TWM478683U - Ammonia-nitrogen wastewater treatment apparatus - Google Patents
Ammonia-nitrogen wastewater treatment apparatus Download PDFInfo
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本創作係關於一種廢水處理設備，特別係關於一種含氨氮廢水之處理設備。This creation relates to a wastewater treatment facility, in particular to a treatment facility for ammonia-containing wastewater.
按，高科技產業大量使用含氮化學藥品，因此經常伴隨著大量含氨氮廢水的產生，由於氨氮在硝化過程中會大量消耗水中的溶氧，造成水質惡化，因此含氨氮廢水必須經過處理，降低廢水中的氨氮含量，始得對外排放，以免對環境造成危害。According to the high-tech industry, a large number of nitrogen-containing chemicals are used, so it is often accompanied by a large amount of ammonia-containing wastewater. Because ammonia nitrogen consumes a large amount of dissolved oxygen in the water during the nitrification process, the water quality deteriorates. Therefore, the ammonia-containing wastewater must be treated and reduced. The ammonia nitrogen content in the wastewater is discharged to the outside to avoid harm to the environment.
有鑑於此，本創作之主要目的係提供一種可以有效去除廢水中氨氮的處理設備。In view of this, the main purpose of this creation is to provide a treatment equipment that can effectively remove ammonia nitrogen from wastewater.
為了達成前述及其他目的，本創作提供一種含氨氮廢水之處理設備，其包括一氣提塔、一加熱器、一觸媒反應器及一氣對氣熱交換器。該氣提塔具有一液體入口、一液體出口、一氣體入口、一氣體出口及一氣提室與該液體入口、液體出口、氣體入口及氣體出口連通，該液體入口係供一含氨氮廢水流入該氣提室，該氣體入口係供一氣提氣體流入該氣提室而對含氨氮廢水進行氣提，含氨氮廢水經氣提後成為氣提後廢水，氣提氣體於氣提時帶出含氨氮廢水中的氨而成為含氨氣體，該氣體出口係供含氨氣體流出該氣提室，該液體出口則係供氣提後廢水流出該氣提室。該加熱器用以加熱所述含氨氣體而得到加熱氣體。該觸媒反應器用以處理所述加 熱氣體，使加熱氣體中的氨氧化並得到一處理後氣體。該氣對氣熱交換器內部具有一第一路徑及一第二路徑，由氣體出口流出氣提室的所述含氨氣體係經由該氣對氣熱交換器的第一路徑而進入該加熱器，經觸媒反應器處理後的處理後氣體則被導入氣對氣熱交換器的第二路徑，用以令所述含氨氣體與處理後氣體進行熱交換，經熱交換之處理後氣體部分排出至外界，餘份與外界氣體混合後成為所述氣提氣體。其中，氣對氣熱交換器之熱交換效率係根據所述含氨氣體之總熱值而相應調整，令所述熱交換效率隨著所述總熱值之升高而相應地調低，或令所述熱交換效率隨著所述總熱值之降低而相應地調高。In order to achieve the foregoing and other objects, the present invention provides a treatment apparatus for ammonia-containing wastewater comprising a stripper, a heater, a catalyst reactor, and a gas-to-gas heat exchanger. The stripper has a liquid inlet, a liquid outlet, a gas inlet, a gas outlet and a stripping chamber in communication with the liquid inlet, the liquid outlet, the gas inlet and the gas outlet, the liquid inlet is for supplying an ammonia-containing wastewater into the liquid In the stripping chamber, the gas inlet is for stripping gas into the stripping chamber to strip the ammonia-containing wastewater, and the ammonia-containing wastewater is stripped to become post-gas stripping wastewater, and the stripping gas brings out ammonia nitrogen during stripping. The ammonia in the wastewater becomes an ammonia-containing gas, and the gas outlet is for the ammonia-containing gas to flow out of the stripping chamber, and the liquid outlet is for supplying the wastewater to the stripping chamber after the stripping. The heater is for heating the ammonia-containing gas to obtain a heated gas. The catalyst reactor is used to process the addition The hot gas oxidizes the ammonia in the heated gas and obtains a treated gas. The gas-to-gas heat exchanger has a first path and a second path inside, and the ammonia-containing gas system exiting the stripping chamber from the gas outlet enters the heater via the first path of the gas-to-gas heat exchanger The treated gas after being treated by the catalytic reactor is introduced into the second path of the gas-to-gas heat exchanger for heat exchange between the ammonia-containing gas and the treated gas, and the gas portion after the heat exchange treatment It is discharged to the outside, and the remainder is mixed with the outside air to become the stripping gas. Wherein the heat exchange efficiency of the gas-to-gas heat exchanger is adjusted according to the total heat value of the ammonia-containing gas, so that the heat exchange efficiency is correspondingly lowered as the total heat value is increased, or The heat exchange efficiency is correspondingly increased as the total heat value decreases.
為了達成前述及其他目的，本創作還提供一種含氨氮廢水之 處理設備，其包括一氣提塔、一加熱器、一觸媒反應器及一氣對氣熱交換器。該氣提塔具有一液體入口、一液體出口、一氣體入口、一氣體出口及一氣提室與該液體入口、液體出口、氣體入口及氣體出口連通，該液體入口係供一含氨氮廢水流入該氣提室，該氣體入口係供一氣提氣體流入該氣提室而對含氨氮廢水進行氣提，含氨氮廢水經氣提後成為氣提後廢水，氣提氣體於氣提時帶出含氨氮廢水中的氨而成為含氨氣體，該液體出口係供氣提後廢水流出該氣提室，該氣體出口則係供含氨氣體流出該氣提室，所述含氨氣體於流出該氣提室後係與外界氣體混合。該加熱器用以加熱所述混有外界氣體的含氨氣體而得到加熱氣體。該觸媒反應器用以處理所述加熱氣體，使加熱氣體中的氨氧化並得到一處理後氣體。該氣對氣熱交換器內部具有一第一路徑及一第二路徑，所述混有外界氣體的含氨氣體係經由該氣對氣熱交換器的第一路徑而進入該加熱器，經觸媒反應器處理後的處理後氣體則被導入氣對氣熱交換器的第二路徑，用以令所述含氨氣體與處理後氣體進行熱交換，經熱交換之處理後氣體部分排出至外界，餘份成為 所述氣提氣體。其中，氣對氣熱交換器之熱交換效率係根據所述含氨氣體之總熱值而相應調整，令所述熱交換效率隨著所述總熱值之升高而相應地調低，或令所述熱交換效率隨著所述總熱值之降低而相應地調高。In order to achieve the above and other objectives, the present invention also provides a wastewater containing ammonia nitrogen. A processing apparatus comprising a stripper, a heater, a catalyst reactor, and a gas to gas heat exchanger. The stripper has a liquid inlet, a liquid outlet, a gas inlet, a gas outlet and a stripping chamber in communication with the liquid inlet, the liquid outlet, the gas inlet and the gas outlet, the liquid inlet is for supplying an ammonia-containing wastewater into the liquid In the stripping chamber, the gas inlet is for stripping gas into the stripping chamber to strip the ammonia-containing wastewater, and the ammonia-containing wastewater is stripped to become post-gas stripping wastewater, and the stripping gas brings out ammonia nitrogen during stripping. The ammonia in the waste water becomes an ammonia-containing gas, and the liquid outlet is supplied to the stripping chamber after the gas is supplied, and the gas outlet is for the ammonia-containing gas to flow out of the stripping chamber, and the ammonia-containing gas flows out of the stripping chamber. The post-chamber is mixed with outside air. The heater is for heating the ammonia-containing gas mixed with an external gas to obtain a heated gas. The catalyst reactor is for treating the heated gas to oxidize ammonia in the heated gas and to obtain a treated gas. The gas-to-gas heat exchanger has a first path and a second path inside, and the ammonia-containing gas system mixed with the external gas enters the heater through the first path of the gas-to-gas heat exchanger, and is touched The treated gas after the treatment of the media reactor is introduced into the second path of the gas-to-gas heat exchanger for heat exchange between the ammonia-containing gas and the treated gas, and the gas is partially discharged to the outside after the heat exchange treatment. , the remainder becomes The stripping gas. Wherein the heat exchange efficiency of the gas-to-gas heat exchanger is adjusted according to the total heat value of the ammonia-containing gas, so that the heat exchange efficiency is correspondingly lowered as the total heat value is increased, or The heat exchange efficiency is correspondingly increased as the total heat value decreases.
本創作藉由依據含氨氣體之總熱值來調整氣對氣熱交換器 的熱交換效率，使得系統的操作溫度可以得到較佳分配，從而使水中氨氮可被有效去除。This creation adjusts the gas-to-gas heat exchanger based on the total calorific value of the ammonia-containing gas. The heat exchange efficiency allows the operating temperature of the system to be better distributed so that ammonia nitrogen in the water can be effectively removed.
10‧‧‧氣提塔10‧‧‧Flat Tower
11‧‧‧液體入口11‧‧‧Liquid inlet
12‧‧‧液體出口12‧‧‧Liquid exports
13‧‧‧氣體入口13‧‧‧ gas inlet
14‧‧‧氣體出口14‧‧‧ gas export
15‧‧‧氣提室15‧‧‧Air extraction room
20‧‧‧加熱器20‧‧‧heater
30‧‧‧觸媒反應器30‧‧‧catalyst reactor
40‧‧‧氣對氣熱交換器40‧‧‧ gas to gas heat exchanger
41‧‧‧熱交換單元41‧‧‧Heat exchange unit
50‧‧‧洩氣閥50‧‧‧Discharge valve
60‧‧‧液對液熱交換器60‧‧‧Liquid-to-liquid heat exchanger
70‧‧‧進氣閥70‧‧‧Intake valve
P1‧‧‧第一管線P1‧‧‧ first pipeline
P2‧‧‧第二管線P2‧‧‧Second pipeline
P3‧‧‧第三管線P3‧‧‧ third pipeline
P4‧‧‧第四管線P4‧‧‧ fourth pipeline
P5‧‧‧第五管線P5‧‧‧ fifth pipeline
P6‧‧‧第六管線P6‧‧‧ sixth pipeline
P7‧‧‧第七管線P7‧‧‧ seventh pipeline
第1圖係本創作第一實施例之處理設備組成示意圖。Fig. 1 is a schematic view showing the composition of a processing apparatus of the first embodiment of the present invention.
第2圖係本創作第二實施例之處理設備組成示意圖。Fig. 2 is a schematic view showing the composition of a processing apparatus of the second embodiment of the present invention.
第3圖係本創作氣對氣熱交換器之一較佳實施例組成示意圖。Figure 3 is a schematic diagram showing the composition of a preferred embodiment of the gas-to-gas heat exchanger.
第4圖係本創作氣對氣熱交換器另一較佳實施例之示意圖。Figure 4 is a schematic illustration of another preferred embodiment of the present gas-to-gas heat exchanger.
請參考第1圖。在本創作的第一實施例中，一種含氨氮廢水之處理設備包括一氣提塔10、一加熱器20、一觸媒反應器30及一氣對氣熱交換器40。Please refer to Figure 1. In a first embodiment of the present invention, a treatment apparatus for ammonia-containing wastewater includes a stripper 10, a heater 20, a catalyst reactor 30, and a gas-to-gas heat exchanger 40.
該氣提塔10具有一液體入口11、一液體出口12、一氣體入口13、一氣體出口14及一氣提室15與該液體入口11、液體出口12、氣體入口13及氣體出口14連通。The stripper 10 has a liquid inlet 11, a liquid outlet 12, a gas inlet 13, a gas outlet 14, and a stripping chamber 15 in communication with the liquid inlet 11, the liquid outlet 12, the gas inlet 13, and the gas outlet 14.
該液體入口11係供一經由第一管線P1輸送的含氨氮廢水流入該氣提室15。顧名思義，含氨氮廢水是指含有氨氮(ammonia nitrogen)的廢水，氨氮在水中可以銨離子(NH4 + )或氨分子(NH3 )的形式存在，相較於銨離子而言，氨分子更容易揮發，因此含氨氮廢水的pH值較佳是大於10，若pH值高於前揭數值時，水中的氨傾向於以氨分子的型態存在，而較 容易被氣提氣體帶走。可以理解的是，為了調整含氨氮廢水的pH值至前述較佳數值，含氨氮廢水於進入氣提塔之前還可以預先經過一pH值調整之處理，該處理可於一pH調整池內完成，惟對於原本pH值即大於10的含氨氮廢水而言，此pH值調整處理是可以省略的。在可能的實施例中，所述含氨氮廢水還可能含有揮發性有機化合物，所述揮發性有機化合物可為但不限於下列至少一者：丙酮、乙醇、乙醚、二氯甲烷、苯、甲苯及二甲苯。The liquid inlet 11 is for a flow of ammonia-containing wastewater delivered via the first line P1 into the stripping chamber 15. As the name suggests, ammonia-containing wastewater refers to wastewater containing ammonia nitrogen, which can be present in the form of ammonium ions (NH 4 + ) or ammonia molecules (NH 3 ) in water. Compared to ammonium ions, ammonia molecules are easier. Volatilization, so the pH of the ammonia-containing wastewater is preferably greater than 10. If the pH is higher than the previous value, the ammonia in the water tends to exist in the form of ammonia molecules, and is more easily carried away by the stripping gas. It can be understood that, in order to adjust the pH value of the ammonia-containing wastewater to the above preferred value, the ammonia-containing wastewater may be subjected to a pH adjustment process before entering the stripping tower, and the treatment may be completed in a pH adjusting tank. However, for the ammonia-containing wastewater having an original pH value of more than 10, the pH adjustment treatment can be omitted. In a possible embodiment, the ammonia-containing nitrogen wastewater may further contain a volatile organic compound, which may be, but not limited to, at least one of the following: acetone, ethanol, diethyl ether, dichloromethane, benzene, toluene, and Xylene.
該氣體入口13係供一經由第二管線P2輸送的氣提氣體流入 該氣提室15而對含氨氮廢水進行氣提，含氨氮廢水經氣提後成為氣提後廢水，氣提後廢水中的氨含量較含氨氮廢水顯著降低，因為氣提氣體於氣提時會帶出含氨氮廢水中的至少部分氨而成為含氨氣體。在含氨氮廢水中含有揮發性有機化合物的場合，至少部分所述揮發性有機化合物也會於氣提時被氣提氣體帶出，因此含氨氣體中也會含有揮發性有機化合物。The gas inlet 13 is for inflow of a stripping gas delivered via the second line P2. The stripping chamber 15 strips the ammonia-containing wastewater, and the ammonia-containing wastewater is stripped to become post-gas stripping wastewater. The ammonia content in the wastewater after stripping is significantly lower than that in the ammonia-containing wastewater, because the stripping gas is stripped. At least part of the ammonia in the ammonia-containing wastewater is taken out to become an ammonia-containing gas. When the volatile ammonia compound is contained in the ammonia-containing wastewater, at least a part of the volatile organic compound is also taken out by the stripping gas during stripping, and therefore the ammonia-containing gas also contains volatile organic compounds.
該液體出口12係供氣提後廢水流出該氣提室15，而該氣體 出口14則供含氨氣體流出該氣提室15。The liquid outlet 12 is for supplying the waste water out of the stripping chamber 15 after the gas is extracted, and the gas The outlet 14 is for the ammonia-containing gas to flow out of the stripping chamber 15.
在本較佳實施例中，液體入口11及氣體出口14是位於氣提 室15的上側，液體出口12及氣體入口13則是位於氣提室15的下側，藉此令液體及氣體的流動方向相反，並提升氣提效率。In the preferred embodiment, the liquid inlet 11 and the gas outlet 14 are located in the stripping On the upper side of the chamber 15, the liquid outlet 12 and the gas inlet 13 are located on the lower side of the stripping chamber 15, whereby the flow direction of the liquid and the gas are reversed, and the stripping efficiency is improved.
該加熱器20係用以加熱所述含氨氣體而得到加熱氣體，所 述含氨氣體是先經第三管線P3進入氣對氣熱交換器40之後，再經由第四管線P4進入加熱器20。The heater 20 is configured to heat the ammonia-containing gas to obtain a heated gas. The ammonia-containing gas enters the gas-to-gas heat exchanger 40 through the third line P3, and then enters the heater 20 via the fourth line P4.
該觸媒反應器30用以處理經由第五管線P5輸送的所述加熱 氣體，使加熱氣體中的氨以及其他可能存在的揮發性有機化合物氧化並得到一處理後氣體。以氨為例，所述觸媒反應器30中的觸媒可為但不限於矽、鋁、鈰、銅、鎳、鋯、銀、鈀、鉑、銠或其氧化物等無機材料。由於處理 氨或揮發性有機化合物的觸媒並非本創作的創作重點，且為習知技藝之範疇，於此不再多作列舉。The catalyst reactor 30 is configured to process the heating delivered via the fifth line P5 The gas oxidizes ammonia in the heated gas and other volatile organic compounds that may be present and obtains a treated gas. Taking ammonia as an example, the catalyst in the catalyst reactor 30 may be, but not limited to, an inorganic material such as ruthenium, aluminum, ruthenium, copper, nickel, zirconium, silver, palladium, platinum, rhodium or an oxide thereof. Due to processing Catalysts of ammonia or volatile organic compounds are not the focus of this creation, and are within the scope of conventional techniques and will not be enumerated here.
由於氨氣等揮發性物質氧化時會放熱，因此經觸媒反應器 30氧化後的處理後氣體的溫度較高，而氣對氣熱交換器40即是用以令經由第三管線P3輸送的所述含氨氣體與經由第六管線P6輸送的處理後氣體進行熱交換。可以理解的是，氣對氣熱交換器40內部會具有一第一路徑及一第二路徑，兩者原則上並不連通，由氣體出口流出氣提室10的所述含氨氣體係經由該第一路徑而進入該加熱器20，經觸媒反應器30處理後的處理後氣體則被導入氣對氣熱交換器40的第二路徑，俾與含氨氣體進行熱交換。 經處理後之處理氣體經第七管線P7輸送至洩氣閥50而部分排出至外界，餘份則與外界氣體混合後成為所述氣提氣體，並經由第二管線P2再次循環至氣提塔10；所述外界氣體可為空氣，且外界氣體的補充量可經由一進氣閥70調節。Catalytic reactor due to exothermic heat when volatile substances such as ammonia are oxidized The temperature of the treated gas after oxidation is higher, and the gas-to-gas heat exchanger 40 is for heating the ammonia-containing gas transported through the third line P3 and the treated gas transported through the sixth line P6. exchange. It can be understood that the gas-to-gas heat exchanger 40 has a first path and a second path inside, and the two are not in communication with each other. The ammonia-containing gas system exiting the stripping chamber 10 from the gas outlet passes through the The first path enters the heater 20, and the treated gas treated by the catalytic reactor 30 is introduced into the second path of the gas-to-gas heat exchanger 40, and the helium exchanges heat with the ammonia-containing gas. The treated process gas is sent to the vent valve 50 via the seventh line P7 and partially discharged to the outside, and the remainder is mixed with the outside air to become the stripping gas, and is circulated again to the stripping tower 10 via the second line P2. The ambient gas may be air, and the supplemental amount of the outside air may be adjusted via an intake valve 70.
其中，氣對氣熱交換器40之熱交換效率是根據所述含氨氣 體之總熱值而相應調整，令所述熱交換效率可隨著所述總熱值之升高而相應地調低，或令所述熱交換效率可隨著所述總熱值之降低而相應地調高，亦即熱交換效率與總熱值成反比關係。所述熱交換效率調高時，處理後氣體交換給含氨氣體的熱能較多；所述熱交換效率調低時，處理後氣體交換給含氨氣體的熱能較少。藉由此等設計，當含氨氣體的總熱值偏高時，氣對氣熱交換器40的熱交換效率調低，處理後氣體不會給予含氨氣體太多熱能，以避免含氨氣體經觸媒反應器30處理後溫度過高，因為觸媒反應器30溫度過高時容易產生其他有害副產物；相對地，當含氨氣體的總熱值偏低時，氣對氣熱交換器40的熱交換效率調高，處理後氣體給予含氨氣體較多熱能，降低加熱器20額外供給熱量的負擔，並使得加熱氣體經觸媒反應器 30處理後可維持在較適溫度。Wherein the heat exchange efficiency of the gas-to-gas heat exchanger 40 is based on the ammonia-containing gas The total heating value of the body is adjusted accordingly, so that the heat exchange efficiency can be correspondingly lowered as the total heating value increases, or the heat exchange efficiency can be lowered as the total heat value decreases. Correspondingly, the heat exchange efficiency is inversely proportional to the total heat value. When the heat exchange efficiency is increased, the heat energy exchanged to the ammonia-containing gas after treatment is large; when the heat exchange efficiency is lowered, the heat energy exchanged to the ammonia-containing gas after the treatment is less. With such a design, when the total heating value of the ammonia-containing gas is high, the heat exchange efficiency of the gas-to-gas heat exchanger 40 is lowered, and the treated gas does not give too much heat energy to the ammonia-containing gas to avoid the ammonia-containing gas. The temperature is too high after being treated by the catalytic reactor 30, because the harmful temperature of the catalyst reactor 30 is too high, and other harmful by-products are easily generated; relatively, when the total calorific value of the ammonia-containing gas is low, the gas-to-gas heat exchanger The heat exchange efficiency of 40 is increased, and the treated gas gives more heat to the ammonia-containing gas, reduces the burden of additional heat supply to the heater 20, and allows the heated gas to pass through the catalytic reactor. 30 can be maintained at a suitable temperature after treatment.
另一方面，由於含氨氮廢水經氣提成為氣提後廢水的過程中 也會吸收氣提氣體的熱量，因此氣提後廢水的溫度會升高；為了實現溫度的較佳配置，本創作的處理設備還可以包括一液對液熱交換器60，用以令所述含氨氮廢水及氣提後廢水進行熱交換，讓含氨氮廢水預先升溫。由於較高的溫度會降低氨在水中的溶解度，因此廢水中的氨將更容易被氣提氣體帶出。On the other hand, due to the stripping of ammonia-containing wastewater into stripping wastewater The heat of the stripping gas is also absorbed, so the temperature of the wastewater after the stripping is increased; in order to achieve a better temperature setting, the processing apparatus of the present invention may further include a liquid-to-liquid heat exchanger 60 for The ammonia-containing wastewater and the post-extracted wastewater are exchanged for heat to preheat the ammonia-containing wastewater. Since higher temperatures reduce the solubility of ammonia in water, ammonia in the wastewater will be more easily carried out by the stripping gas.
但是，若氣提塔10內的溫度過高，氣提塔10內有可能會產 生鹽類結晶，因此還需避免氣提塔10內部過度升溫。誠如前述，由於至少一部份氣提氣體是由處理後氣體所構成，因此在前述熱交換效率調低的場合，氣提氣體的溫度會提高，但過高的氣提溫度卻有可能導致氣提塔10內產生鹽類結晶。為了解決這樣的問題，可以增加熱交換後之處理後氣體之排出量，亦即讓更多處理後氣體經由洩氣閥50排出，這樣的作法可以減少氣提氣體所含總熱量，從而改善氣提塔10容易過度升溫的情形；當然，為了維持系統內的氣壓，當處理後氣體之排出量增加時，外界氣體的補充量也會相應地調高，且在本實施例中，增加外界氣體的補充量還有其他好處在於，由於外界氣體的溫度一般為常溫且低於處理後氣體的溫度，因此當處理後氣體與外界氣體相混之後，所得的氣提氣體之溫度可以降低(相較於處理後氣體而言)，從而輔助減少氣提塔10溫度過度提升的問題。However, if the temperature in the stripper 10 is too high, there may be a production in the stripper 10. The salt is crystallized, so it is also necessary to avoid excessive temperature rise inside the stripper 10. As described above, since at least a part of the stripping gas is composed of the treated gas, when the heat exchange efficiency is lowered, the temperature of the stripping gas is increased, but an excessively high stripping temperature may cause Salt crystals are produced in the stripper 10. In order to solve such a problem, it is possible to increase the discharge amount of the treated gas after the heat exchange, that is, to allow more of the treated gas to be discharged through the vent valve 50, which can reduce the total heat contained in the stripping gas, thereby improving the stripping The tower 10 is prone to excessive temperature rise; of course, in order to maintain the air pressure in the system, when the discharge amount of the treated gas is increased, the amount of external gas replenishment is correspondingly increased, and in the present embodiment, the external gas is increased. The other advantage of the replenishing amount is that since the temperature of the external gas is generally normal temperature and lower than the temperature of the treated gas, when the treated gas is mixed with the external gas, the temperature of the obtained stripping gas can be lowered (compared with The treated gas) assists in reducing the problem of excessive temperature rise of the stripper 10.
另一方面，如果氣提塔的氣提效能不足，亦即處理後廢水的 氨氮濃度未低於預定值時，可以調整氣對氣熱交換器的處理後氣體出口溫度來改善，此一目的可由調整氣對氣熱交換器的熱交換效率來實現，藉此，氣提氣體的溫度可以提升，於氣提的同時可以讓含氨氮廢水提升至較高的溫度，讓水中的氨氮更容易被帶出，以增加氣提效能。On the other hand, if the stripping efficiency of the stripper is insufficient, that is, the treated wastewater When the ammonia nitrogen concentration is not lower than the predetermined value, the treated gas outlet temperature of the gas-to-gas heat exchanger can be adjusted to be improved. This purpose can be achieved by adjusting the heat exchange efficiency of the gas-to-gas heat exchanger, whereby the stripping gas is obtained. The temperature can be increased, and the ammonia-containing wastewater can be raised to a higher temperature while being stripped, so that the ammonia nitrogen in the water can be more easily taken out to increase the gas stripping efficiency.
在前述實施例中，外界氣體是在處理後氣體經熱交換之後才 與其混合，惟在如第2圖所示的本創作第二實施例中，含氨氣體也可先與外界氣體混合後，再進入氣對氣熱交換器40，而後依序經由加熱器20及觸媒反應器30處理而成為處理後氣體，所述處理後氣體進入氣對氣熱交換器40而與含氨氣體進行熱交換，熱交換後的處理後氣體部分排出至外界後，餘份成為所述氣提氣體繼續循環。In the foregoing embodiment, the external gas is only after the heat exchange of the treated gas. In combination with the second embodiment of the present invention as shown in FIG. 2, the ammonia-containing gas may be first mixed with the outside air, then enter the gas-to-gas heat exchanger 40, and then sequentially passed through the heater 20 and The catalyst reactor 30 processes to become a treated gas, and the treated gas enters the gas-to-gas heat exchanger 40 to exchange heat with the ammonia-containing gas, and after the heat exchange, the treated gas is partially discharged to the outside, and the remaining portion becomes The stripping gas continues to circulate.
如第3圖所示，為了讓氣對氣熱交換器40的熱交換效率可 得調整，所述氣對氣熱交換器40可以具有若干熱交換單元41，並選擇性地令經由第三管線P3輸送的含氨氣體與經由第六管線P6輸送的處理後氣體進入其中一所述熱交換單元41進行熱交換，從而，藉由改變熱交換單元41的切換頻率，氣對氣熱交換器40的熱交換效率即可得到調整。對此，本創作的處理設備還可以包括一微控制器(未繪示)及一總熱值偵測單元(未繪示)，總熱值偵測單元用以偵測含氨氣體的總熱值並輸出一總熱值訊號至微控制器，微控制器則根據總熱值訊號，藉由控制第三、第六管線P3、P6閥體的啟閉來調整熱交換單元41之間的切換頻率，進而實現調整氣對氣熱交換器40的熱交換效率的目的。作為一種可能的實施方式，總熱值偵測單元可以包括一用以偵測一或多種揮發性物質(包含氨及其他揮發性有機化合物)濃度的濃度計及一測量含氨氣體的溫度之溫度計，而後再根據所測得的濃度及溫度換算得出含氨氣體的總熱值並發出所述總熱值訊號。As shown in Fig. 3, in order to make the heat exchange efficiency of the gas-to-gas heat exchanger 40 Alternatively, the gas-to-gas heat exchanger 40 may have a plurality of heat exchange units 41 and selectively cause the ammonia-containing gas delivered via the third line P3 and the treated gas delivered via the sixth line P6 to enter one of the The heat exchange unit 41 performs heat exchange, whereby the heat exchange efficiency of the gas-to-gas heat exchanger 40 can be adjusted by changing the switching frequency of the heat exchange unit 41. In this regard, the processing device of the present invention may further include a microcontroller (not shown) and a total calorific value detecting unit (not shown), and the total calorific value detecting unit is configured to detect the total heat of the ammonia-containing gas. And outputting a total calorific value signal to the microcontroller, and the microcontroller adjusts the switching between the heat exchange units 41 by controlling the opening and closing of the third and sixth pipelines P3 and P6 according to the total heating value signal. The frequency, in turn, achieves the purpose of adjusting the heat exchange efficiency of the gas-to-gas heat exchanger 40. As a possible implementation manner, the total calorific value detecting unit may include a concentration meter for detecting the concentration of one or more volatile substances (including ammonia and other volatile organic compounds) and a thermometer for measuring the temperature of the ammonia-containing gas. Then, the total heating value of the ammonia-containing gas is converted according to the measured concentration and temperature, and the total heating value signal is issued.
前述實施例中，熱交換單元41是以兩個為例，實際上熱交 換單元41的數量也可改為三個或更多，同樣可藉由熱交換單元41之間的切換頻率，實現調整熱交換效率的目的。除此之外，氣對氣熱交換器40的熱交換效率也可以其他方式調整，例如使用如第4圖所示的轉輪式熱交換器作為氣對氣熱交換器40，此時可藉由調整轉輪式熱交換器的轉輪旋轉速度 而調整其熱交換效率。In the foregoing embodiment, the heat exchange unit 41 is exemplified by two, in fact, hot The number of the changing units 41 can also be changed to three or more, and the purpose of adjusting the heat exchange efficiency can also be achieved by the switching frequency between the heat exchange units 41. In addition, the heat exchange efficiency of the gas-to-gas heat exchanger 40 can be adjusted in other manners, for example, using a rotary heat exchanger as shown in Fig. 4 as the gas-to-gas heat exchanger 40. Rotating speed of the wheel by adjusting the rotary heat exchanger And adjust its heat exchange efficiency.
基於前揭設計，本創作的含氨氮廢水處理設備可以調節系統中的熱能分配，使系統中的各單元於較佳的溫度條件下運作，進而提升處理設備的操作效能，實現有效去除氨氮的目的。Based on the previous design, the ammonia-containing wastewater treatment equipment of the present invention can adjust the heat energy distribution in the system, so that the units in the system operate under the better temperature conditions, thereby improving the operation efficiency of the processing equipment and achieving the purpose of effectively removing ammonia nitrogen. .
最後，必須再次說明的是，本創作於前揭實施例中所揭露的構成元件僅為舉例說明，並非用來限制本案之範圍，其他等效元件的替代或變化，亦應為本案之申請專利範圍所涵蓋。Finally, it must be stated that the constituent elements disclosed in the foregoing embodiments are merely illustrative and are not intended to limit the scope of the present invention. Alternatives or variations of other equivalent elements should also be applied for in this case. Covered by the scope.
10‧‧‧氣提塔10‧‧‧Flat Tower
11‧‧‧液體入口11‧‧‧Liquid inlet
12‧‧‧液體出口12‧‧‧Liquid exports
13‧‧‧氣體入口13‧‧‧ gas inlet
14‧‧‧氣體出口14‧‧‧ gas export
15‧‧‧氣提室15‧‧‧Air extraction room
20‧‧‧加熱器20‧‧‧heater
30‧‧‧觸媒反應器30‧‧‧catalyst reactor
40‧‧‧氣對氣熱交換器40‧‧‧ gas to gas heat exchanger
50‧‧‧洩氣閥50‧‧‧Discharge valve
60‧‧‧液對液熱交換器60‧‧‧Liquid-to-liquid heat exchanger
70‧‧‧進氣閥70‧‧‧Intake valve
P1‧‧‧第一管線P1‧‧‧ first pipeline
P2‧‧‧第二管線P2‧‧‧Second pipeline
P3‧‧‧第三管線P3‧‧‧ third pipeline
P4‧‧‧第四管線P4‧‧‧ fourth pipeline
P5‧‧‧第五管線P5‧‧‧ fifth pipeline
P6‧‧‧第六管線P6‧‧‧ sixth pipeline
P7‧‧‧第七管線P7‧‧‧ seventh pipeline
Claims (8)
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
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| TW103200858U TWM478683U (en) | 2014-01-15 | 2014-01-15 | Ammonia-nitrogen wastewater treatment apparatus |
| CN201410290249.0A CN104772035B (en) | 2014-01-15 | 2014-06-25 | Volatile organic compound processing device |
| CN201420344061.5U CN203990301U (en) | 2014-01-15 | 2014-06-25 | Volatile organic compound processing device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| TW103200858U TWM478683U (en) | 2014-01-15 | 2014-01-15 | Ammonia-nitrogen wastewater treatment apparatus |
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| Publication Number | Publication Date |
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| TWM478683U true TWM478683U (en) | 2014-05-21 |
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