CN102190399A - Method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption - Google Patents
Method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption Download PDFInfo
- Publication number
- CN102190399A CN102190399A CN 201010124435 CN201010124435A CN102190399A CN 102190399 A CN102190399 A CN 102190399A CN 201010124435 CN201010124435 CN 201010124435 CN 201010124435 A CN201010124435 A CN 201010124435A CN 102190399 A CN102190399 A CN 102190399A
- Authority
- CN
- China
- Prior art keywords
- zeolite
- ammonia nitrogen
- regeneration
- reactor
- adsorption column
- 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.)
- Pending
Links
Landscapes
- Water Treatment By Sorption (AREA)
Abstract
The invention belongs to the technical field of environmental protection, and relates to a method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption. The method comprises the following steps of: contacting pretreated town sewage with high-activity anaerobic sludge in a reactor, degrading organic pollutants in the sewage into final products such as CH4, CO2, H2O and the like by using various microbes in the anaerobic sludge, and performing electrochemical regeneration. By the method, the zeolite regeneration time is short; moreover, the ammonia nitrogen is oxidized into nitrogen and other substances in the electrochemical process, so the difficulty in treating used regenerated liquid is overcome to realize ammonia-nitrogen-free emission. Compared with bio-regeneration method and the like, the method has the advantages of small occupied area, simple operation and larger development space, and can fulfill the aims of recycling energy and saving energy.
Description
Technical field
The invention belongs to environmental technology field, the method that relates to the zeolite behind a kind of electrochemical regeneration anaerobic biological-absorption ammonia nitrogen is specifically related to utilize the method for electrochemical regeneration to make the zeolite regeneration behind anaerobic biological-absorption ammonia nitrogen reach the purpose of the recycling energy, save energy.
Background technology
Town sewage is handled the normal method that adopts anaerobic biological treatment.Anaerobic biological treatment has following characteristics: (1) construction, operation and simple to operate, and the expense of capital construction and operation is low; (2) energy requirement is low, but save energy; (3) the treatment scale elastic range is big, makes dispersion treatment become possibility; (4) few, the good stability of the generation of excess sludge, dewatering is good, aftertreatment is easy etc., thereby be used widely aspect the high concentrated organic wastewater processing.The advantage of anaerobic biological treatment meets the requirement that town sewage is handled required new technology, but it remains in following weak point: except that the microorganism synthetic cell needs small amount of nitrogen, almost can not remove nitrogen in anaerobic process; And owing to contain protein usually in the town sewage, under the effect of anerobe, can be converted into ammonia nitrogen, so town sewage is through anaerobic treatment also rising to some extent of ammonia nitrogen concentration sometimes.Because general anaerobic treatment does not possess the function of removing ammonia nitrogen, can the water outlet ammonia nitrogen up to standard, is decided by influent ammonium concentration and protein content fully.In order to overcome above-mentioned defective, guarantee that ammonia nitrogen also can qualified discharge, research and utilization zeolite adsorption ammonia nitrogen in the waste water after biochemical treatment was once arranged, eliminating rate of absorption can reach 90%.But how the regenerated problem still has technical problem to adsorb zeolite after saturated.Regeneration at zeolite at present has following several method.
(1) chemical regeneration method: mainly be to utilize single solution or wherein both combinations such as NaCl, KCl, HCl or NaOH.In some cases, it is not best using sodium salt to cook the regenerator effect separately, and particularly repeatedly exchange repeatedly makes skeleton structure of zeolite suffer destruction to a certain degree, and regeneration effect obviously reduces.Its regenerative process generally through soaking or flushing through regenerated liquid after washing, the filtration, is cleaned with pure water then again, at last oven dry.Behind the chemical solution regeneration zeolite repeated regeneration to NH
4 +Exchange capacity of absorption influence little, but because coexistence positively charged ion such as Ca in the sewage
2+Can make the exchange capacity of zeolite be the non-reversibility reduction.There is research that clinoptilolite has been carried out NaCl, KCl, NaHCO
3, HCl, NaCl+NaOH regeneration research, find that the regenerated liquid regeneration effect of NaCl+NaOH is relatively good, its recovery time is respectively to use NaCl, KCl, NaHCO separately
3, HCl regeneration required time 33.9%, 42.9%, 37.9% and 35.0%.Mass ratio is that 3: 7 the regeneration effect of NaCl+NaOH mixed solution is best.This method produces the high salinity waste liquid that contains ammonia nitrogen, easily environment is caused secondary pollution.
(2) physical method regeneration: the zeolite behind the absorption ammonia nitrogen, can pass through calcination under 500 ℃-600 ℃ hot conditions, with the NH in the zeolite
4 +Change NH into
3Gas oppositely purges with rare gas element then and realizes regeneration.Have research once the porous matter zeolite granular drying behind the adsorb ammonia nitrification to be placed in the vertical furnace, calcining 20min removes the ammonia nitrogen that is adsorbed under 650 ℃, recovers its vesicular structure.This type of calcination method expense height, and can be to environment is caused secondary pollution.
(3) absorption-bio-regeneration method two-stage method: people such as Murphy proposed zeolite " bio-regeneration method " in 1978, he adds a certain amount of nitrobacteria in the solution of submergence zeolite, the effect of 28d when the changing effect of observing 15d is equivalent to not add bacterial classification, the zeolite behind the bio-regeneration can recover 80% ammonia nitrogen absorption capacity.The bio-regeneration method is with low cost, but regeneration rate is slow, efficient is low, as if so actual application value is little, the research of this respect once once stayed cool.Along with the complexity day by day of environmental problem, the bio-regeneration problem of zeolite is familiar with again, and obtains further investigation.Green and Lahav etc. have designed the ammonia nitrogen in biology-ion exchange process (biological-ion exchange process) removal secondary treatment yielding water, in a reactor, zeolite at first adsorbs the ammonia nitrogen of removing in the water, rely on the nitrifier of zeolite surface growth to remove the ammonia nitrogen of zeolite enrichment again, realize Zeolite-bio regeneration.They have also carried out " ion-exchange-bio-regeneration " technology (ion-exchange and biological regeneration) experimental study, divide absorption and the operation of two stages of bio-regeneration with the filter post of filling chabazite, obtain the ammonia nitrogen removal frank more than 95%, and point out that the biological nitration effect can constantly promote zeolite desorb ammonia nitrogen, thereby zeolite is regenerated gradually; After this they have reported that " ion exchange process of bio-regeneration " (bioregenerated ion-exchange process) can be to the ammonia nitrogen steady removal in actual secondary and the one-level treat effluent.But this method regeneration rate is slow, and floor space is big, the operational administrative trouble.And the activity of nitrifier is subjected to temperature effect consumingly, the low temperature aging rate variance, and denitrification needs additional carbon simultaneously, has also increased a part of expense.
(4) absorption-bio-regeneration method one-stage process: at present, there are some technologies on the basis of traditional A/O, A/A/O or SBR technology, to add zeolite powder and carry out the enhanced biological denitrogenation, adsorb saturated zeolite powder and utilize microorganism to regenerate, formed Zeolite strengthened biological denitrification process.These technologies can also realize the bio-regeneration of zeolite when denitrogenation.Wheat head sea etc. adds the result of study that zeolite carries out the enhanced biological denitrogenation and shows in the A/O pond, zeolite powder is accumulated the equilibrium concentration that reaches certain in biological tank, compare former technology at normal temperatures, zeolite powder can't be brought into play the advantage of the selective adsorption of ammonia nitrogen, but can guarantee that when low temperature ammonia nitrogen concentration is up to standard in the treat effluent.During normal temperature, aeration 6h, the concentration of ammonia nitrogen is less than 5mg/L; When low temperature, aeration 6h, ammonia nitrogen concentration is near 15mg/L.But this kind method zeolite powder can be difficult to recycling utilization along with excess sludge discharge, produces secondary pollution.The adsorptive power of zeolite is and water outlet ammonia nitrogen concentration balance, can not effectively utilize the adsorptive power of zeolite, and the zeolite consumption of removing the unit ammonia nitrogen is big.
At present, remove in studying for a long period of time of ammonia nitrogen and the application process at zeolite, the regeneration problem of zeolite is its key of applying, also is the focus of zeolite applied research.Chemistry and physics method of reproduction easily and fast, but the cost height and can produce a large amount of waste liquid and waste gas that need processing; Absorption-bio-regeneration method two-stage method, working cost is lower, but speed is slow, and floor space is big, and the operational administrative trouble, the easy temperature influence of efficient; Absorption-bio-regeneration method one-stage process, the zeolite consumption is big, is difficult to recycling utilization, produces secondary pollution.
Summary of the invention
The objective of the invention is to overcome the deficiencies in the prior art, propose the method for the zeolite behind a kind of electrochemical regeneration anaerobic biological-absorption ammonia nitrogen.It is simple, efficient that the inventive method is done, and with the method for the electrochemical regeneration zeolite regeneration after with anaerobic biological-absorption ammonia nitrogen, reaches the purpose of save energy.
The present invention is based on nearest discovering, zeolite can effectively adsorb the ammonia nitrogen in the anaerobic biological processed waste water, and clearance reaches 90%, can obviously reduce the concentration of ammonia nitrogen in the outer draining.But this method need expend a large amount of zeolites, if can not be effectively with zeolite regeneration, with the cost of lifting sewage work wastewater treatment.
The present invention adopts town sewage to contact with highly active anaerobic sludge in the reactor after pre-treatment, is CH by planting microorganism in the anaerobic sludge with the organic pollutant degradation in the sewage
4, CO
2, H
2Final products such as O carry out electrochemical regeneration again.
Among the present invention, adopt sewage through pretreatment unit, comprise power supply, electrochemical reactor, adsorption column, peristaltic pump and connecting tube thereof, described electrochemical reactor, water tank, peristaltic pump, adsorption column are connected successively and are formed the loop, the recirculated water of electrochemical reactor, the may command flow velocity.The pipeline of water tank is connected with the lower end of adsorption column through peristaltic pump, and the upper end outlet pipe of adsorption column is connected with the lower end of electrochemical reactor.The upper end outlet conduit of electrochemical reactor is connected with water tank.Thus, the flow direction of recirculated water is: water tank → peristaltic pump → adsorption column → electrochemical reactor → water tank.
Adsorption column of the present invention adopts demountable structure, conveniently packs into and pours out zeolite.
The electrode anode of described electrochemical reactor is surface-coated IrO
2IrO
2/ Ti electrode, negative electrode are stainless steel.
The cell current of described electrochemical reactor is 0～2A, and bath voltage is 0～10V.
Regenerating unit of the present invention can also comprise the parts that other are conventional, as plays the parts that show pressure and current, deceleration, quicken, prevent function such as water conservancy diversion.
Among the present invention, can be according to the requirement of experiment design of zeolite adsorption impurity and reclaim equiment, so that zeolite is directly regenerated in adsorption column, need not container is put in the zeolite taking-up in addition, human and material resources have been saved, adsorption column directly can be taken off and is connected in the adsorption unit after regeneration finishes, process is very simple.
Regenerating unit of the present invention can also comprise the parts that other are conventional, as plays the parts that show pressure and current, deceleration, quicken, prevent function such as water conservancy diversion.
Particularly, the method for the zeolite behind a kind of electrochemical regeneration anaerobic biological provided by the invention-absorption ammonia nitrogen is characterized in that it comprises step:
(1) town sewage is entered whirlwind-type EGSB reactor by water distributor after the pre-treatment of necessity such as grid, sand setting, contact with highly active anaerobic sludge in the reactor from bottom to top, described anaerobic sludge is made up of multiple Institute of Micro-biology such as zymogenic bacteria, product hydrogen acetogen, methanogen, sulfatereducting bacterias, is CH by the microorganism in the anaerobic sludge with the organic pollutant degradation in the town sewage
4, CO
2, H
2Final products such as O;
Among the present invention, anaerobic reactor hydraulic detention time 2～12 hours all can, optimal water power standing time is 3 hours.
(2) supernatant that goes out stream from waste disposal plant middle and upper part gas, liquid, solid triphase separator is back to reactor bottom with 1: 1 ratio, to increase upflow velocity and stirring, improves rate of mass transfer, thereby improves the removal efficient of reactor.
(3) water outlet after above-mentioned triphase separator will be handled effectively separates with the gas and the anaerobic sludge of generation.
(4) design adsorption column as required, amount of zeolite and flooding velocity in the adsorption column are all decided according to physical condition, and waste water is pumped in the adsorption column, go out on advancing under water intake mode adopts.Take suitable flow velocity, the ammonia nitrogen in the waste water fully contacts with zeolite, and ammonia nitrogen farthest is adsorbed to above the zeolite.
(5) after reaching 90% penetrate, the zeolite in the adsorption column promptly carries out electrochemical regeneration,
The condition of electrochemical regeneration is as follows:
The experiment cycling use of water: chlorine ion concentration is the NaCl solution of 300mg/L, 2.0286g sodium sulfate; Getter device: adopted for two steps, the first step adopts the boric acid 50mL of 1mol/L, and the sodium hydroxide 50mL that second step was adopted 1mol/L carries out respectively waste gas is absorbed; Recovery time is 3h.
The present invention compares with general ion exchange method regeneration, adopt electrochemical regeneration to last shorter, general adopt NaCl to make regenerated liquid need to last about 15h with the ammonia nitrogen solution of isoconcentration, and adopt NaCl+NaOH (weight ratio is 3: 7) also to need 3.5h for regenerated liquid, and this electrochemical regeneration only needs 3h, and because electrochemical process is oxidized to ammonia nitrogen forms such as nitrogen, solved the difficulty that used regenerated liquid is handled, realized no ammonia nitrogen discharging.In addition, electrochemical regeneration takes up an area of little with respect to methods such as bio-regenerations, and operation is simple, has bigger development space.
Table 1 is that the present invention and chemical method, biological process regenerated compare.
Table 1
| ? | The present invention | Chemical method regeneration | Biological process regeneration |
| Floor space | 20％～50％ | 50％ | Standard |
| Energy consumption | Little | Greatly | Little |
| Running cost | Low | High | Low |
| Operating Complexity | Simply | Complicated | Complicated |
| Recovery time | 3h | 3.5h～15h | Very long |
| Regeneration effect | Good | Better | Better |
| The regenerated liquid problem | Do not have | Need to handle | Do not have |
The present invention is the efficient height not only, and simple to operate, reduce investment outlay.Compare favorable regeneration effect with other chemical method or biological process, the regeneration efficiency height, the recovery time is short; Compare with biological process, floor space is less, can save 20～50% soil; Compare with chemical method, can save energy consumption equally, and do not have regenerated liquid, need not the further processing of regenerated liquid.
For the ease of understanding, below will describe in detail the present invention by specific embodiment.It needs to be noted, specific examples only is in order to illustrate, obviously those of ordinary skill in the art can illustrate according to this paper, within the scope of the invention the present invention is made various corrections and change, and these corrections and change are also included in the scope of the present invention.
Embodiment
Embodiment 1
Come from the somewhere municipal effluent and after grid, sand setting pre-treatment, enter the EGSB reactor by water distributor, contact with highly active anaerobic sludge in the reactor from bottom to top, and anaerobic sludge is made up of multiple Institute of Micro-biology such as zymogenic bacteria, product hydrogen acetogen, methanogen, sulfatereducting bacterias, and they are CH with organic pollutant degradation in the town sewage
4, CO
2, H
2Final products such as O.Under the effect of sulfatereducting bacteria, the SO in the town sewage
4 2-Be H
2S, anaerobic reactor hydraulic detention time 3 hours.The supernatant that comes from the top triphase separator simultaneously is back to reactor bottom with 1: 1 ratio, to increase upflow velocity and stirring.In whole 1 year operational process, the ammonia nitrogen concentration that comes from the water outlet of EGSB reactor is substantially about 30mg/L, with peristaltic pump the water outlet of EGSB reactor is pumped in the adsorption column, after the zeolite in the adsorption column reaches 90% penetrate, carry out electrochemical regeneration: with sodium-chlor as cycling use of water, getter device adopts boric acid and sodium hydroxide, regenerates 3 hours.
Zeolite behind electrochemical regeneration is used for adsorbing the ammonia nitrogen in the water outlet of EGSB reactor, and the zeolite after experiment regeneration can reach 90% to the eliminating rate of absorption of ammonia nitrogen, and the concentration of ammonia nitrogen only is 3mg/L in the water outlet.
Embodiment 2
Come from the somewhere municipal effluent and after grid, sand setting pre-treatment, enter the UASB reactor by water distributor, contact with highly active anaerobic sludge in the reactor from bottom to top, and anaerobic sludge is made up of multiple Institute of Micro-biology such as zymogenic bacteria, product hydrogen acetogen, methanogen, sulfatereducting bacterias, and they are CH with organic pollutant degradation in the town sewage
4, CO
2, H
2Final products such as O.Under the effect of sulfatereducting bacteria, the SO in the town sewage
4 2-Be H
2S, anaerobic reactor hydraulic detention time 4 hours.The supernatant that comes from the top triphase separator simultaneously is back to reactor bottom with 1: 2 ratio, to increase upflow velocity and stirring.In whole 1 year operational process, in whole 1 year operational process, the ammonia nitrogen concentration that comes from the water outlet of EGSB reactor is substantially about 40mg/L, with peristaltic pump the water outlet of UASB reactor is pumped in the adsorption column, after the zeolite in the adsorption column reaches 90% penetrate, carry out electrochemical regeneration: with sodium-chlor as cycling use of water, getter device adopts boric acid and sodium hydroxide, regenerates 3 hours.
Zeolite behind electrochemical regeneration is used for adsorbing the ammonia nitrogen in the water outlet of UASB reactor, and the zeolite after experiment regeneration can reach 90% to the eliminating rate of absorption of ammonia nitrogen, and the concentration of ammonia nitrogen only is 3mg/L in the water outlet.
Embodiment 3
Come from the somewhere municipal effluent and after grid, sand setting pre-treatment, enter the EGSB reactor by water distributor, contact with highly active anaerobic sludge in the reactor from bottom to top, and anaerobic sludge is made up of multiple Institute of Micro-biology such as zymogenic bacteria, product hydrogen acetogen, methanogen, sulfatereducting bacterias, and they are CH with organic pollutant degradation in the town sewage
4, CO
2, H
2Final products such as O.Under the effect of sulfatereducting bacteria, the SO in the town sewage
4 2-Be H
2S, anaerobic reactor hydraulic detention time 6 hours.The supernatant that comes from the top triphase separator simultaneously is back to reactor bottom with 1: 1 ratio, to increase upflow velocity and stirring.The ammonia nitrogen concentration that comes from the water outlet of EGSB reactor is substantially about 30mg/L, with peristaltic pump the water outlet of EGSB reactor is pumped in the adsorption column, after the zeolite in the adsorption column reaches 90% penetrate, carry out electrochemical regeneration: with sodium-chlor as cycling use of water, getter device adopts boric acid and sodium hydroxide, regenerates 3 hours.
Zeolite behind electrochemical regeneration is used for adsorbing the ammonia nitrogen in the water outlet of EGSB reactor, and the zeolite after experiment regeneration can reach 90% to the eliminating rate of absorption of ammonia nitrogen, and the concentration of ammonia nitrogen only is 3mg/L in the water outlet.
Claims (5)
1. the method for the zeolite behind electrochemical regeneration anaerobic biological-absorption ammonia nitrogen is characterized in that it comprises step:
(1) with town sewage after grid or sand setting pre-treatment, enter whirlwind-type EGSB reactor by water distributor, contact with highly active anaerobic sludge in the reactor from bottom to top, the microorganism in the anaerobic sludge is CH with the organic pollutant degradation in the town sewage
4, CO
2Or H
2The O final product;
(2) supernatant that goes out stream from waste disposal plant middle and upper part gas, liquid, solid triphase separator is back to reactor bottom with 1: 1 ratio, and making increases upflow velocity and stirring, improves rate of mass transfer;
(3) water outlet after above-mentioned triphase separator will be handled effectively separates with the gas and the anaerobic sludge of generation;
(4) design adsorption column as required, amount of zeolite and flooding velocity in the adsorption column are decided according to physical condition, and waste water is pumped in the adsorption column, adopt the flow velocity that is fit to, ammonia nitrogen in the waste water is fully contacted with zeolite, make ammonia nitrogen farthest be adsorbed to above the zeolite;
(5) after reaching 90% penetrate, the zeolite in the adsorption column carries out electrochemical regeneration,
The condition of electrochemical regeneration is:
The experiment cycling use of water: chlorine ion concentration is the NaCl solution of 300mg/L, 2.0286g sodium sulfate; Getter device: adopted for two steps, the first step adopts the boric acid 50mL of 1mol/L, and the sodium hydroxide 50mL that second step was adopted 1mol/L carries out respectively waste gas is absorbed; Recovery time is 3h.
2. by the described method of claim 1, it is characterized in that described anaerobic sludge is made up of zymogenic bacteria, product hydrogen acetogen, methanogen and sulfatereducting bacteria.
3. by the described method of claim 1, it is characterized in that described anaerobic reactor hydraulic detention time is 2～12 hours.
4. by the described method of claim 3, it is characterized in that described anaerobic reactor hydraulic detention time is 3 hours.2～12 hours.
5. by the described method of claim 1, it is characterized in that described waste water pumps into water intake mode in the adsorption column and goes out on advancing under adopting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010124435 CN102190399A (en) | 2010-03-12 | 2010-03-12 | Method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010124435 CN102190399A (en) | 2010-03-12 | 2010-03-12 | Method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102190399A true CN102190399A (en) | 2011-09-21 |
Family
ID=44599391
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010124435 Pending CN102190399A (en) | 2010-03-12 | 2010-03-12 | Method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102190399A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106186567A (en) * | 2016-08-29 | 2016-12-07 | 杭州师范大学 | A kind of sewage-treatment plant simultaneously realizing biogas and recovery ammonia |
| CN108557941A (en) * | 2018-01-15 | 2018-09-21 | 北京城市排水集团有限责任公司 | A kind of the desorption and regeneration device in situ and its application method of ammonia nitrogen in waste water sorbing material |
| CN115502188A (en) * | 2022-10-19 | 2022-12-23 | 北京时代桃源环境科技股份有限公司 | Exogenous additive and application thereof in anaerobic digestion of kitchen waste |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1463253A (en) * | 2001-05-21 | 2003-12-24 | 三菱电机株式会社 | Process and appts. for treating nitrogen compound contg. water |
| CN1778712A (en) * | 2005-10-13 | 2006-05-31 | 复旦大学 | Urban sewage treatment of anaerobic biological-low voltage electric field oxidizing coupling system |
| JP2007098272A (en) * | 2005-10-04 | 2007-04-19 | Kobelco Eco-Solutions Co Ltd | Ammonia-containing water treatment method and apparatus |
-
2010
- 2010-03-12 CN CN 201010124435 patent/CN102190399A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1463253A (en) * | 2001-05-21 | 2003-12-24 | 三菱电机株式会社 | Process and appts. for treating nitrogen compound contg. water |
| JP2007098272A (en) * | 2005-10-04 | 2007-04-19 | Kobelco Eco-Solutions Co Ltd | Ammonia-containing water treatment method and apparatus |
| CN1778712A (en) * | 2005-10-13 | 2006-05-31 | 复旦大学 | Urban sewage treatment of anaerobic biological-low voltage electric field oxidizing coupling system |
Non-Patent Citations (1)
| Title |
|---|
| 《Journal of Hazardous Materials》 20090815 Yan Liu etal. Kinetic study of electrolytic ammonia removal using Ti/IrO2 as anode under different experimental conditions 第959-965页 1-5 第167卷, 第1-3期 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106186567A (en) * | 2016-08-29 | 2016-12-07 | 杭州师范大学 | A kind of sewage-treatment plant simultaneously realizing biogas and recovery ammonia |
| CN108557941A (en) * | 2018-01-15 | 2018-09-21 | 北京城市排水集团有限责任公司 | A kind of the desorption and regeneration device in situ and its application method of ammonia nitrogen in waste water sorbing material |
| CN115502188A (en) * | 2022-10-19 | 2022-12-23 | 北京时代桃源环境科技股份有限公司 | Exogenous additive and application thereof in anaerobic digestion of kitchen waste |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102078803A (en) | Regenerating unit for zeolite with ammonia-nitrogen saturation and application thereof | |
| CN102107977B (en) | Method for recycling wastewater containing high-concentration ammonia nitrogen | |
| CN1312063C (en) | Method for removing ammonia nitrogen from sewage in subzone | |
| CN105384302A (en) | Aquaculture wastewater processing system and method thereof | |
| CN105174621A (en) | System and method for treating wastewater by applying activated sludge | |
| CN112520838A (en) | Waste water and waste gas combined treatment system for efficient decarbonization and denitrification | |
| CN102188959A (en) | Regeneration method for saturated zeolite absorbing ammonia nitrogen in sewage | |
| CN101844075B (en) | Using method of electrochemical active carbon regeneration device | |
| CN102190399A (en) | Method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption | |
| CN201648186U (en) | Composite membrane bioreactor | |
| CN106904769B (en) | Method for integrated adsorption and desorption liquid application for removing total nitrogen pollutants in wastewater | |
| CN202808537U (en) | Town sewage deep treatment system | |
| CN202688153U (en) | Deep treatment device of municipal sewage | |
| CN209835752U (en) | Double-carrier anaerobic ammonia oxidation denitrification device | |
| CN112520949A (en) | Denitrification and energy self-integration system for high-carbon-nitrogen-ratio wastewater | |
| CN202022787U (en) | Minitype efficient composite type ammonia nitrogen removal equipment for domestic sewage | |
| CN112811710A (en) | Wastewater treatment device and process in xylitol processing | |
| CN115626751A (en) | A divide biological treatment device fast for sewage advanced treatment | |
| CN102205996A (en) | Chambered electrolysis wastewater device and application thereof | |
| KR100460225B1 (en) | Apparatus and method for purifying water through an electrical adsorption-desorption cycle using an activated carbon electrode with both positive and negative | |
| CN112551632B (en) | Functional filler for riverway phosphorus restoration, preparation method and use method | |
| CN211635954U (en) | Effluent water sump adds lid tail gas purification deodorizing device | |
| CN210150911U (en) | Artificial floating island type sewage purification device | |
| CN209940525U (en) | System for ammonia nitrogen in advanced treatment waste water | |
| CN204325003U (en) | A kind of ammonia nitrogen waste water 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 | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20110921 |