CN102964003A - Method for treating ammonia nitrogen in wastewater by using integrated process - Google Patents
Method for treating ammonia nitrogen in wastewater by using integrated process Download PDFInfo
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- CN102964003A CN102964003A CN2012104912106A CN201210491210A CN102964003A CN 102964003 A CN102964003 A CN 102964003A CN 2012104912106 A CN2012104912106 A CN 2012104912106A CN 201210491210 A CN201210491210 A CN 201210491210A CN 102964003 A CN102964003 A CN 102964003A
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Abstract
The invention relates to a method for treating ammonia nitrogen in wastewater by using an integrated process, and the method comprises a magnesium ammonium phosphate chemical precipitation process and a membrane treatment process and comprises the processing steps of collecting water, dosing, adjusting the pH (potential of Hydrogen) value, reacting, precipitating and filtering. The method has the technical characteristics that magnesium salt and phosphate are added during the dosing; a NaOH solution is added to regulate the pH to 8.5-10 during the adjustment; during the reaction, the wastewater retention time is greater than or equal to 30 minutes, the ammonia ion in the wastewater is fully reacted to generate magnesium ammonium phosphate precipitates and heavy metal ion is converted into hydroxide precipitates; the precipitation time is greater than or equal to 6 hours to realize solid-liquid separation during the precipitation; and the supernatant liquid enters a membrane treatment system, the reverse osmosis clear water can be directly discharged and the concentrated water returns to a water collecting tank or is subjected to nanofiltration. The method has the advantages that ammonia nitrogen-containing wastewater with various concentrations can be treated; heating is not needed in the treatment process; the ammonia nitrogen content in the effluent can meet the national first grade effluent standard; and the content of other pollutants such as heavy metals and the like in the effluent can be used for achieving the effluent standard. The method is suitable for treating low-biodegradability ammonia nitrogen-containing wastewater and the ammonia nitrogen-containing wastewater of factories without heat resources.
Description
Technical field
The invention belongs to technical field of waste water processing, particularly the method for ammonia nitrogen in a kind of application combination art breading waste water.
Background technology
Along with day by day expanding of population and developing rapidly of industrial or agricultural, the water environment pollution accident occurs repeatedly, and human and environment has been consisted of serious harm.Many lakes, river are because of the excessive emissions eutrophication of nitrogen, phosphorus, and serious threat is to human productive life and the eubiosis, and ammonia nitrogen is one of principal element that causes body eutrophication.Present stage, the heavy metal pollution of water body event takes place frequently, and HUMAN HEALTH and safety have been caused great impact.How administering ammonia nitrogen, heavy metal wastewater thereby has become one of main task of water treatment field, especially for the improvement of the industry waste water such as the ore deposit choosing that contains simultaneously ammonia nitrogen, heavy metal, metallurgy, plating, electrolysis.
Process in the treatment process of nitrogen-containing wastewater, method commonly used has blow-off method and biochemical process.Although adopt blow-off method to have higher removal efficient, it is high to have investment running cost, and deamination tail gas often needs waste water is heated up in the application of blow-off method simultaneously than the shortcoming of refractory reason, is difficult to realize in the plant area that does not have thermal source.Another kind method biochemical process, be aerobic/anaerobic technique, this technical process is short, construction cost is low, removal effect is reliable and stable, but is only suitable for then being not suitable for for the poor factory effluent of the lower biochemical of BOD/COD in city domestic sewage and the lower sewage disposal of concentration.All there are various shortcomings in other such as methods such as electrochemical treatment, breakpoint chlorination, chemical precipitations, and range of application is little.The improvement of heavy metal wastewater thereby method commonly used is chemical precipitation method, and its main drawback is out that water concentration control is unstable, is difficult to realize direct qualified discharge.
At present, utilize combination process to process nitrogen-containing wastewater and become a kind of development trend.Publication number is the combination process that has proposed a kind of electricity flocculation+biochemical treatment (aerobic/anaerobic)+film processing in the patent of invention of CN 101671090A, publication number is to mention the combination process that biochemical treatment (stabilization pond)+film is processed in the patent of invention of CN 101767890A, two kinds of methods all are applicable to the processing of percolate, but still have the limitation of biochemical processing process; Publication number is the combination process of having announced a kind of blow-off method+film processing+ion-exchange in the patent of invention of CN 101531425A, publication number is the combination process of having announced a kind of blow-off method+chemical precipitation method+breakpoint chlorination in the patent of invention of CN 101555077A, all have the wider scope of application, but the shortcomings such as the combination process scale of investment is large, blow-off method power consumption height are difficult to overcome.For the factory effluent without thermal source, biochemical poor (BOD/COD＜0.1), above combination process all can't be realized the effective removal to ammonia nitrogen.
Summary of the invention
The present invention proposes the method for ammonia nitrogen in a kind of application combination art breading waste water, its objective is the combination process that utilizes a kind of chemical precipitation method+film to process, to overcome unstable, the shortcoming that can't qualified discharge of method of chemical treatment water outlet ammonia nitrogen, simultaneously film is processed the lower concentration nitrogen-containing wastewater, effluent quality is constant, processing efficiency is high combination of advantages is come in, the advantage of two kinds of techniques is embodied, shortcoming with two kinds of techniques overcomes simultaneously, can realize ammonia nitrogen and heavy metal qualified discharge in the waste water, satisfy GB8978-96 " integrated wastewater discharge standard " first discharge standard.
The technical scheme that the present invention proposes is, the method for ammonia nitrogen is comprised of magnesium ammonium phosphate chemical precipitation technique and membrane treatment process in a kind of application combination art breading waste water, and its technological process comprises catchments, the pH value is regulated in dispensing, reaction, precipitation is filtered, and its technical characterictic is:
(1) after nitrogen-containing wastewater is collected water collecting basin, enter the dosing pond, add magnesium salts and phosphoric acid salt, magnesium salts is selected sal epsom (or magnesium oxide, magnesium chloride), phosphoric acid salt is selected Sodium phosphate dibasic (or dipotassium hydrogen phosphate), introduce magnesium ion and phosphate anion, according to ammonia-nitrogen content in the former water, the ammonia nitrogen mol ratio is n (N): n (P): n (Mg)=1 in interpolation reagent and the waste water: (1.1～1.2): (1.3～1.7);
(2) after fully mixing, enter equalizing tank, add NaOH solution and regulate pH to 8.5～10, determine concrete pH value according to different heavy metal content in the former water of detection, usually select pH=9.5;
(3) enter into reaction tank, waste water stop 〉=30min, ammonium ion fully reacts the generation magnesium ammonium phosphate sediment in the waste water, and heavy metal ion is converted into the precipitation of hydroxide thing;
Principal reaction is: NH
4 ++ Mg
2++ PO
4 3-+ 6H
2O=MgNH
4PO
46H
2O ↓ ksp=2.5 * 10
-13
Side reaction: R
N++ nOH
-=R (OH)
n↓
3R
n++n?PO
4 3-＝R
3(PO
4)
n↓
R in the formula
N+The expression heavy metal cation.
(4) enter settling tank, precipitate 〉=6 hours, realize solid-liquid separation;
(5) the settling tank supernatant liquor enters film processing system, and film processing system comprises sand filtration, nanofiltration and reverse osmosis, filters suspended particle by sand filtration, enters nanofiltration, working pressure 1～2.5MPa, nanofiltration clear water producing water ratio 〉=75%;
The nanofiltration clear water enters reverse osmosis, working pressure 1～2.5MPa, and reverse osmosis clear water producing water ratio 〉=80%, the reverse osmosis clear water is except a small amount of flushing nanofiltration membrane that is used for, and all the other can directly discharge, and dense water returns water collecting basin or nanofiltration;
According to the water yield and water quality, can select to adopt one-level nanofiltration or multistage nanofiltration, every grade of optional majority of nanofiltration is propped up the form of nanofiltration membrane parallel connection.
According to draining water quality and the water yield, can select to adopt first-stage reverse osmosis or multistage reverse osmosis, every grade of optional majority of reverse osmosis is propped up the form of reverse osmosis membrane parallel connection.
Heavy-metal ion removal in the pH regulator process, each heavy metal ion precipitation of hydroxide pH scope is usually
Fe
3+6～12；Cr
3+8～9；Cu
2+＞8；Zn
2+9～10；Sn
2+8；Ni
2+＞9.5；Pb
2+?9～9.5；Cd
2+＞10；Fe
2+5～12；Mn
2+10～14。
Advantage of the present invention: can process various concentration nitrogen-containing wastewaters, not need heating in the treating processes, the water outlet ammonia nitrogen can satisfy national grade one discharge standard, can guarantee simultaneously in the water outlet other pollutant discharge in compliance with the standards such as heavy metal, realizes sewage zero-discharge.The present invention is particularly useful for processing low biochemical nitrogen-containing wastewater and without the processing of the nitrogen-containing wastewater of thermal source plant area, but is not limited only to this.
Description of drawings
The process flow sheet of ammonia nitrogen in a kind of application combination art breading of Fig. 1 the present invention waste water
Embodiment
In conjunction with Fig. 1, the method for ammonia nitrogen is comprised of magnesium ammonium phosphate chemical precipitation technique and membrane treatment process in a kind of application combination art breading of the present invention waste water, and its technological process comprises catchments, and the pH value is regulated in dispensing, reaction, and precipitation is filtered, and its technical characterictic is:
(1) after nitrogen-containing wastewater is collected water collecting basin, enter medicine system, medicine system comprises dosing pond, stirrer, proof dry powder feeding machine and pipe valve pump etc., adds magnesium salts and phosphoric acid salt by dry powder respectively.Magnesium salts is selected sal epsom (or magnesium oxide, magnesium chloride), phosphoric acid salt is selected Sodium phosphate dibasic (or dipotassium hydrogen phosphate), according to ammonia-nitrogen content in the former water, wherein adding reagent and ammonia nitrogen mol ratio is n (N): n (P): n (Mg)=1: (1.1～1.2): (1.3～1.7).
(2) enter regulation system after fully mixing, comprise equalizing tank, stirrer, dosing pump and pipe valve etc., such waste water slant acidity need to add alkali and regulate the pH value usually.Select NaOH to regulate pH to 8.5～10, determine concrete pH value according to different heavy metal content in the former water of detection, under normal conditions, select pH=9.5.NaOH solution adds by dosing pump.
(3) enter into reactive system behind the adjusting pH, reactive system is mainly reaction tank and stirrer, and waste water stops more than the 30min at this, fully enters settling tank after the reaction, and precipitates more than 6 hours the realization solid-liquid separation in settling tank.
(4) the settling tank supernatant liquor is driven into the film system through pump, filters suspended particle by sand filtration first, enters nanofiltration system again, according to effluent quality control nanofiltration clear water producing water ratio, common nanofiltration clear water producing water ratio 〉=75%, working pressure 1～2.5MPa; The nanofiltration clear water enters reverse osmosis system, and dense water returns water collecting basin.In this process, chemical precipitation method can be processed the again concentrated rear circulation of ammonia nitrogen to low concentration, again remove.According to the water yield and water quality, can select to adopt one-level nanofiltration or multistage nanofiltration, every grade of optional majority of nanofiltration is propped up the form of nanofiltration membrane parallel connection.
(5) after the nanofiltration system clear water entered reverse osmosis, the reverse osmosis clear water was except a small amount of flushing nanofiltration membrane that is used for, and all the other all can directly discharge, and dense water is back to water collecting basin or nanofiltration.Reverse osmosis clear water producing water ratio 〉=80%, working pressure 1～2.5MPa can regulate according to draining water quality.According to the water yield and water quality, can select to adopt first-stage reverse osmosis or multistage reverse osmosis, every grade of optional majority of reverse osmosis is propped up the form of reverse osmosis membrane parallel connection.
Its specific embodiment has:
Embodiment 1: the form of selecting one-level nanofiltration+first-stage reverse osmosis, reverse osmosis concentrated water is back to water collecting basin, magnesium salts is selected sal epsom, phosphoric acid salt is selected Sodium phosphate dibasic, n (N): n (P): n (Mg)=1: 1.1: 1.3, pH=9.5, nanofiltration clear water producing water ratio=85%, working pressure 1.4MPa, reverse osmosis clear water producing water ratio=85%, working pressure 1.6MPa;
Waste water quality: 2m
3/ h, pH=6.4, Mn
2+Concentration 341mg/L, NH
4 +Concentration 1080mg/L.Agitated pool residence time 30min, settling tank residence time 6h.Under these conditions, water outlet NH
4 +Concentration 9mg/L, Mn
2+Concentration 0.5mg/L.
Embodiment 2: the form of selecting one-level nanofiltration+first-stage reverse osmosis, reverse osmosis concentrated water is back to water collecting basin, magnesium salts is selected sal epsom, phosphoric acid salt is selected Sodium phosphate dibasic, n (N): n (P): n (Mg)=1: 1.1: 1.4, pH=9.5, nanofiltration clear water producing water ratio=75%, working pressure 1.2MPa, reverse osmosis clear water producing water ratio=80%, working pressure 1.4MPa;
Waste water quality: 2m
3/ h, pH=6.4, Mn
2+Concentration 341mg/L, NH
4 +Concentration 1080mg/L.Agitated pool residence time 30min, settling tank residence time 6h.Under these conditions, water outlet NH
4 +Concentration 6mg/L, Mn
2+Concentration 0.2mg/L.
Embodiment 3: the form of selecting secondary nanofiltration series connection+first-stage reverse osmosis, reverse osmosis concentrated water is back to water collecting basin, magnesium salts is selected magnesium chloride, phosphoric acid salt is selected Sodium phosphate dibasic, n (N): n (P): n (Mg)=1: 1.1: 1.3, pH=9.5, nanofiltration clear water producing water ratio=85%, working pressure 1.4MPa, reverse osmosis clear water producing water ratio=90%, working pressure 1.8MPa;
Waste water quality: 5m
3/ h, pH=6.4, Mn
2+Concentration 341mg/L, NH
4 +Concentration 1080mg/L.Agitated pool residence time 30min, settling tank residence time 6h.Under these conditions, water outlet NH
4 +Concentration 10mg/L, Mn
2+Concentration 0.3mg/L.
Embodiment 4: the form of selecting one-level nanofiltration+first-stage reverse osmosis, reverse osmosis concentrated water is back to water collecting basin, magnesium salts is selected sal epsom, phosphoric acid salt is selected Sodium phosphate dibasic, n (N): n (P): n (Mg)=1: 1.3: 1.5, pH=8.5, nanofiltration clear water producing water ratio=85%, working pressure 1.4MPa, reverse osmosis clear water producing water ratio=85%, working pressure 1.6MPa;
Waste water quality: 2m
3/ h, pH=5.8, Cu
2+Concentration 53mg/L, NH
4 +Concentration 3340mg/L.Agitated pool residence time 30min, settling tank residence time 6h.Under these conditions, water outlet NH
4 +Concentration 7mg/L, Cu
2+Concentration 0.8mg/L.
Embodiment 5: the form of selecting one-level nanofiltration+first-stage reverse osmosis, reverse osmosis concentrated water is back to water collecting basin, magnesium salts is selected magnesium oxide, phosphoric acid salt is selected Sodium phosphate dibasic, n (N): n (P): n (Mg)=1: 1.1: 1.3, pH=9.5, nanofiltration clear water producing water ratio=75%, working pressure 1.2MPa, reverse osmosis clear water producing water ratio=80%, working pressure 1.4MPa;
Waste water quality: 2m
3/ h, pH=6.1, Ni
2+Concentration 133mg/L, NH
4 +Concentration 2755mg/L.Agitated pool residence time 30min, settling tank residence time 6h.Under these conditions, water outlet NH
4 +Concentration 12mg/L, Ni
2+Concentration 0.9mg/L.
Embodiment 6: the form of selecting one-level nanofiltration+first-stage reverse osmosis, reverse osmosis concentrated water is back to water collecting basin, magnesium salts is selected magnesium oxide, phosphoric acid salt is selected Sodium phosphate dibasic, n (N): n (P): n (Mg)=1: 1.2: 1.3, pH=9, nanofiltration clear water producing water ratio=75%, working pressure 1.2MPa, reverse osmosis clear water producing water ratio=90%, working pressure 1.8MPa;
Waste water quality: 2m
3/ h, pH=5.3, Cr
3+Concentration 292mg/L, NH
4 +Concentration 897mg/L.Agitated pool residence time 30min, settling tank residence time 6h.Under these conditions, water outlet NH
4 +Concentration 5mg/L, Cr
3+Concentration 1.2mg/L.
Claims (5)
1. the method for ammonia nitrogen in the application combination art breading waste water is comprised of magnesium ammonium phosphate chemical precipitation technique and membrane treatment process, and its technological process comprises catchments, and pH value is regulated in dispensing, reaction, and precipitation, filtration, its technical characterictic is:
(1) after nitrogen-containing wastewater is collected water collecting basin, enter the dosing pond, add magnesium salts and phosphoric acid salt, introduce magnesium ion and phosphate anion, according to ammonia-nitrogen content in the former water, the ammonia nitrogen mol ratio is n (N): n (P): n (Mg)=1 in interpolation reagent and the waste water: (1.1～1.2): (1.3～1.7);
(2) after fully mixing, enter equalizing tank, add NaOH solution and regulate pH to 8.5～10, determine concrete pH value according to different heavy metal content in the former water of detection, usually select pH=9.5;
(3) enter into reaction tank, waste water stop 〉=30min, ammonium ion fully reacts the generation magnesium ammonium phosphate sediment in the waste water, and heavy metal ion is converted into the precipitation of hydroxide thing;
(4) enter settling tank, precipitate 〉=6 hours, realize solid-liquid separation;
(5) the settling tank supernatant liquor enters film processing system, and film processing system comprises sand filtration, nanofiltration and reverse osmosis, filters suspended particle by sand filtration, enters nanofiltration, working pressure 1～2.5MPa, nanofiltration clear water producing water ratio 〉=75%;
The nanofiltration clear water enters reverse osmosis, working pressure 1～2.5MPa, and reverse osmosis clear water producing water ratio 〉=80%, the reverse osmosis clear water is except a small amount of flushing nanofiltration membrane that is used for, and all the other can directly discharge, and dense water returns water collecting basin or nanofiltration.
2. the method for ammonia nitrogen in a kind of application combination art breading waste water as claimed in claim 1 is characterized in that adding magnesium salts in the step (1) is sal epsom, or magnesium oxide, or magnesium chloride.
3. the method for ammonia nitrogen in a kind of application combination art breading waste water as claimed in claim 1 is characterized in that adding phosphoric acid salt in the step (1) is Sodium phosphate dibasic, or dipotassium hydrogen phosphate.
4. the method for ammonia nitrogen in a kind of application combination art breading waste water as claimed in claim 1 is characterized in that can select to adopt one-level nanofiltration or multistage nanofiltration, every grade of optional majority of nanofiltration is propped up the form of nanofiltration membrane parallel connection.
5. the method for ammonia nitrogen in a kind of application combination art breading waste water as claimed in claim 1 is characterized in that can select to adopt first-stage reverse osmosis or multistage reverse osmosis, every grade of optional majority of reverse osmosis is propped up the form of reverse osmosis membrane parallel connection.
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103466770A (en) * | 2013-09-27 | 2013-12-25 | 中南大学 | Copper ammonia complexation wastewater treatment method |
| CN103936192A (en) * | 2014-04-02 | 2014-07-23 | 化工部长沙设计研究院 | High-concentration ammonia-nitrogen wastewater treatment process |
| CN106517656A (en) * | 2016-11-16 | 2017-03-22 | 环境保护部南京环境科学研究所 | Collaborative treatment device and method for phosphatizing wastewater and ammonia-nitrogen wastewater |
| CN107235535A (en) * | 2017-06-23 | 2017-10-10 | 中国矿业大学(北京) | A kind of method of advanced treatment of industrial waste water |
| CN108117190A (en) * | 2017-12-14 | 2018-06-05 | 瓮福（集团）有限责任公司 | A kind of technique of phosphate fertilizer plant's Low Concentration Ammonia Containing Wastewater processing |
| CN109626623A (en) * | 2017-10-09 | 2019-04-16 | 上海集承环保技术有限公司 | A kind for the treatment of process of cupric and ammonia nitrogen waste water |
| CN109809597A (en) * | 2019-04-08 | 2019-05-28 | 盛隆资源再生（无锡）有限公司 | A kind of processing method of the high chlorine nitrogen-containing wastewater of nitric acid type |
| CN109928540A (en) * | 2019-03-06 | 2019-06-25 | 广州市广环环保科技有限公司 | A kind of processing of high ammonia-nitrogen wastewater and resource recovering system and method |
| CN110759453A (en) * | 2019-08-07 | 2020-02-07 | 南京工业大学 | Method for removing ammonia nitrogen from biogas slurry |
| CN111377558A (en) * | 2020-03-17 | 2020-07-07 | 航天凯天环保科技股份有限公司 | Synchronous treatment of Fenton iron mud and FePO obtaining4Resource utilization method |
| CN112551729A (en) * | 2021-01-06 | 2021-03-26 | 南京万德斯环保科技股份有限公司 | Treatment method for removing ammonia nitrogen from kitchen wastewater |
| CN114163050A (en) * | 2021-11-12 | 2022-03-11 | 合肥恒力装备有限公司 | Comprehensive treatment process for ammonia nitrogen-containing electroplating aging liquid wastewater |
| CN117228901A (en) * | 2023-11-13 | 2023-12-15 | 中国电力工程顾问集团华东电力设计院有限公司 | System for be used for nuclear power plant to contain ammonia waste water treatment |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5907094A (en) * | 1997-04-14 | 1999-05-25 | Burnham, Iii; Walter V. | Nitrification activity test (NAT): procedure to monitor nitrifier biomass |
| CN100999366A (en) * | 2006-12-30 | 2007-07-18 | 山东大隆实业有限公司 | Coking waste water reuse treatment method |
| CN102674516A (en) * | 2012-05-22 | 2012-09-19 | 河海大学 | Method for circularly treating nitrogen-phosphorus wastewater |
| CN202465422U (en) * | 2012-02-22 | 2012-10-03 | 南京赛佳环保实业有限公司 | Ammonia nitrogen wastewater recycling treatment equipment |
-
2012
- 2012-11-22 CN CN2012104912106A patent/CN102964003A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5907094A (en) * | 1997-04-14 | 1999-05-25 | Burnham, Iii; Walter V. | Nitrification activity test (NAT): procedure to monitor nitrifier biomass |
| CN100999366A (en) * | 2006-12-30 | 2007-07-18 | 山东大隆实业有限公司 | Coking waste water reuse treatment method |
| CN202465422U (en) * | 2012-02-22 | 2012-10-03 | 南京赛佳环保实业有限公司 | Ammonia nitrogen wastewater recycling treatment equipment |
| CN102674516A (en) * | 2012-05-22 | 2012-09-19 | 河海大学 | Method for circularly treating nitrogen-phosphorus wastewater |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103466770A (en) * | 2013-09-27 | 2013-12-25 | 中南大学 | Copper ammonia complexation wastewater treatment method |
| CN103936192A (en) * | 2014-04-02 | 2014-07-23 | 化工部长沙设计研究院 | High-concentration ammonia-nitrogen wastewater treatment process |
| CN103936192B (en) * | 2014-04-02 | 2015-05-27 | 化工部长沙设计研究院 | High-concentration ammonia-nitrogen wastewater treatment process |
| CN106517656A (en) * | 2016-11-16 | 2017-03-22 | 环境保护部南京环境科学研究所 | Collaborative treatment device and method for phosphatizing wastewater and ammonia-nitrogen wastewater |
| CN107235535A (en) * | 2017-06-23 | 2017-10-10 | 中国矿业大学(北京) | A kind of method of advanced treatment of industrial waste water |
| CN109626623A (en) * | 2017-10-09 | 2019-04-16 | 上海集承环保技术有限公司 | A kind for the treatment of process of cupric and ammonia nitrogen waste water |
| CN108117190B (en) * | 2017-12-14 | 2021-04-02 | 瓮福（集团）有限责任公司 | Process for treating low-concentration ammonia nitrogen wastewater of phosphate fertilizer plant |
| CN108117190A (en) * | 2017-12-14 | 2018-06-05 | 瓮福（集团）有限责任公司 | A kind of technique of phosphate fertilizer plant's Low Concentration Ammonia Containing Wastewater processing |
| CN109928540A (en) * | 2019-03-06 | 2019-06-25 | 广州市广环环保科技有限公司 | A kind of processing of high ammonia-nitrogen wastewater and resource recovering system and method |
| CN109928540B (en) * | 2019-03-06 | 2024-02-02 | 广州市广环环保科技有限公司 | High ammonia nitrogen wastewater treatment and resource recovery system and method |
| CN109809597A (en) * | 2019-04-08 | 2019-05-28 | 盛隆资源再生（无锡）有限公司 | A kind of processing method of the high chlorine nitrogen-containing wastewater of nitric acid type |
| CN109809597B (en) * | 2019-04-08 | 2021-06-01 | 盛隆资源再生（无锡）有限公司 | Method for treating nitric acid type high-chlorine ammonia nitrogen-containing wastewater |
| CN110759453A (en) * | 2019-08-07 | 2020-02-07 | 南京工业大学 | Method for removing ammonia nitrogen from biogas slurry |
| CN111377558A (en) * | 2020-03-17 | 2020-07-07 | 航天凯天环保科技股份有限公司 | Synchronous treatment of Fenton iron mud and FePO obtaining4Resource utilization method |
| CN112551729A (en) * | 2021-01-06 | 2021-03-26 | 南京万德斯环保科技股份有限公司 | Treatment method for removing ammonia nitrogen from kitchen wastewater |
| CN114163050A (en) * | 2021-11-12 | 2022-03-11 | 合肥恒力装备有限公司 | Comprehensive treatment process for ammonia nitrogen-containing electroplating aging liquid wastewater |
| CN117228901A (en) * | 2023-11-13 | 2023-12-15 | 中国电力工程顾问集团华东电力设计院有限公司 | System for be used for nuclear power plant to contain ammonia waste water treatment |
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Application publication date: 20130313 |