JPH06182325A - Removing method for ammonium ion in liquid - Google Patents
Removing method for ammonium ion in liquidInfo
- Publication number
- JPH06182325A JPH06182325A JP33753092A JP33753092A JPH06182325A JP H06182325 A JPH06182325 A JP H06182325A JP 33753092 A JP33753092 A JP 33753092A JP 33753092 A JP33753092 A JP 33753092A JP H06182325 A JPH06182325 A JP H06182325A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- ammonia
- ammonium ions
- water
- membrane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Removal Of Specific Substances (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Degasification And Air Bubble Elimination (AREA)
- Physical Water Treatments (AREA)
Abstract
(57)【要約】
【構成】 アンモニウムイオンを含む液からアンモニウ
ムイオンを除去する方法において、該液にアルカリを添
加し、アンモニウムイオンをアンモニアにした後、気体
は透過するが水は透過させない脱気膜装置に供給して、
該アンモニアを水蒸気とともに膜透過させてアンモニウ
ムイオンを除去することを特徴とする液中のアンモニウ
ムイオンの除去方法。
【効果】 本発明の方法によれば、コンパクトな構成で
アンモニウムイオンを除去し、除去したアンモニウムイ
オンを臭気公害を発生させることなくアンモニア水とし
て回収再利用することができる。
(57) [Summary] [Structure] In a method of removing ammonium ions from a liquid containing ammonium ions, after adding an alkali to the liquid and converting the ammonium ions into ammonia, degassing does not allow water to permeate gas. Supply to the membrane device,
A method for removing ammonium ions in a liquid, characterized in that the ammonia is passed through a membrane together with water vapor to remove ammonium ions. According to the method of the present invention, ammonium ions can be removed with a compact structure, and the removed ammonium ions can be recovered and reused as ammonia water without causing odor pollution.
Description
【０００１】[0001]
【産業上の利用分野】本発明は、液中のアンモニウムイ
オンの除去方法に関し、詳しくは、疎水性多孔質の脱気
膜に接触させ除去する方法である。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for removing ammonium ions in a liquid, and more particularly to a method for contacting and removing a hydrophobic porous degassing membrane.
【０００２】[0002]
【従来の技術】従来、液中のアンモニウムイオン除去方
法としては、アンモニアストリッピング法が一般的であ
る。このアンモニアストリッピング法は、液のｐＨを上
げてアンモニウムイオンを遊離のアンモニアに変えエア
ーストリッピングを行い、該アンモニアを液中から空気
中に移動させ、除去するものである。エアーストリッピ
ングを行う脱アンモニア塔には、空気と液の接触を充分
に行わせるために木製やプラスチック製の充填材が挿入
されており、被処理液はｐＨ調整後脱アンモニア塔上部
より散水され、充填材の間を水滴の形成とその破壊を繰
り返しながら落下させる。その間、脱アンモニア塔には
空気をファンあるいはブロワーによってこの水滴に対し
て対向、あるいは水平方向から吹き付け、アンモニアを
ガスとして水中より空気中に逸散させる方法である。2. Description of the Related Art Conventionally, an ammonia stripping method has been generally used as a method for removing ammonium ions in a liquid. In this ammonia stripping method, the pH of the liquid is raised to change ammonium ions into free ammonia and air stripping is performed, and the ammonia is removed from the liquid by moving it into the air. The deammonification tower that performs air stripping has a wooden or plastic filler inserted to ensure sufficient contact between air and liquid. The liquid to be treated is sprayed from the top of the deammonification tower after pH adjustment. , Drop between the fillers by repeating the formation and destruction of water droplets. Meanwhile, air is blown to the deammonification tower from a horizontal direction by facing the water droplets with a fan or a blower, and ammonia is diffused as a gas from the water into the air.
【０００３】しかし、このアンモニアストリッピング法
には次の問題点がある。第一に、液が充填材の間を落下
する間にアンモニアを除去するので、ストリッピングの
効率を上げるためには、脱アンモニア塔は５〜１０ｍの
塔高が必要で、装置もきわめて大きなものになる。However, this ammonia stripping method has the following problems. First, since the ammonia is removed while the liquid falls between the packing materials, the deammonification tower requires a tower height of 5 to 10 m in order to increase the stripping efficiency, and the equipment is extremely large. become.
【０００４】第二に、ストリッピングの効果を高めるた
めには、投入空気量と被処理水との比いわゆる気液比で
１，８００〜４，５００ｍ3 ／ｍ3 と多量の空気を使用
するため、臭気公害を招く恐れがある放散アンモニアを
経済的に吸収処理することは極めて困難である。そこ
で、最近になり装置全体がコンパクトに構成されたアン
モニウムイオンの除去方法が要求されている。[0004] Secondly, in order to enhance the effect of stripping uses 1,800~4,500m 3 / m 3 and a large amount of air in a ratio so-called gas-liquid ratio of the charged air amount and the water to be treated Therefore, it is extremely difficult to economically absorb and process the emitted ammonia that may cause odor pollution. Therefore, recently, there has been a demand for a method for removing ammonium ions, which is compact in the entire apparatus.
【０００５】[0005]
【発明が解決しようとする課題】本発明者等は、コンパ
クトな構成でアンモニウムイオンを除去し、除去したア
ンモニウムイオンを、臭気公害を発生させることなくア
ンモニア水として回収再利用できるアンモニウムイオン
の除去方法について、新しいタイプの脱気膜による真空
脱気方法すなわち、気体は透過するが水は透過させない
疎水性多孔質膜を用いてアンモニアを真空脱気する方法
の採用について鋭意検討した。DISCLOSURE OF THE INVENTION The present inventors have devised a method for removing ammonium ions which has a compact structure and which can be recovered and reused as ammonia water without generating odor pollution. , A new type of vacuum degassing method using a degassing membrane, that is, a method of vacuum degassing ammonia by using a hydrophobic porous membrane that allows gas to permeate but does not allow water to permeate was studied.
【０００６】その結果、アンモニウムイオンをｐＨ調整
によりアンモニアに変えても、アンモニアの水に対する
溶解度が高いため、水に対する溶解度の小さい空気や酸
素の脱気で行なわれる真空条件すなわち、脱気膜の真空
側の圧力が被処理液の水蒸気圧より高い場合はアンモニ
アがほとんど除去できないのに対し、真空側の圧力を被
処理液の水蒸気圧より低くした特定の条件で運転する場
合には、被処理液からの水蒸気がアンモニアを同伴して
膜の微多孔を通り真空側へ移動し、脱気膜モジュールで
もアンモニアが除去でき、しかも、真空側に移動した水
蒸気とアンモニアは、真空ポンプ出口に設けた凝縮器で
水蒸気を凝縮水に変えることにより、水に対する溶解度
の高いアンモニアが凝縮水に吸収されるので、アンモニ
ア水として回収できることを見いだした。As a result, even if ammonium ions are changed to ammonia by adjusting the pH, the solubility of ammonia in water is high. Therefore, the vacuum condition for degassing air or oxygen, which has low solubility in water, that is, the vacuum of the degassing film. When the pressure on the side is higher than the water vapor pressure of the liquid to be treated, almost no ammonia can be removed.On the other hand, when operating under specific conditions where the pressure on the vacuum side is lower than the water vapor pressure of the liquid to be treated, the liquid to be treated is Water vapor from the gas moves along with ammonia through the micropores of the membrane to the vacuum side, and ammonia can be removed even in the degassing membrane module. Moreover, the water vapor and ammonia that have moved to the vacuum side are condensed at the outlet of the vacuum pump. By changing the steam to condensed water in the reactor, the highly soluble ammonia is absorbed in the condensed water, so it can be recovered as ammonia water. It was found Rukoto.
【０００７】従って、本発明は従来方法に比べ、装置が
コンパクト、特に高さにおいて改善され、臭気公害をだ
す恐れの無い液中のアンモニウムイオンを除去する方法
を提供する事を目的とするものである。Therefore, it is an object of the present invention to provide a method for removing ammonium ions in a liquid which is more compact than the conventional method, particularly improved in height, and which does not cause odor pollution. is there.
【０００８】[0008]
【課題を解決するための手段】本発明は上記の知見に基
づいて更に検討を重ねた結果達成されたもので、その要
旨は、アンモニウムイオンを含む液からアンモニウムイ
オンを除去する方法において、該液にアルカリを添加
し、アンモニウムイオンをアンモニアにした後、気体は
透過するが水は透過させない脱気膜モジュールを設備し
た脱気膜装置に該液を供給して、アンモニアを水蒸気と
ともに膜透過させることを特徴とする液中のアンモニウ
ムイオンの除去方法である。The present invention has been achieved as a result of further studies based on the above findings, and its gist is to provide a method for removing ammonium ions from a solution containing ammonium ions. After adding alkali to ammonia and converting ammonium ion into ammonia, supply the liquid to a degassing membrane device equipped with a degassing membrane module that allows gas to permeate but does not allow water to permeate, and allows ammonia to permeate with water vapor. Is a method for removing ammonium ions in a liquid.
【０００９】以下、本発明方法の具体的構成を図示の実
施例により詳細に説明する。図１は本発明のアンモニウ
ムイオン除去方法の一例を示すフロー図、図２は内圧式
脱気膜モジュールの概念略図を示す。図１に於いて、貯
槽１からポンプ２により送られたアンモニウムイオン含
有液は、アルカリ添加後ミキサー３で攪拌されｐＨ調整
される。ｐＨはアンモニウムイオンがアンモニアに変換
するｐＨ９〜１０付近に調整する。ｐＨ調整された被処
理液は脱気膜モジュール５に供給される。脱気膜装置５
には疎水性多孔質脱気膜モジュールが装着されており、
図２にその概念略図を示す。脱気モジュール５は膜を介
して通液側と真空側に分かれるが、本発明方法によれ
ば、真空側の圧力を真空ポンプ７により通液側の液の水
蒸気圧より低くする事により、通液側の水蒸気にアンモ
ニアガスを同伴させ、この混合気体を膜の微多孔を通し
真空側へ移動させ、液中のアンモニアを除去する。The specific construction of the method of the present invention will be described in detail below with reference to the embodiments shown in the drawings. FIG. 1 is a flow chart showing an example of the ammonium ion removal method of the present invention, and FIG. 2 is a conceptual schematic diagram of an internal pressure type degassing membrane module. In FIG. 1, the ammonium ion-containing liquid sent from the storage tank 1 by the pump 2 is agitated by the mixer 3 after the alkali addition, and the pH is adjusted. The pH is adjusted to around pH 9 to 10 at which ammonium ions are converted to ammonia. The liquid to be treated whose pH has been adjusted is supplied to the degassing membrane module 5. Degassing membrane device 5
Is equipped with a hydrophobic porous degassing membrane module,
FIG. 2 shows a conceptual schematic diagram thereof. Although the degassing module 5 is divided into a liquid-passing side and a vacuum side via a membrane, according to the method of the present invention, the pressure on the vacuum side is made lower than the water vapor pressure of the liquid on the liquid-passing side by the vacuum pump 7, and Ammonia gas is caused to accompany the liquid-side water vapor, and this mixed gas is moved to the vacuum side through the micropores of the membrane to remove ammonia in the liquid.
【００１０】一方、真空側へ移動した水蒸気とアンモニ
アガスの混合気体は、真空ポンプ７出口の凝縮器８で１
０℃以下に冷却する事により水蒸気を凝縮水に変える
と、凝縮水にアンモニアガスが吸収されるので、アンモ
ニアガスを大気に放散することなく、容易にアンモニア
水として回収槽１０に回収できる。本発明において用い
る脱気膜装置の膜は、気体は透過するが水は透過させな
い疎水性多孔質膜であることが必要である。On the other hand, the mixed gas of water vapor and ammonia gas moved to the vacuum side is transferred to the condenser 8 at the outlet of the vacuum pump 1
When the steam is changed to condensed water by cooling to 0 ° C. or lower, the condensed water absorbs the ammonia gas, so that the ammonia gas can be easily recovered in the recovery tank 10 as ammonia water without being emitted to the atmosphere. The membrane of the degassing membrane device used in the present invention needs to be a hydrophobic porous membrane that allows gas to permeate but does not allow water to permeate.
【００１１】疎水性については、水との接触角が９０度
以上ある材質であれば良く、ポリエチレン、ポリプロピ
レン、ポリ四弗化エチレン等が適用できる。膜の孔径に
ついては、耐水圧が１．５ｋｇ／ｃｍ2 以上である孔径
であれば良い。耐水圧は、膜を介し、液側と真空側の圧
力差で液が膜の孔から真空側に漏れ出ない限界の圧力差
を示し液の表面張力、接触角、孔径により変化する。接
触角を９１度表面張力を水の７２ｄｙｎｅ／ｃｍとした
場合、耐水圧１．５ｋｇ／ｃｍ2 を満足する孔径はおよ
そ０．０３μｍ以下となる。With respect to hydrophobicity, any material having a contact angle with water of 90 degrees or more may be used, and polyethylene, polypropylene, polytetrafluoroethylene or the like can be applied. The pore size of the membrane may be any pore size that has a water pressure resistance of 1.5 kg / cm 2 or more. The water pressure resistance shows a limit pressure difference between the liquid side and the vacuum side, which is a pressure difference between the liquid side and the vacuum side, so that the liquid does not leak from the holes of the film to the vacuum side, and varies depending on the surface tension of the liquid, the contact angle, and the hole diameter. When the contact angle is 91 degrees and the surface tension is 72 dyne / cm of water, the pore diameter satisfying the water pressure resistance of 1.5 kg / cm 2 is about 0.03 μm or less.
【００１２】また、モジュールの形式は特に制限され
ず、中空糸膜タイプ、スパイラルタイプ、あるいは平膜
を用いる事ができ、内圧式あるいは外圧式いずれでも良
く、モジュールの置き方も制限されず、水平あるいは垂
直のどちらでも良い。また、本発明方法では、真空側の
圧力を液側の液の水蒸気圧より低くすることが必須条件
であるが、液の水蒸気圧は、液に溶解しているイオンの
濃度、液の温度により変化する。例えば２０℃の水で
は、水蒸気圧は約１８ｍｍＨｇであり、水蒸気を発生さ
せるためには真空側の圧力を水蒸気圧の約１８ｍｍＨｇ
より低くすれば良い。また、真空側に移動した水蒸気
は、真空ポンプ出口（大気圧）の凝縮器で１０℃以下に
冷却する事により、凝縮水になり、アンモニアガスを十
分吸収するのでアンモニア水として回収できる。Further, the form of the module is not particularly limited, and a hollow fiber membrane type, a spiral type, or a flat membrane can be used, and either an internal pressure type or an external pressure type can be used, and the module can be placed in any horizontal direction. Or it may be vertical. In the method of the present invention, it is an essential condition that the pressure on the vacuum side be lower than the water vapor pressure of the liquid on the liquid side, but the water vapor pressure of the liquid depends on the concentration of ions dissolved in the liquid and the temperature of the liquid. Change. For example, with 20 ° C. water, the water vapor pressure is about 18 mmHg, and in order to generate water vapor, the pressure on the vacuum side is about 18 mmHg which is the water vapor pressure.
It should be lower. Further, the water vapor that has moved to the vacuum side becomes condensed water by cooling to 10 ° C. or less in the condenser at the outlet of the vacuum pump (atmospheric pressure), and sufficiently absorbs the ammonia gas, so that it can be recovered as ammonia water.
【００１３】[0013]
【実施例】ｐＨ７、液温２０℃でアンモニウムイオン
１，０００ｍｇ−Ｎ／ｌを含む液にＮａＯＨ溶液を加え
ｐＨ１０に調整し、中空糸膜タイプの疎水性多孔質膜モ
ジュール（外径３０ｍｍ，長さ２００ｍｍ，有効膜面積
０．３ｍ2 ）に通液した。[Example] A pH of 10 was adjusted to pH 10 by adding a NaOH solution to a solution containing 1,000 mg-N / l of ammonium ions at a liquid temperature of 20 ° C and a hollow fiber membrane type hydrophobic porous membrane module (outer diameter 30 mm, long length). The solution was passed through a membrane having a thickness of 200 mm and an effective membrane area of 0.3 m 2 ).
【００１４】流量２００ｍｌ／ｈ、真空側の圧力を１０
ｍｍＨｇ（真空度で１０Ｔｏｒｒ）にした場合、処理液
のアンモニウムイオン濃度は、５５０ｍｇ−Ｎ／ｌ（除
去率＝４５％）であり、処理１時間での回収槽の液量は
８ｍｌとなり、回収液のアンモニア濃度は１．１ｗｔ％
であった。 ［比較例］流量２００ｍｌ／ｈ、真空側の圧力を２５ｍ
ｍＨｇ（真空度で２５Ｔｏｒｒ）にした場合、処理液の
アンモニウムイオン濃度は、１，０００ｍｇ−Ｎ／ｌ
（除去率＝０％）であり、処理１時間での回収槽の液量
は０ｍｌであった。A flow rate of 200 ml / h and a vacuum side pressure of 10
In the case of mmHg (10 Torr in vacuum), the ammonium ion concentration of the treatment liquid was 550 mg-N / l (removal rate = 45%), and the liquid volume in the recovery tank in 1 hour of the treatment was 8 ml. Ammonia concentration is 1.1 wt%
Met. [Comparative example] Flow rate 200 ml / h, vacuum side pressure 25 m
When the pressure is set to mHg (25 Torr in vacuum), the ammonium ion concentration of the treatment liquid is 1,000 mg-N / l.
(Removal rate = 0%), and the liquid volume in the recovery tank in 1 hour of the treatment was 0 ml.
【００１５】[0015]
【発明の効果】本発明の方法によれば、従来のような大
かがりな装置を必要とせずにコンパクトな構成でアンモ
ニウムイオンを除去し、除去したアンモニウムイオンを
臭気公害を発生させることなくアンモニア水として回収
再利用することができる。According to the method of the present invention, ammonium ions can be removed with a compact structure without the need for a large-scale overhanging device as in the prior art, and the removed ammonium ions can be treated with ammonia water without causing odor pollution. It can be recovered and reused.
【図１】本発明の実施態様を示すフローの説明図。FIG. 1 is an explanatory diagram of a flow showing an embodiment of the present invention.
【図２】中空糸タイプの外圧式脱気膜モジュールの概略
図である。FIG. 2 is a schematic view of a hollow fiber type external pressure type degassing membrane module.
１ 貯槽 ２ ポンプ ３ ミキサー ４ ｐＨ検出器 ５ 脱気膜装置 ６ 処理水槽 ７ 真空ポンプ ８ 凝縮器 ９ 冷却水 １０ 回収槽 １１ 被処理液入口 １２ 処理液出口 １３ 中空糸脱気膜 １４ 脱気ガス出口 1 Storage Tank 2 Pump 3 Mixer 4 pH Detector 5 Degassing Membrane Device 6 Treatment Water Tank 7 Vacuum Pump 8 Condenser 9 Cooling Water 10 Recovery Tank 11 Treatment Liquid Inlet 12 Treatment Liquid Outlet 13 Hollow Fiber Degassing Membrane 14 Degassing Gas Outlet
フロントページの続き (72)発明者 岡田 宗久 東京都千代田区丸の内二丁目５番２号 三 菱化成株式会社内 (72)発明者 長橋 由規雄 東京都千代田区丸の内三丁目２番３号 日 本錬水株式会社内 (72)発明者 渡辺 力 東京都千代田区丸の内三丁目２番３号 日 本錬水株式会社内Front Page Continuation (72) Inventor Munehisa Okada 2-5-2 Marunouchi, Chiyoda-ku, Tokyo Sanryo Kasei Co., Ltd. (72) Inventor Yukio Nagahashi 3-2-3 Marunouchi, Chiyoda-ku, Tokyo Ren Nihon Ren Water Co., Ltd. (72) Inventor Tsuyoshi Watanabe 3 2-3 Marunouchi, Chiyoda-ku, Tokyo Nihon Renshui Co., Ltd.
Claims (1)
ニウムイオンを除去する方法において、該液にアルカリ
を添加し、アンモニウムイオンをアンモニアにした後、
気体は透過するが水は透過させない脱気膜モジュールを
設備した脱気膜装置に該液を供給して、アンモニアを水
蒸気とともに膜透過させることによりアンモニウムイオ
ンを除去することを特徴とする液中のアンモニウムイオ
ンの除去方法。1. A method for removing ammonium ions from a liquid containing ammonium ions, wherein alkali is added to the liquid to convert ammonium ions into ammonia,
The liquid is supplied to a degassing membrane device equipped with a degassing membrane module that is permeable to gas but impermeable to water, and ammonium ions are removed by membrane permeation of ammonia together with water vapor to remove ammonium ions. Method for removing ammonium ion.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP33753092A JP3235800B2 (en) | 1992-12-17 | 1992-12-17 | Method for removing ammonium ions from liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP33753092A JP3235800B2 (en) | 1992-12-17 | 1992-12-17 | Method for removing ammonium ions from liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06182325A true JPH06182325A (en) | 1994-07-05 |
| JP3235800B2 JP3235800B2 (en) | 2001-12-04 |
Family
ID=18309518
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP33753092A Expired - Fee Related JP3235800B2 (en) | 1992-12-17 | 1992-12-17 | Method for removing ammonium ions from liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3235800B2 (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5762684A (en) * | 1995-11-30 | 1998-06-09 | Dainippon Screen Mfg. Co., Ltd. | Treating liquid supplying method and apparatus |
| US5871566A (en) * | 1994-11-09 | 1999-02-16 | Lang Apparatebau Gmbh | Vented metering pump |
| KR100345728B1 (en) * | 1997-12-16 | 2003-02-19 | 주식회사 포스코 | Method for eliminating nitrogen compounds from coke wastewater using ammonia stripping |
| KR100374008B1 (en) * | 2000-07-31 | 2003-03-03 | 박경렬 | A method for regeneration and separate recovery of waste water, waste absorbent, waste absorbent oil and waste organic solvent etc. which have been involved odor and VOCs. |
| JP2007124931A (en) * | 2005-11-02 | 2007-05-24 | Ccy:Kk | Lactic acid purification method |
| GB2449180A (en) * | 2007-05-11 | 2008-11-12 | Enpar Technologies Inc | Wastewater ammonium extraction and electrolytic conversion to nitrogen gas |
| CN104926009A (en) * | 2015-06-09 | 2015-09-23 | 江苏好山好水环保科技有限公司 | Ammonia-nitrogen wastewater treatment system |
| CN105776715A (en) * | 2016-05-13 | 2016-07-20 | 江苏理工学院 | Cyclic utilization method of sodium hydroxide and nitric acid in aluminum powder production |
| US9560839B2 (en) | 2010-11-17 | 2017-02-07 | Technion Research And Development Foundation Ltd. | Physico-chemical process for removal of nitrogen species from recirculated aquaculture systems |
| JP2019055346A (en) * | 2017-09-19 | 2019-04-11 | 株式会社東芝 | Ammonia separation method, water treatment method, ammonia separation device, and water treatment device |
| US10980220B2 (en) | 2016-03-08 | 2021-04-20 | Technion Research & Development Foundation Limited | Disinfection and removal of nitrogen species from saline aquaculture systems |
| WO2024004828A1 (en) * | 2022-06-27 | 2024-01-04 | Dic株式会社 | Degassing device |
| CN119139888A (en) * | 2024-11-19 | 2024-12-17 | 厦门海洋职业技术学院 | Rotary gas membrane separation equipment and wastewater deamination system thereof |
-
1992
- 1992-12-17 JP JP33753092A patent/JP3235800B2/en not_active Expired - Fee Related
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5871566A (en) * | 1994-11-09 | 1999-02-16 | Lang Apparatebau Gmbh | Vented metering pump |
| US5762684A (en) * | 1995-11-30 | 1998-06-09 | Dainippon Screen Mfg. Co., Ltd. | Treating liquid supplying method and apparatus |
| KR100345728B1 (en) * | 1997-12-16 | 2003-02-19 | 주식회사 포스코 | Method for eliminating nitrogen compounds from coke wastewater using ammonia stripping |
| KR100374008B1 (en) * | 2000-07-31 | 2003-03-03 | 박경렬 | A method for regeneration and separate recovery of waste water, waste absorbent, waste absorbent oil and waste organic solvent etc. which have been involved odor and VOCs. |
| JP2007124931A (en) * | 2005-11-02 | 2007-05-24 | Ccy:Kk | Lactic acid purification method |
| GB2449180A (en) * | 2007-05-11 | 2008-11-12 | Enpar Technologies Inc | Wastewater ammonium extraction and electrolytic conversion to nitrogen gas |
| GB2449180B (en) * | 2007-05-11 | 2012-06-13 | Enpar Technologies Inc | Wastewater ammonium extraction and electrolytic conversion to nitrogen gas |
| US9560839B2 (en) | 2010-11-17 | 2017-02-07 | Technion Research And Development Foundation Ltd. | Physico-chemical process for removal of nitrogen species from recirculated aquaculture systems |
| CN104926009A (en) * | 2015-06-09 | 2015-09-23 | 江苏好山好水环保科技有限公司 | Ammonia-nitrogen wastewater treatment system |
| US10980220B2 (en) | 2016-03-08 | 2021-04-20 | Technion Research & Development Foundation Limited | Disinfection and removal of nitrogen species from saline aquaculture systems |
| CN105776715A (en) * | 2016-05-13 | 2016-07-20 | 江苏理工学院 | Cyclic utilization method of sodium hydroxide and nitric acid in aluminum powder production |
| JP2019055346A (en) * | 2017-09-19 | 2019-04-11 | 株式会社東芝 | Ammonia separation method, water treatment method, ammonia separation device, and water treatment device |
| WO2024004828A1 (en) * | 2022-06-27 | 2024-01-04 | Dic株式会社 | Degassing device |
| JPWO2024004828A1 (en) * | 2022-06-27 | 2024-01-04 | ||
| CN119139888A (en) * | 2024-11-19 | 2024-12-17 | 厦门海洋职业技术学院 | Rotary gas membrane separation equipment and wastewater deamination system thereof |
| CN119139888B (en) * | 2024-11-19 | 2025-03-11 | 厦门海洋职业技术学院 | Rotary gas membrane separation equipment and wastewater deamination system thereof |
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