CN102219323A - Method for simultaneously removing organic pollutants and ammonia in waste water and reactor - Google Patents
Method for simultaneously removing organic pollutants and ammonia in waste water and reactor Download PDFInfo
- Publication number
- CN102219323A CN102219323A CN 201110079739 CN201110079739A CN102219323A CN 102219323 A CN102219323 A CN 102219323A CN 201110079739 CN201110079739 CN 201110079739 CN 201110079739 A CN201110079739 A CN 201110079739A CN 102219323 A CN102219323 A CN 102219323A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- reactor
- waste water
- stripping
- water
- 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
Images
Landscapes
- Physical Water Treatments (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
A method for simultaneously removing organic pollutants and ammonia in waste water and a reactor. The method provided by the invention simultaneously accomplishes the degradation of organic pollutants by the activated oxygen catalytic oxidation and the removal of ammonia by spraying and air-stripping in the same reactor. The reactor, which comprises an upper part for stripping and removing ammonia and a lower part for the activated oxygen catalytic oxidation, is mainly composed of a housing, a water distributor, atomizing nozzles, a catalyst, a power pump, porous trays, a microporous aeration plate, air pumps and an air intake. The method provided by the invention is characterized in that waste water undergoes the pH value adjustment and flows into the atomizing nozzles from the upper water distributor; air flows into the reactor from the microporous aeration plate or the air intake; ammonia is stripped and removed during the fogdrop dripping process on one hand and through porous trays on the other hand; ammonia gas flows out of an outlet on the top and then is sent for a next treatment; fogdrop drips into an activated oxygen catalytic oxidation pool on the bottom; air flows from the microporous aeration plate on the bottom and reacts with the catalyst in the catalytic oxidation pool so as to produce oxygen-containing free radicals to remove organic pollutants in the waste water. The method for simultaneously removing organic pollutants and ammonia in waste water and the reactor in the invention are suitable for the treatment of diversified ammonia-containing organic waste water.
Description
Technical field
The present invention relates to a kind of method and reactor of removing organic pollutant and ammonia in the waste water simultaneously, belong to technical field of water pollution control.
Background technology
As a kind of widely used water treatment high-level oxidation technology, in that the Fenton oxidation is specially adapted to some refractory such as phenols, arylamine class, aromatic hydrocarbons, agricultural chemicals and nuke rubbish reason or the processing to the virose trade effluent of biology.Why Fenton reagent has very strong oxidation capacity is that OH compares with other oxygenant has stronger oxidizing electrode current potential (2.8V), than ozone (O because hydrogen peroxide can produce hydroxyl radical free radical (OH) under the katalysis of iron ion
3, 2.07V), and hydrogen peroxide (hydrogen peroxide, 1.77V) respectively high 35% and 59%, oxidation capacity is only second to fluorine; In addition, OH also has high electronegativity (Electron Affinities), and its electron affinity is 569.3KJ, the easy high cloud density point of attack, and then realize that as intermediate product the deep oxidation of pollutent decomposes O
3, hydrogen peroxide, Cl
2, strong oxidizer intermediate product such as O, utilize the strong oxidizing property of these intermediate products the organism complete oxidation in the waste water can be CO
2And H
2O.Traditional Fenton's reaction exists the restriction aspect three when large-scale application: 1. must carry out in the acidic medium of pH＜3; 2. conventional Fenton catalyzer (Fe
2+Or Fe
3+) existence form in the aqueous solution is subjected to the influence of factors such as the potential of hydrogen of medium, total concentration of iron, shelf-time, its separation and recycle and face many difficulties; Although 3. H
2O
2Be a kind of oxygen source convenient for cleaning, but it exist and cost an arm and a leg poor stability, the restriction of aspects such as shortcoming that utilization ratio is low and accumulating.Thus, the Fenton technology of many materializations unit combination such as light-Fenton technology, electricity-Fenton technology, ultrasonic-the Fenton technology, photoelectricity-Fenton technology etc. are arisen at the historic moment; Simultaneously, be the deficiency that the out-phase Fenton's reaction of representative also can solve traditional Fenton's reaction with Zero-valent Iron and mixture thereof.But present Fenton system does not still solve H
2O
2Cost an arm and a leg and shortcoming that utilization ratio is low.
Petrochemical industry, metallurgy, the ammonia-containing water that industries such as food produce has increased the weight of the eutrophication of water body.Ammonia nitrogen waste water has caused the attention of environmental protection field and global range to the influence of environment.Research and development are economical, denitrogenate emphasis and focus that treatment technology has become water pollution control engineering area research efficiently.The main method of removing ammonia nitrogen has: physics method, chemical method, biological process.The at present widely used ammonia technology of removing mainly comprises ion exchange method, stripping-vaporizing extract process, chemical precipitation method, break point chlorination, catalytic pyrolysis etc.Though the ion exchange method ammonia nitrogen removal frank is high, when ammonia nitrogen concentration was high, resin regeneration was frequent, operational difficulty, and regenerated liquid still is a high ammonia-nitrogen wastewater, reagent consumption is big, the processing cost height; Air stripping method is to utilize the difference that exists between the actual concentrations of volatile matter such as ammonia nitrogen contained in the waste water and the equilibrium concentration, under alkaline condition with air stripping or steam stripped, volatile matter such as ammonia nitrogen in the waste water are constantly transferred to the gas phase from liquid phase, thereby reach the purpose of removing ammonia nitrogen in the waste water, blow-off method is removed ammonia nitrogen, clearance can reach 60%～95%, technical process is simple, treatment effect is stable, the ammonia that stripping goes out absorbs generation ammonium chloride with hydrochloric acid can be back to soda ash production as mother liquor, also can be according to the market requirement, water absorb to be produced ammoniacal liquor or is produced the ammonium sulfate byproduct with sulfuric acid absorption, and tail gas returns in the stripping tower, but water temperature is when low, stripping efficient is low, is not suitable for using in the winter of cold; Chemical precipitation method is by add certain chemical agent in ammonia nitrogen waste water, make it with waste water in some dissolubility pollutant matter react, the formation difficulty soluble salt precipitates, thereby the method for dissolubility pollutant concentration in the reduction water, chemical precipitation method can be handled the ammonia nitrogen waste water of various concentration, is particularly suitable for the processing of high-concentration ammonia nitrogenous wastewater; Break point chlorination is to add excessive chlorine or clorox, is that the ammonia complete oxidation in the waste water is N
2Method, this method speed of response is fast, needs equipment few, but the safe handling of liquid chlorine and store to require highly, processing cost is also higher; Catalytic pyrolysis provides the comprehensive treating process and the recovery method that contain ammonia/ammonium waste water that produces in a kind of Catalyst Production technology.But the waste water ammonia-removal method all can not effectively be removed for the organic pollutant in the waste water bar none at present.
At present organic pollutant and the method for ammonia and the document of reactor rarely have report in the waste water about removing simultaneously." Fudan Journal " (2006 the 45th the 3rd phases of volume) reported the research paper that is entitled as " influence factor that electrochemical oxidation process removes ammonia nitrogen ", this result of study shows that the electrochemical oxidation process Treating Municipal Sewage can drop to 6.1mg/L from 26.8 with the preliminary sedimentation tank ammonia nitrogen concentration, second pond goes out after the water treatment ammonia nitrogen concentration and reduces to 0.1mg/L from 19.9, and this process can be removed the organism in the municipal effluent to a certain extent simultaneously; Have not yet to see about removing organic pollutant and the method for ammonia and the patent of reactor in the waste water simultaneously, domestic only relevant for organic pollutant in the Fenton oxidation removal waste water respectively with remove the relevant patent of ammonia with blow-off method, utility model patent of invention as CN2937066Y discloses the patent that is entitled as " the high dispersive spraying removes the ammonia tower ", this utility model provides a kind of high dispersive spraying to remove the ammonia tower, its high dispersive arrangements of elements is in removing ammonia Tata body, be positioned at the top of air intake sparger, the high dispersive element is by atomizing nozzle and divide water distributor to form, atomizing nozzle is provided with up or down, communicates with service pump by minute water distributor and water inlet pipe; This tower adopts the high dispersive element that ammonia nitrogen waste water is carried out high dispersing and handles, and increases the flowing fluid ratio surface-area, has improved to be dissolved in the speed that the free ammonia in the water is escaped from liquid phase, thereby has reached the purpose of ammonia nitrogen removal in the solution.The patent of invention of CN101445290A discloses and has been entitled as the patent of " a kind of environmental protection, waste water ammonia-removal process and equipment thereof " efficiently for another example, this invention adopts dilute acid soln to absorb except that the ammonia in the ammonia tail gas, adopt pipeline to introduce blower inlet the air that does not contain ammonia or contain micro-ammonia and recycle, make except that ammonia efficient to maintain in the higher scope.
The inventive method is that the waste water degassing that contains organic pollutant and ammonia removes ammonia after the Fenton oxidation removal organic pollutant of catalytic activation molecular oxygen.Contain ammonia organic waste water and spray into reactor from atomizing nozzle via aeration tube, start pneumatic pump from inlet mouth via micro-pore aeration plate bubbling air, and regulate air flow quantity, ammonia is removed under the stripping of air in the waste water of atomizing back; Molecular oxygen in the catalyzed oxidation pond of reactor lower end in the catalyzer energy catalytic activation oxidation pond produces the oxide species of strong oxidizing property, thereby removes wastewater organic pollutant.The present invention removes the organic pollutant in the waste water and removes ammonia when setting up reactor is applicable to the various ammonia treatment of Organic Wastewater that contain, efficient height, environmental friendliness, non-secondary pollution, facility compact, easy handling, whole reactor is controlled easily, the needs of realistic unit for treating water.
Summary of the invention
The objective of the invention is in same unit for treating water to realize simultaneously that activation oxygen catalyzing oxidizing degrading organic pollutant and spraying stripping remove ammonia, and a kind of reactor that can remove organic pollutant and ammonia in the water simultaneously is provided.
Technical scheme of the present invention is: a kind of method of removing organic pollutant and ammonia in the waste water simultaneously, it is characterized in that, on a top is that stripping removes the ammonia chamber and the bottom is in the reactor in activation oxygen catalyzed oxidation pond, with pending contain ammonia organic waste water and adjust pH after, the atomizing nozzle that removes top, ammonia chamber via the stripping on reactor top sprays into reactor, start pneumatic pump simultaneously, with air via the micro-pore aeration plate of the bottom, activation oxygen catalyzed oxidation pond of reactor lower part expose to the sun into, perhaps expose to the sun into sending into reactor except that the inlet mouth of bottom, ammonia chamber with described stripping via described micro-pore aeration plate, and adjusting air flow quantity, ammonia is removed under the stripping of air in the waste water of atomizing back, and follows air to send next stage to handle after the escape orifice that is positioned at reactor top overflows; Droplet drops down onto the activation oxygen catalyzed oxidation pond of reactor lower part, the catalyst activate molecular oxygen produces the strong oxidizing property oxygen radical in activation oxygen catalyzed oxidation pond, organic pollutant in the oxidation removal waste water, the water after stripping removes ammonia and catalyzed oxidation removal organism flows out from water outlet.
By technique scheme, described catalyzer is ferrous sulfate, ferric sulfate, Zero-valent Iron, ferric oxide, Z 250 or hydrous iron oxide.
By technique scheme, the concentration of catalyzer in waste water is 0.2～1g/L, and in waste water, dissolved oxygen concentration is 0.5-2.0mg/L to molecular oxygen by micro-pore aeration plate dissolved air.
By technique scheme, described pH value is in the 10-12 scope.
A kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously of the present invention, its structure comprise that reactor shell, atomizing nozzle, water outlet, catalyzer, pneumatic pump, micro-pore aeration plate, ammonia escape orifice, charging opening, mud discharging mouth, power water pump, porous plate, stripping remove ammonia chamber, catalyzed oxidation pond, aeration tube, water distributor and inlet mouth; Reactor is made up of except that the catalyzed oxidation pond of ammonia chamber and bottom the stripping on top; Atomizing nozzle is uniform to be installed on the water distributor, be arranged on the interior stripping of reactor and remove top, ammonia chamber, the water distributor import is communicated with the power water pump outlet, porous plate is arranged on the interior stripping of reactor and removes the ammonia chamber) in, position between charging opening and atomizing nozzle, the micro-pore aeration plate is positioned at bottom, reactor catalyzed oxidation pond, on the micro-pore aeration plate of catalyzer in the catalyzed oxidation pond, the pneumatic pump outlet is communicated with inlet mouth and aeration tube, aeration tube extend into micro-pore aeration plate bottom, water outlet is positioned at the bottom of the upper spacer top inlet mouth in catalyzed oxidation pond, and mud discharging mouth is positioned at reactor near the bottom, and the ammonia escape orifice is positioned at reactor head.
In the method for removing organic pollutant and ammonia in the waste water simultaneously of the present invention, ammonia can be removed through stripping in the process that droplet descends on the one hand, can slough via the porous plate after-blow of reactor on the other hand and remove.Porous plate can increase the residence time that the droplet stripping removes ammonia, removes ammonia efficient thereby increase.Ammonia overflows from the ammonia escape orifice that is positioned at reactor top.Droplet drops down onto the catalyzed oxidation pond of reactor lower end, air by the micro-pore aeration plate of bottom, catalyzed oxidation pond expose to the sun into, and produce the strong oxidizing property oxygen radical, the organic pollutant in the oxidation removal waste water behind the catalyst action in the catalyzed oxidation pond.Water after stripping removes ammonia and catalyzed oxidation removal organism flows out from water outlet.By regulating the waste water flow velocity, adjustings such as air flow quantity, pH make the abundant contact reacts of air and catalyzer and waste water, preferably remove ammonia and organic efficient to reach.
Advantage of the present invention is as follows:
1. remove ammonia and catalytic activation molecular oxygen removal organism in conjunction with air stripping, in same reactor, realize removing organic pollutant and ammonia in the water simultaneously.
2. adopt and to utilize atomizing nozzle and porous plate to increase the contact area and the duration of contact of ammonia and gas in the waste water.
3. adopting airborne oxygen molecule is the oxygen source of catalyzed oxidation, and its oxygen source wide material sources are with low cost, good economy performance.
4. various parameters are controlled easily, can be as required conditioned response parameter at any time.
5. remove when the present invention sets up that organic pollutant and ammonia reactor are applicable to the various ammonia treatment of Organic Wastewater that contain in the waste water, facility compact, easy handling, whole reactor is controlled easily, the needs of realistic unit for treating water have very big application potential in the environmental pollution improvement field.
Description of drawings
Fig. 1 is a structural representation of removing the reactor of organism and ammonia in the waste water simultaneously.
Embodiment
The structure of removing the reactor of organism and ammonia in the waste water simultaneously of the present invention as shown in Figure 1.The structure of reactor comprises that reactor shell 1, atomizing nozzle 2, water outlet 3, catalyzer 4, pneumatic pump 5, micro-pore aeration plate 6, ammonia escape orifice 7, charging opening 8, mud discharging mouth 9, power water pump 10, porous plate 11, stripping remove ammonia chamber 12, catalyzed oxidation pond 13, aeration tube 14, water distributor 15 and inlet mouth 16; Reactor is made up of except that the catalyzed oxidation pond 13 of ammonia chamber 12 and bottom the stripping on top; Atomizing nozzle 2 uniform being installed on the water distributor 15, be arranged on the interior stripping of reactor and remove 12 tops, ammonia chamber, water distributor 15 imports are communicated with power water pump 10 outlets, porous plate 11 is arranged on the interior stripping of reactor and removes in the ammonia chamber 12, position between charging opening 8 and atomizing nozzle 2, micro-pore aeration plate 6 is positioned at 13 bottoms, reactor catalyzed oxidation pond, on the micro-pore aeration plate 6 of catalyzer 4 in catalyzed oxidation pond 13, pneumatic pump 5 outlets are communicated with inlet mouth 16 and aeration tube 14, aeration tube 14 extend into micro-pore aeration plate 6 bottoms, water outlet 3 is positioned at the bottom of the upper spacer top inlet mouth 16 in catalyzed oxidation pond 13, mud discharging mouth 9 is positioned at reactor near the bottom, and ammonia escape orifice 7 is positioned at reactor head.
By pneumatic pump 5 air is fed reactors by inlet mouth 16 or via aeration tube 14, contain ammonia organic waste water through atomizing nozzle 2 ejections, the ammonia in the high dispersive droplet of ejection removes under the effect of air, send next stage to handle after ammonia escape orifice 7 is overflowed; Droplet drops down onto the catalyzed oxidation pond of reactor lower part, catalyzer in the catalyzed oxidation pond and micro-pore aeration plate 6 expose to the sun into air reaction generate hyperoxia voltinism oxygen radical, the organic pollutant in the oxidation removal waste water.
Treating refuse percolate in a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously
Get percolate 30L, regulate pH to 12, COD is 1835mg/L, NH
3-N is 1367mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 0.5mg/L, adds ferric sulfate 24g, after 120 minutes, the NH of waste water
3-N is 372mg/L, NH
3The clearance of-N is about 73%, and the COD of waste water is 632mg/L, the clearance of organic pollutant about 65%.
Treating refuse percolate in a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously
Get percolate 30L, regulate pH to 11, COD is 1987mg/L, NH
3-N is 2691mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 1.0mg/L, adds ferric oxide 20g, the NH of waste water
3-N is 989mg/L, NH
3The clearance of-N is about 63%, and after 120 minutes, the COD of waste water is 598mg/L, the clearance of organic pollutant about 70%.
In a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously, handle waste water
Get waste water 30L, pH=12, COD are 1530mg/L, NH
3-N is 1269mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 1.2mg/L, adds ferric sulfate 18g, after 120 minutes, the NH of waste water
3-N is 486mg/L, NH
3The clearance of-N is about 62%, and the COD of waste water is 543mg/L, the clearance of organic pollutant about 65%.
In a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously, handle waste water
Get waste water 30L, pH=11.5, COD are 1610mg/L, NH
3-N is 2013mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 1.4mg/L, adds hydrous iron oxide 25g, after 120 minutes, the NH of waste water
3-N is 983mg/L, NH
3The clearance of-N is about 51%, and the COD of waste water is 812mg/L, the clearance of organic pollutant about 50%.
In a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously, handle waste water
Get waste water 30L, regulate pH to 10, COD is 912mg/L, NH
3-N is 387mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 1.2mg/L, adds sulfurous acid iron 20g, after 120 minutes, the NH of waste water
3-N is 152mg/L, NH
3The clearance of-N is about 61%, and the COD of waste water is 543mg/L, the clearance of organic pollutant about 40%.
In a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously, handle waste water
Get waste water 30L, regulate pH to 12, COD is 1230mg/L, NH
3-N is 296mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 1.5mg/L, adds ferric sulfate 30g, after 120 minutes, the NH of waste water
3-N is 53mg/L, NH
3The clearance of-N is about 82%, and the COD of waste water is 672mg/L, the clearance of organic pollutant about 45%.
In a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously, handle waste water
Get waste water 30L, regulate pH to 11, COD is 793mg/L, NH
3-N is 453mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 1.8mg/L, adds Zero-valent Iron 15g, after 120 minutes, the NH of waste water
3-N is 123mg/L, NH
3The clearance of-N is about 73%, and the COD of waste water is 247mg/L, the clearance of organic pollutant about 70%.
In a kind of reactor of removing organic pollutant and ammonia in the waste water simultaneously, handle waste water
Get 30L, regulate pH to 12, COD is 745mg/L, NH
3-N is 1208mg/L.Waste water sprays into stripping through atomizing nozzle and removes the ammonia chamber, while bubbling air in the catalyzed oxidation pond, and making oxygen in water concentration is 2.0mg/L, adds Z 250 6g, after 120 minutes, the NH of waste water
3-N is 432mg/L, NH
3The clearance of-N is about 74%, and the COD of waste water is 372mg/L, the clearance of organic pollutant about 50%.
Claims (5)
1. method of removing organic pollutant and ammonia in the waste water simultaneously, it is characterized in that, on a top is that stripping removes the ammonia chamber and the bottom is in the reactor in activation oxygen catalyzed oxidation pond, with pending contain ammonia organic waste water and adjust pH after, the atomizing nozzle that removes top, ammonia chamber via the stripping on reactor top sprays into reactor, start pneumatic pump simultaneously, with air via the micro-pore aeration plate of the bottom, activation oxygen catalyzed oxidation pond of reactor lower part expose to the sun into, perhaps expose to the sun into sending into reactor except that the inlet mouth of bottom, ammonia chamber with described stripping via described micro-pore aeration plate, and adjusting air flow quantity, ammonia is removed under the stripping of air in the waste water of atomizing back, and follows air to send next stage to handle after the escape orifice that is positioned at reactor top overflows; Droplet drops down onto the activation oxygen catalyzed oxidation pond of reactor lower part, the catalyst activate molecular oxygen produces the strong oxidizing property oxygen radical in activation oxygen catalyzed oxidation pond, organic pollutant in the oxidation removal waste water, the water after stripping removes ammonia and catalyzed oxidation removal organism flows out from water outlet.
2. a kind of method of removing organic pollutant and ammonia in the waste water simultaneously as claimed in claim 1 is characterized in that described catalyzer is ferrous sulfate, ferric sulfate, Zero-valent Iron, ferric oxide, Z 250 or hydrous iron oxide.
3. a kind of method of removing organic pollutant and ammonia in the waste water simultaneously as claimed in claim 1, it is characterized in that, the concentration of catalyzer in waste water is 0.2～1g/L, and in waste water, dissolved oxygen concentration is 0.5-2.0mg/L to molecular oxygen by micro-pore aeration plate dissolved air.
4. a kind of method of removing organic pollutant and ammonia in the waste water simultaneously as claimed in claim 1 is characterized in that described pH value is in the 10-12 scope.
5. reactor of removing organic pollutant and ammonia in the waste water simultaneously, it is characterized in that the structure of reactor comprises that reactor shell (1), atomizing nozzle (2), water outlet (3), catalyzer (4), pneumatic pump (5), micro-pore aeration plate (6), ammonia escape orifice (7), charging opening (8), mud discharging mouth (9), power water pump (10), porous plate (11), stripping remove ammonia chamber (12), catalyzed oxidation pond (13), aeration tube (14), water distributor (15) and inlet mouth (16); Reactor is made up of except that the catalyzed oxidation pond (13) of ammonia chamber (12) and bottom the stripping on top; Atomizing nozzle (2) is uniform to be installed on the water distributor (15), be arranged on the interior stripping of reactor and remove top, ammonia chamber (12), water distributor (15) import is communicated with power water pump (10) outlet, porous plate (11) is arranged on the interior stripping of reactor and removes in the ammonia chamber (12), be positioned at position between charging opening (8) and the atomizing nozzle (2), micro-pore aeration plate (6) is positioned at bottom, reactor catalyzed oxidation pond (13), on the micro-pore aeration plate (6) of catalyzer (4) in catalyzed oxidation pond (13), pneumatic pump (5) outlet is communicated with inlet mouth (16) and aeration tube (14), aeration tube (14) extend into micro-pore aeration plate (6) bottom, water outlet (3) is positioned at the bottom of the upper spacer top inlet mouth (16) in catalyzed oxidation pond (13), mud discharging mouth (9) is positioned at reactor near the bottom, and ammonia escape orifice (7) is positioned at reactor head.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100797392A CN102219323B (en) | 2011-03-31 | 2011-03-31 | Method for simultaneously removing organic pollutants and ammonia in waste water and reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100797392A CN102219323B (en) | 2011-03-31 | 2011-03-31 | Method for simultaneously removing organic pollutants and ammonia in waste water and reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102219323A true CN102219323A (en) | 2011-10-19 |
| CN102219323B CN102219323B (en) | 2012-07-25 |
Family
ID=44776075
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011100797392A Expired - Fee Related CN102219323B (en) | 2011-03-31 | 2011-03-31 | Method for simultaneously removing organic pollutants and ammonia in waste water and reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102219323B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102489495A (en) * | 2011-12-23 | 2012-06-13 | 王启庚 | Garbage treatment apparatus |
| CN102531209A (en) * | 2012-02-21 | 2012-07-04 | 哈尔滨工业大学 | Separation type tail gas circulation pressurization aeration device |
| CN103253725A (en) * | 2013-04-09 | 2013-08-21 | 北京建筑工程学院 | Method for removing organic matters in reclaimed water by using in situ FeOxHy |
| CN104229971A (en) * | 2014-08-26 | 2014-12-24 | 常州大学 | Device for treating high-concentration ammonia nitrogen in coal chemical industry wastewater by using surface activity catalyst |
| CN104740989A (en) * | 2015-04-13 | 2015-07-01 | 华东理工大学 | Method and device for vortex-Fenton demercuration of flue gas |
| CN106219728A (en) * | 2016-08-29 | 2016-12-14 | 浙江正洁环境科技有限公司 | The method that a kind of high efficiency dispersion atomization synergy ozone processes waste water |
| CN107758936A (en) * | 2017-12-08 | 2018-03-06 | 济南大学 | A kind of organic waste-water treating apparatus containing ammonia and processing method |
| CN110040839A (en) * | 2019-05-08 | 2019-07-23 | 赵佳妮 | Handle the composition and preparation method thereof of fruits and vegetables rubbish |
| CN110104725A (en) * | 2019-06-03 | 2019-08-09 | 上海力脉环保设备有限公司 | A kind of device and method of the useless Organic substance in water of ultraviolet catalytic ozone oxidation |
| CN110713292A (en) * | 2019-11-07 | 2020-01-21 | 湖南海利常德农药化工有限公司 | Continuous pretreatment system and process for pirimiphos-methyl wastewater |
| CN116282536A (en) * | 2023-02-24 | 2023-06-23 | 安徽瑞柏新材料有限公司 | Ethyl acetate production is with waste water circulation purifier who has self-cleaning function |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006069418A1 (en) * | 2004-12-30 | 2006-07-06 | Aid-Development Engineering Pty Limited | Method for ground water and wastewater treatment |
| CN101423283A (en) * | 2008-11-18 | 2009-05-06 | 项贤富 | High efficiency detoxifcation method and device of organic wastewater |
| CN101618921A (en) * | 2009-06-25 | 2010-01-06 | 山东国信水处理有限公司 | TDI wastewater advanced treatment method |
| CN101781036A (en) * | 2009-12-23 | 2010-07-21 | 新奥科技发展有限公司 | Equipment and method for treating nondegradable wastewater by utilizing catalytic oxidation of ozone |
-
2011
- 2011-03-31 CN CN2011100797392A patent/CN102219323B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006069418A1 (en) * | 2004-12-30 | 2006-07-06 | Aid-Development Engineering Pty Limited | Method for ground water and wastewater treatment |
| CN101423283A (en) * | 2008-11-18 | 2009-05-06 | 项贤富 | High efficiency detoxifcation method and device of organic wastewater |
| CN101618921A (en) * | 2009-06-25 | 2010-01-06 | 山东国信水处理有限公司 | TDI wastewater advanced treatment method |
| CN101781036A (en) * | 2009-12-23 | 2010-07-21 | 新奥科技发展有限公司 | Equipment and method for treating nondegradable wastewater by utilizing catalytic oxidation of ozone |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102489495A (en) * | 2011-12-23 | 2012-06-13 | 王启庚 | Garbage treatment apparatus |
| CN102531209A (en) * | 2012-02-21 | 2012-07-04 | 哈尔滨工业大学 | Separation type tail gas circulation pressurization aeration device |
| CN102531209B (en) * | 2012-02-21 | 2015-04-08 | 哈尔滨工业大学 | Separation type tail gas circulation pressurization aeration device |
| CN103253725A (en) * | 2013-04-09 | 2013-08-21 | 北京建筑工程学院 | Method for removing organic matters in reclaimed water by using in situ FeOxHy |
| CN104229971A (en) * | 2014-08-26 | 2014-12-24 | 常州大学 | Device for treating high-concentration ammonia nitrogen in coal chemical industry wastewater by using surface activity catalyst |
| CN104740989A (en) * | 2015-04-13 | 2015-07-01 | 华东理工大学 | Method and device for vortex-Fenton demercuration of flue gas |
| CN104740989B (en) * | 2015-04-13 | 2017-05-10 | 华东理工大学 | Method and device for vortex-Fenton demercuration of flue gas |
| CN106219728B (en) * | 2016-08-29 | 2019-07-16 | 浙江精安再生资源发展有限公司 | A kind of method of high efficiency dispersion atomization synergy ozone processing waste water |
| CN106219728A (en) * | 2016-08-29 | 2016-12-14 | 浙江正洁环境科技有限公司 | The method that a kind of high efficiency dispersion atomization synergy ozone processes waste water |
| CN107758936A (en) * | 2017-12-08 | 2018-03-06 | 济南大学 | A kind of organic waste-water treating apparatus containing ammonia and processing method |
| CN110040839A (en) * | 2019-05-08 | 2019-07-23 | 赵佳妮 | Handle the composition and preparation method thereof of fruits and vegetables rubbish |
| CN110040839B (en) * | 2019-05-08 | 2022-12-16 | 山东生态家园环保股份有限公司 | Composition for treating fruit and vegetable garbage and preparation method thereof |
| CN110104725A (en) * | 2019-06-03 | 2019-08-09 | 上海力脉环保设备有限公司 | A kind of device and method of the useless Organic substance in water of ultraviolet catalytic ozone oxidation |
| CN110713292A (en) * | 2019-11-07 | 2020-01-21 | 湖南海利常德农药化工有限公司 | Continuous pretreatment system and process for pirimiphos-methyl wastewater |
| CN116282536A (en) * | 2023-02-24 | 2023-06-23 | 安徽瑞柏新材料有限公司 | Ethyl acetate production is with waste water circulation purifier who has self-cleaning function |
| CN116282536B (en) * | 2023-02-24 | 2023-09-22 | 安徽瑞柏新材料有限公司 | Ethyl acetate production is with waste water circulation purifier who has self-cleaning function |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102219323B (en) | 2012-07-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102219323B (en) | Method for simultaneously removing organic pollutants and ammonia in waste water and reactor | |
| CN203568944U (en) | Coking wastewater reuse treatment system | |
| CN102161537A (en) | Deep purification method of coking wastewater based on advanced ozone oxidation | |
| CN101601998A (en) | A kind of Preparation of catalysts method that is used for treating high-concentration organic wastewater through catalytic oxidation | |
| CN102500391A (en) | Catalyst for non-biodegradable wastewater treatment and preparation method thereof | |
| CN103833166B (en) | A kind of methyldiethanolamine (MDEA) process for treating industrial waste water | |
| CN108434958A (en) | A kind of sludge workshop foul gas advanced treatment device and its treatment process | |
| CN102167435A (en) | Solid catalytic Fenton water treatment technique | |
| AU636505B2 (en) | Process for the removal of hydrogensulphide (h2s) from biogas | |
| CN103951107A (en) | Device and method for treating coking wastewater | |
| CN208389756U (en) | A kind of sludge workshop foul gas advanced treatment device | |
| CN111252884A (en) | Integrated catalytic membrane ozone gas distributor, preparation method and application | |
| CN108786433B (en) | Flue gas dust, waste liquid and waste gas co-treatment device and method | |
| CN204022601U (en) | The micro-electrolysis advanced oxidation of MEO reactor | |
| CN101428887B (en) | Treatment for nickel-ammonia wastewater with aeration-hydrolyzing process | |
| CN103706234B (en) | A kind of stench flue gas processing method and device | |
| CN106039972B (en) | A method of with phosphate ore pulp purified industrial tail gas | |
| CN111871182A (en) | Fenton combined biological filter system for treating organic waste gas | |
| CN112456729A (en) | System and method for treating alkali waste water | |
| CN102372378A (en) | Treatment method of waste water produced by adopting castor oil to prepare decanedioic acid | |
| CN206232465U (en) | A kind of device for catalyzing and oxidating ozone for being applied to organic wastewater with difficult degradation thereby treatment | |
| CN105541056B (en) | A kind of remove the processing method of stannum in PCB industrial wastewater | |
| CN101811769B (en) | Method for treating parachloronitrobenzene waste water through liquid-liquid two-phase fluidization and ozone oxidation | |
| CN212215092U (en) | Device for simultaneously removing hydrogen sulfide and ammonia waste gas | |
| CN212532677U (en) | Landfill leachate treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120725 Termination date: 20150331 |
|
| EXPY | Termination of patent right or utility model |