自身或外加之溫度維持器件或者是第二熱交換器26或第二熱交換器26’使得氨水槽24內之氨水的溫度維持在第二溫度。其中，第二溫度之溫度範圍可例如為-30℃至30℃。 此外，如第1圖所示，純水20是以內循環之方式提供至第一氨吸收器16，即，純水20會以循環方式流通至第一氨吸收器16。In other words, the first ammonia absorber 16 is connected to the reaction tank 14, and the second ammonia heat exchanger 26 is used to cool the first ammonia absorber 16 to the second temperature, and the ammonia gas is dissolved by spraying the pure water 20. Pure water is converted into ammonia water. As shown in Figure 1, the resulting aqueous ammonia can be stored in the ammonia water tank 24 and can be made, for example, by the ammonia water tank 24 itself or with a temperature maintaining device or a second heat exchanger 26 or a second heat exchanger 26'. The temperature of the ammonia water in the ammonia water tank 24 is maintained at the second temperature. Wherein, the temperature range of the second temperature may be, for example, -30 ° C to 30 ° C. Further, as shown in Fig. 1, the pure water 20 is supplied to the first ammonia absorber 16 in an internal circulation, that is, the pure water 20 is circulated to the first ammonia absorber 16.
此外，如第1圖所示，本發明之氨回收系統更包含連通第一氨吸收器16之第二氨吸收器18。第二氨吸收器18係藉由第二熱交換器26’以冷卻第二氨吸收器18至第二溫度，並藉由噴灑純水20使得部分未被第一氨吸收器16轉化成氨水之氨氣溶於純水中而轉化成氨水。 其中，第一氨吸收器16及第二氨吸收器18的氨氣吸收效率可分別例如介於26%至32%，但不限定於此。同樣地，如同純水20之供應方式，純水20’也是以內循環之方式提供至第二氨吸收器18，即，純水20’會以循環方式流通至第二氨吸收器18。並且，由於從第一氨吸收器16所轉化而得之氨水的量較多，故純水20所消耗的純水量也較多，因此如第1圖所示，在本發明中，純水20’可與純水20連通，以從純水20’補充純水至純水20。此外，由於純水20’連通至純水20，因此，在第二氨吸收器18所轉化而得之氨水可藉此流通至第一氨吸收器16並進而儲存至氨水槽24中。Further, as shown in FIG. 1, the ammonia recovery system of the present invention further includes a second ammonia absorber 18 that communicates with the first ammonia absorber 16. The second ammonia absorber 18 is cooled by the second heat exchanger 26' to the second ammonia absorber 18 to a second temperature, and is partially converted into ammonia water by the first ammonia absorber 16 by spraying the pure water 20. Ammonia gas is dissolved in pure water and converted into ammonia water. The ammonia absorption efficiency of the first ammonia absorber 16 and the second ammonia absorber 18 may be, for example, 26% to 32%, respectively, but is not limited thereto. Similarly, as with the supply of pure water 20, the pure water 20' is also supplied to the second ammonia absorber 18 in an internal circulation, i.e., the pure water 20' is circulated to the second ammonia absorber 18. Further, since the amount of the ammonia water converted from the first ammonia absorber 16 is large, the amount of pure water consumed by the pure water 20 is also large. Therefore, as shown in Fig. 1, in the present invention, the pure water 20 'Can be connected to pure water 20 to replenish pure water from pure water 20' to pure water 20. Further, since the pure water 20' is connected to the pure water 20, the ammonia water converted by the second ammonia absorber 18 can be circulated to the first ammonia absorber 16 and further stored in the ammonia water tank 24.
由於可能仍會有部分氨氣無法在第二氨吸收器18中被轉化成氨水，因此，如第1圖所示，本發明之氨回收系統更可包含洗滌塔22連通第二氨吸收器18，且洗滌塔22中設置有硫酸，以藉由硫酸與氨氣反應而得硫酸銨。Since there may still be some ammonia gas that cannot be converted into ammonia water in the second ammonia absorber 18, as shown in Fig. 1, the ammonia recovery system of the present invention may further comprise a scrubber 22 connected to the second ammonia absorber 18 And sulfuric acid is disposed in the scrubbing tower 22 to obtain ammonium sulfate by reacting sulfuric acid with ammonia gas.
此外，由於第一熱交換器12進行預熱之溫度可能無法很準確地維持在70℃。因此，在本發明之氨回收系統中，更可包含與第一熱交換器12及反應槽14連通之一恆溫加熱器(第1圖中未繪示)，以對已被第一熱交換器12預熱之硫酸銨進行恆溫加熱至溫度範圍為50℃至90℃之間。Further, the temperature at which the first heat exchanger 12 is preheated may not be maintained at 70 ° C very accurately. Therefore, in the ammonia recovery system of the present invention, a thermostat heater (not shown in FIG. 1) connected to the first heat exchanger 12 and the reaction tank 14 may be further included to be opposed to the first heat exchanger. 12 preheated ammonium sulfate is heated at a constant temperature to a temperature ranging from 50 ° C to 90 ° C.
請參閱第2圖，其係為本發明之氨回收系統之第二實施例之示意圖。在本發明之氨回收系統之第二實施例中，氨回收系統更包含第二廢水槽28、催化槽30、第一氨滲析模組32及硫酸槽36。第二廢水槽28連通反應槽14，以容納反應槽14中未被第一催化劑催化之廢水。催化槽30設置有第二催化劑且連通第二廢水槽28，用以將第二廢水槽28內之廢水中的銨催化成氨氣。第一氨滲析模組32包含至少一滲析膜，並藉由滲析膜滲析已被第二催化劑催化之氨氣。硫酸槽36內設置有硫酸，用以與已被第一氨滲析模組32滲析之氨氣反應而得硫酸銨。其中，第一氨滲析模組32中之滲析膜可例如為透氣式滲析膜。透氣式滲析膜之透氣孔洞尺寸可例如為5 μm至20 μm，或者透氣式滲析膜之透氣率可例如介於0至25%。然而，在本發明之第一氨滲析模組32中，滲析膜並不限定於上述舉例之滲析膜及其尺寸、透氣率等規格，任何可有效達到分離氨氣與氨氮廢水之目的的滲析元件，皆為本發明所請求保護之範圍。此外，如第2圖所示， 硫酸槽36 是以內循環之方式提供硫酸至第一氨滲析模組32，即，硫酸槽36中的硫酸會以循環方式流通於硫酸槽36與第一氨滲析模組32之間。Please refer to FIG. 2, which is a schematic view of a second embodiment of the ammonia recovery system of the present invention. In a second embodiment of the ammonia recovery system of the present invention, the ammonia recovery system further includes a second wastewater tank 28, a catalytic tank 30, a first ammonia dialysis module 32, and a sulfuric acid tank 36. The second wastewater tank 28 is connected to the reaction tank 14 to accommodate the wastewater in the reaction tank 14 that is not catalyzed by the first catalyst. The catalytic tank 30 is provided with a second catalyst and communicates with the second wastewater tank 28 for catalyzing the ammonium in the wastewater in the second wastewater tank 28 to ammonia gas. The first ammonia dialysis module 32 includes at least one dialysis membrane and dialysis of ammonia gas that has been catalyzed by the second catalyst by a dialysis membrane. Sulfuric acid is disposed in the sulfuric acid tank 36 for reacting with the ammonia gas which has been dialyzed by the first ammonia dialysis module 32 to obtain ammonium sulfate. The dialysis membrane in the first ammonia dialysis module 32 can be, for example, a gas permeable dialysis membrane. The venting pore size of the gas permeable membrane may be, for example, 5 μm to 20 μm, or the gas permeability of the gas permeable membrane may be, for example, 0 to 25%. However, in the first ammonia dialysis module 32 of the present invention, the dialysis membrane is not limited to the above-mentioned dialysis membrane and its size, gas permeability and the like, and any dialysis element which can effectively achieve the purpose of separating ammonia gas and ammonia nitrogen wastewater. , are the scope of the claimed invention. Further, as shown in FIG. 2, the sulfuric acid tank 36 supplies sulfuric acid to the first ammonia dialysis module 32 in an internal circulation manner, that is, the sulfuric acid in the sulfuric acid tank 36 is circulated in the sulfuric acid tank 36 and the first ammonia dialysis. Between modules 32.
續言之，如第2圖所示，未被第二催化劑催化之廢水中的銨係可例如藉由第三催化劑催化成氨氣，且氨回收系統更可包含第二氨滲析模組34。第二氨滲析模組34包含至少一滲析膜，並藉由滲析膜滲析已被第三催化劑催化之氨氣。其中，已被第二氨滲析模組34滲析之氨氣與硫酸反應而得硫酸銨。其中，第三催化劑係可例如來自於催化槽30，且硫酸係可例如來自於硫酸槽36’。其中，第二氨滲析模組34中的滲析膜為透氣式滲析膜。透氣式滲析膜之透氣孔洞尺寸可例如為5 μm至20 μm，或者透氣式滲析膜之透氣率可例如介於0至25%。然而，在本發明之第二氨滲析模組34中，滲析膜並不限定於上述舉例之滲析膜及其尺寸、透氣率等規格，任何可有效達到分離氨氣與氨氮廢水之目的的滲析元件，皆為本發明所請求保護之範圍。並且，如第2圖所示，本發明之氨回收系統更可包含第三廢水槽42，以容納在第二氨滲析模組34中未被滲析膜滲析之廢水。同樣地，如同硫酸槽36，硫酸槽36’也是以內循環之方式提供硫酸至第二氨滲析模組34，即，硫酸槽36’中的硫酸會以循環方式流通於硫酸槽36’與第二氨滲析模組34之間。並且，由於從第一氨滲析模組32所轉化而得之硫酸銨的量較多，故在硫酸槽36中所消耗的硫酸也較多，因此如第2圖所示，在本發明中，硫酸槽36’可與硫酸槽36連通，以從硫酸槽36’補充硫酸至硫酸槽36。In other words, as shown in FIG. 2, the ammonium in the wastewater not catalyzed by the second catalyst can be catalyzed into ammonia gas, for example, by the third catalyst, and the ammonia recovery system can further include the second ammonia dialysis module 34. The second ammonia dialysis module 34 includes at least one dialysis membrane and dialysis of the ammonia gas that has been catalyzed by the third catalyst by the dialysis membrane. Among them, the ammonia gas which has been dialyzed by the second ammonia dialysis module 34 reacts with sulfuric acid to obtain ammonium sulfate. Among them, the third catalyst system may be derived, for example, from the catalytic tank 30, and the sulfuric acid system may be derived, for example, from the sulfuric acid tank 36'. The dialysis membrane in the second ammonia dialysis module 34 is a gas permeable dialysis membrane. The venting pore size of the gas permeable membrane may be, for example, 5 μm to 20 μm, or the gas permeability of the gas permeable membrane may be, for example, 0 to 25%. However, in the second ammonia dialysis module 34 of the present invention, the dialysis membrane is not limited to the above-mentioned dialysis membrane and its size, gas permeability and the like, and any dialysis element which can effectively achieve the purpose of separating ammonia gas and ammonia nitrogen wastewater. , are the scope of the claimed invention. Further, as shown in Fig. 2, the ammonia recovery system of the present invention may further comprise a third wastewater tank 42 for containing wastewater which is not dialyzed by the dialysis membrane in the second ammonia dialysis module 34. Similarly, like the sulfuric acid tank 36, the sulfuric acid tank 36' also supplies sulfuric acid to the second ammonia dialysis module 34 in an internal circulation manner, that is, the sulfuric acid in the sulfuric acid tank 36' circulates to the sulfuric acid tank 36' and the second in a circulating manner. Between the ammonia dialysis modules 34. Further, since the amount of ammonium sulfate converted from the first ammonia dialysis module 32 is large, the amount of sulfuric acid consumed in the sulfuric acid tank 36 is also large. Therefore, as shown in Fig. 2, in the present invention, The sulfuric acid tank 36' can be in communication with the sulfuric acid tank 36 to supplement the sulfuric acid from the sulfuric acid tank 36' to the sulfuric acid tank 36.
其中，前述第一催化劑、第二催化劑及第三催化劑係可例如分別為氧化鈣或氫氧化鈉且其pH值範圍可例如為10至12，但不限定於此。The first catalyst, the second catalyst, and the third catalyst system may be, for example, calcium oxide or sodium hydroxide, respectively, and the pH thereof may range, for example, from 10 to 12, but is not limited thereto.
此外，在本發明之第一較佳實施例及第二較佳實施例中，各構件之間可例如以真空管路彼此連接，且真空管路之真空度範圍可例如介於100托耳至760托耳之間，較佳為250托耳，但不限定於此。In addition, in the first preferred embodiment and the second preferred embodiment of the present invention, the members may be connected to each other by, for example, a vacuum line, and the vacuum line may have a vacuum ranging, for example, from 100 to 760 Torr. Between the ears, it is preferably 250 Torr, but is not limited thereto.
以上所述僅為舉例性，而非為限制性者。任何未脫離本發明之精神與範疇，而對其進行之等效修改或變更，均應包含於後附之申請專利範圍中。The above is intended to be illustrative only and not limiting. Any equivalent modifications or alterations to the spirit and scope of the invention are intended to be included in the scope of the appended claims.
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10‧‧‧第一廢水槽 10‧‧‧First Wastewater Tank
12‧‧‧第一熱交換器 12‧‧‧First heat exchanger
14‧‧‧反應槽 14‧‧‧Reaction tank
16‧‧‧第一氨吸收器 16‧‧‧First ammonia absorber
18‧‧‧第二氨吸收器 18‧‧‧Second ammonia absorber
20、20’‧‧‧純水 20, 20’‧‧‧ pure water
22‧‧‧洗滌塔 22‧‧‧ Washing tower
24‧‧‧氨水槽 24‧‧‧Ammonia sink
26、26’‧‧‧第二熱交換器 26, 26' ‧ ‧ second heat exchanger
Claims (10)
一第一廢水槽，該第一廢水槽內設置有含有銨之廢水；
一第一熱交換器，係連通該第一廢水槽，以預熱廢水至一第一溫度；
一反應槽，係連通該第一熱交換器，且該反應槽係令一第一催化劑與經該第一熱交換器預熱之廢水反應而得氨氣；以及一第一氨吸收器，係連通該反應槽，該第一氨吸收器係藉由一第二熱交換器以冷卻該第一氨吸收器至一第二溫度，並藉由噴灑純水使得氨氣溶於純水中以轉化成氨水。An ammonia recovery system comprising at least:
a first wastewater tank, wherein the first wastewater tank is provided with wastewater containing ammonium;
a first heat exchanger connected to the first wastewater tank to preheat the wastewater to a first temperature;
a reaction tank connected to the first heat exchanger, wherein the reaction tank is configured to react a first catalyst with waste water preheated by the first heat exchanger to obtain ammonia gas; and a first ammonia absorber Connecting the reaction tank, the first ammonia absorber is cooled by the second heat exchanger to cool the first ammonia absorber to a second temperature, and the ammonia gas is dissolved in pure water by spraying pure water to be converted. Ammonia water.
一第二廢水槽，連通該反應槽，以容納該反應槽中未被該第一催化劑催化之廢水；
一催化槽，設置有一第二催化劑且連通該第二廢水槽，用以將該第二廢水槽內之廢水中的銨催化成氨氣；
一第一氨滲析模組，包含至少一滲析膜，該第一氨滲析模組係藉由該滲析膜滲析已被該第二催化劑催化之氨氣；以及一硫酸槽，該硫酸槽內設置有硫酸，用以與已被該第一氨滲析模組滲析之氨氣反應而得硫酸銨。For example, the ammonia recovery system described in claim 1 of the patent scope further includes:
a second wastewater tank connected to the reaction tank to accommodate waste water in the reaction tank not catalyzed by the first catalyst;
a catalytic tank, a second catalyst is disposed and communicates with the second wastewater tank for catalyzing ammonium in the wastewater in the second wastewater tank into ammonia gas;
a first ammonia dialysis module comprising at least one dialysis membrane, wherein the first ammonia dialysis module dialyzes ammonia gas catalyzed by the second catalyst by the dialysis membrane; and a sulfuric acid tank, the sulfuric acid tank is provided with Sulfuric acid for reacting with ammonia gas which has been dialyzed by the first ammonia dialysis module to obtain ammonium sulfate.
一第二氨滲析模組，包含至少一另一滲析膜，該第二氨滲析模組係藉由該另一滲析膜滲析已被該第三催化劑催化之氨氣，其中已被該第二氨滲析模組滲析之氨氣與另一硫酸反應而得硫酸銨。The ammonia recovery system of claim 6, wherein the ammonium in the wastewater that is not catalyzed by the second catalyst is catalyzed into ammonia by a third catalyst, and the ammonia recovery system further comprises:
a second ammonia dialysis module comprising at least one further dialysis membrane, the second ammonia dialysis module dialysis of ammonia gas catalyzed by the third catalyst by the another dialysis membrane, wherein the second ammonia has been The ammonia gas dialysis of the dialysis module reacts with another sulfuric acid to obtain ammonium sulfate.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107262501A (en) * | 2017-07-07 | 2017-10-20 | 南通大学 | Reaction unit and nitrogen removal system that aluminium lime-ash is denitrogenated |
| CN107350264A (en) * | 2017-07-07 | 2017-11-17 | 江苏海光金属有限公司 | Fountain aluminium lime-ash denitrogenates method |
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2014
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107262501A (en) * | 2017-07-07 | 2017-10-20 | 南通大学 | Reaction unit and nitrogen removal system that aluminium lime-ash is denitrogenated |
| CN107350264A (en) * | 2017-07-07 | 2017-11-17 | 江苏海光金属有限公司 | Fountain aluminium lime-ash denitrogenates method |
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