CN1792897A - Process for depth treating total nitrogen of urban sewage - Google Patents
Process for depth treating total nitrogen of urban sewage Download PDFInfo
- Publication number
- CN1792897A CN1792897A CN 200510110258 CN200510110258A CN1792897A CN 1792897 A CN1792897 A CN 1792897A CN 200510110258 CN200510110258 CN 200510110258 CN 200510110258 A CN200510110258 A CN 200510110258A CN 1792897 A CN1792897 A CN 1792897A
- Authority
- CN
- China
- Prior art keywords
- pond
- nitrogen
- total nitrogen
- denitrification
- reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
A process for removing ammonical nitrogen, nitrate and nitrite from the city sewage includes denitrifying and low-voltage electrochemical reaction.
Description
Technical field
The invention belongs to environmental technology field, be specifically related to a kind of total nitrogen of urban sewage deep treatment method.
Background technology
At the beginning of last century, invention along with biological process of wastewater treatment, the water pollution control technology obtains very big progress, arrived the seventies, the black smelly problem of western developed country water body is resolved basically, and the consequent is the body eutrophication problem that is caused by nitrogen and phosphorus pollution, and worldwide becomes increasingly conspicuous, in the water body in landlocked river and lake, nitrogen is the controlling factor of eutrophication.Since then, denitride technology becomes the research focus of international environmental technology field academia and the concern of engineering circle always, and invented multiple denitride technology, mainly be divided into physico-chemical process (as stripping, stripping, distillation, ion exchange method, reverse osmosis), chemical method (as chemical precipitation method, breakpoint chlorination) and bioremediation (as Microbial denitrogenation and algal culture etc.).
The most widely used method of municipal effluent denitrogenation is a Microbial denitrogenation at present, is promptly undertaken by " nitrated-denitrification " process.Nitrated is the process that ammonia nitrogen is changed continuously into nitrate nitrogen by the nitrobacteria of nourishing one's nature certainly under the condition of aerobic; Denitrification is by the facultative denitrifying bacterium of different oxygen, and transforming nitrate under anoxia condition is the process of nitrogen.Heterotrophic bacterium and denitrification heterotrophic bacterium from nitrifier of nourishing one's nature and degradation of organic substances are compared, and the generation cycle is long, competitive capacity a little less than, therefore nitrated need are low in organic carbon concentration, organic loading is low and the condition of aerobic under just can carry out.And containing pollutents such as organism, ammonia nitrogen in the sewage usually, this makes that removing organism, nitrated, denitrification is difficult in the reactor simultaneously, efficiently finishes.Therefore general bio-denitrifying sewage technology all at its water quality and participate in reaction several big class different microorganisms characteristics and design, its relative merits are respectively arranged, main method has aerobic/anoxic method (O/A) and anoxic/aerobic method (A/O).In the good biological treatment system of control, its water outlet can reach country-level (B) emission standard---total nitrogen 20mg/L, ammonia nitrogen 8mg/L (water temperature＞12 ℃) or 15mg/L (water temperature＜12 ℃).As only using biological treatment system, its water outlet generally can not reach country-level (A) emission standard---total nitrogen 15mg/L, ammonia nitrogen 5mg/L (water temperature＞12 ℃) or 8mg/L (water temperature＜12 ℃).Therefore, biological treatment is difficult to ammonia nitrogen and total nitrogen are reduced to low concentration, and is subjected to external environment (as temperature) influence big.And at some to total nitrogen and the demanding place of ammonia nitrogen, as water conservation district or Dian Chi, Yunnan and other places, emission standard can not satisfy the requirement of water body even water outlet reaches country-level (A).Usually behind biological denitrification process, need to carry out advanced treatment with other method.The main method of advanced treatment has at present:
(1) vaporizing extract process
Vaporizing extract process is by feed high-temperature steam in water, and under the effect of high-temperature steam, the ammonia nitrogen in the water enters in the high-temperature steam by analytic function, thereby obtains removing.Its advantage is that the water outlet ammonia nitrogen concentration can be very low, be lower than 0.1mg/L, but there are some following defectives in it: (1) energy consumption height needs a large amount of high-temperature steams to feed in the water; (2) cost of equipment height is because stripping apparatus and connecting tube need bear high temperature, high pressure; (3) can not remove total nitrogen effectively.The total nitrogen of leading portion in the biological denitrificaion treat effluent is generally ammonia nitrogen and nitrate nitrogen, and vaporizing extract process only can be removed ammonia nitrogen effectively and can not effectively remove nitrate nitrogen, and is so the water outlet total nitrogen after the stripping advanced treatment is subjected to the influence of nitrate nitrogen, still higher; (4) water outlet after the stripping advanced treatment, its pH value and temperature are all high, need the pH value is transferred to neutral range and is cooled to envrionment temperature.
(2) distillation method
Distillation method is by water being heated to boiling, when pH is 11 left and right sides ammonia nitrogen is gone out from water distillation, enter gas phase, thereby obtains removing.Its merits and demerits is similar to vaporizing extract process, and the water outlet ammonia nitrogen concentration can be very low, is lower than 0.1mg/L, but: (1) energy consumption height, need heat water to boiling, and the general water yield of municipal effluent is very big, a large amount of water like this is heated to boiling, required energy consumption is very high; (2) cost of equipment height is because distillation plant and connecting tube need bear high temperature; (3) can not remove total nitrogen effectively.The total nitrogen of leading portion in the biological denitrificaion treat effluent is generally ammonia nitrogen and nitrate nitrogen, and distillation method also only can be removed ammonia nitrogen effectively and can not effectively remove nitrate nitrogen, and be so the water outlet total nitrogen after the distillation advanced treatment is subjected to the influence of nitrate nitrogen, still higher; (4) water outlet after the distillation advanced treatment, its pH value and temperature are all high, need the pH value is transferred to neutral range and is cooled to envrionment temperature.
(3) chemical precipitation method
Chemical precipitation method is to add magnesium salts and phosphoric acid salt and ammonium reaction to generate the ammonium magnesium phosphate precipitation in sewage, thereby removes the ammonia nitrogen in the water.Research and engineering practice show, there is the following defective in this method: (1) must add excessive magnesium salts and phosphoric acid salt for ammonia nitrogen removal is thorough, and excessive phosphoric acid salt must further be handled again, otherwise can form secondary pollution, therefore increase cost of equipment and working cost; (2) the ammonium magnesium phosphate precipitation flco that forms is less, can not effectively separate with water, must connect sand filter to remove small ammonium magnesium phosphate flco behind settling tank, and this has also increased cost of equipment and working cost, has also increased floor space.(3) ammonia nitrogen can be effectively removed, total nitrogen can not be removed effectively.
(4) ion exchange method
Rely on ion exchange resin, with NH
4 +, NO
3 -, NO
2 -Adsorb respectively, exchange on Zeo-karb and anionite-exchange resin, thus ammonia nitrogen and total nitrogen in the removal water.This method is comparatively easy, but research and engineering practice show that there are some following defectives in it: (1) unmatchful NH
4 +Carry out the resin of special efficacy absorption.Whether ion is adsorbed on easily on the resin and other ion-exchange is got off to depend primarily on ionic electricity price number and ionic radius.NH
4 +The electricity price number low, only be+1, and its ionic radius is only than Na
+, Li
+Greatly, less than Fe common in the water
2+, Ca
2+, Mg
2+, Cu
2+Deng, common ion exchange resin could be removed NH after need removing other ion
4 +, efficient is too low, and is easily exchanged to get off to enter in the water by other ion again, existing unmatchful NH
4 +Carry out the resin of special efficacy absorption.Natural material such as clinoptilolite, mordenite, vermiculite, wilkinite etc. are only arranged to NH
4 +Stronger selective adsorption is arranged, and adsorbable efficient is still lower.And these natural materials contain other impurity, are removing NH
4 +The time, other index such as COD value again may be not up to standard.(2) absorption exchanger regeneration trouble, operational difficulty.
Summary of the invention
The objective of the invention is to propose a kind of simple to operate, total nitrogen of urban sewage deep treatment method flexibly.
The total nitrogen of urban sewage deep treatment method that the present invention proposes, be after adopting common biological denitrification apparatus to carry out denitrogenation processing to municipal effluent, further carry out electrochemical treatment with the low voltage electric field electrochemical reactor, the current density of control electrochemical reactor is 30-50A/m
2Hydraulic detention time is 1-4 hour.Through further electrochemical treatment, can remove residual total nitrogen (comprising ammonia nitrogen, nitrate nitrogen, nitrite nitrogen) effectively, its water outlet total nitrogen is reduced to below the 0.5mg/L, satisfy needs to the very high occasion of total nitrogen standard-required.
Description of drawings
Fig. 1 is device of the present invention and flow process diagram.
Number in the figure: 1 is the anoxic denitrification pond, and 2 is the aerobic nitrification pond, and 3 is second pond, and 4 is electrochemical reactor.
Embodiment
The total nitrogen of urban sewage deep treatment method that the present invention proposes, its flow process is seen shown in Figure 1.Concrete steps are as follows:
1, municipal effluent is sent into anoxic denitrification pond 1 after the pre-treatment of grid, sand setting and necessity such as just heavy, mix under anoxia condition with returned sluge that comes from second pond 3 (reflux ratio is 0.5～1.5) and the backflow mixed liquor (reflux ratio 4-8) that comes from aerobic nitrification pond 2, under the effect of denitrification heterotrophic bacterium, with the water inlet in organism as carbon source and electron donor, come from nitrate radical in the macro-mixing liquid in aerobic nitrification pond or nitrite anions as electron acceptor(EA), carry out denitrification, nitrate radical or nitrite ion reduction becoming nitrogen are overflowed.The hydraulic detention time in anoxic denitrification pond 1 is 0.75～2.0 hour, and stirring intensity is: 100-200s
-1
2. the mixed solution in the anoxic denitrification pond 1 enters aerobic nitrification pond 2.Under the condition of aerobic, the heterotrophic bacterium of degradation of organic substances is degraded organism effectively, simultaneously organonitrogen is converted into ammonia nitrogen; From the nitrifier of nourishing one's nature at low COD and BOD, high NH
3Under the condition of-N concentration and aerobic, can effectively transform NH
3-N is to nitrate nitrogen (NO
3-N).This aerobic nitrification pond 2 can be selected for use in the following reactor a kind of according to practical situation: plug flow reactor, suspension fiber packed-bed reactor:
(1) plug flow reactor, controlling reaction time are 5-10 hour, dissolved oxygen (DO) in the solution 〉=1mg/L.
(2) suspension fiber packed column reactor, controlling reaction time are 3～7 hours, DO 〉=2mg/L in the solution, and the filler rate of adding is 20～60%, more excellent is 45%.
3. the mixed solution from aerobic nitrification tank 2 enters second pond 3, and precipitation is carried out mud-water separation, and sedimentation time is 2.0～2.5 hours.Precipitating sludge is partly refluxed to anoxic denitrification tank 1 (50～100%) as required, and the rest part precipitating sludge generally can discharge once as excess sludge discharge in one day.
4. the supernatant liquor of second pond 3 enters low voltage electric field electrochemical reactor 4, with electrochemical method ammonia nitrogen is oxidizing to be lower than 0.3mg/L, NO
3 --N and NO
2 --N is reduced to nitrogen, makes total nitrogen be lower than 0.5mg/L, satisfies water conservation district etc. to total nitrogen and the high demand of ammonia nitrogen particular requirement.The current density of low voltage electric field electrochemical reactor is 30～50A/m
2, hydraulic detention time is 1～4 hour.Electrochemical method can also rely on the strong further oxidation of organic compounds of OH of oxidisability of generation when effectively removing ammonia nitrogen and total nitrogen, reduce COD and BOD
5Value.
Town sewage is after the inventive method is handled; can make water outlet ammonia nitrogen＜0.3mg/l; total nitrogen＜0.5mg/L reaches water environment quality standard II class water water quality standard (GB3838-2002), satisfies the water quality requirement of country to first class of protection district, centralized Drinking Water surface water seedbed.
Table 1 for the present invention with the comparison of other typical total nitrogen and ammonia nitrogen advanced treatment process feature.Hence one can see that of the present inventionly has a remarkable advantages.
Table 1. the present invention and other typical total nitrogen and ammonia nitrogen advanced treatment process are relatively
| Feature | The present invention | Vaporizing extract process | Distillation method | Chemical precipitation method | Ion exchange method |
| Reaction tank volume (floor space) capital cost cost of equipment mud medicament expense energy consumption operating cost subsequent treatment expense is removed the ammonia nitrogen ability and is removed NO3 --N and NO 2 --N ability is removed the total nitrogen ability | Do not have greatly in during slight big nothing has | Little do not have in the greatly big-and-middle big nothing greatly | In greatly do not have in the greatly big-and-middle big nothing | Big size is much big-and-middle no little in little | In in big no big-and-middle in in greatly |
Embodiment 1
The somewhere municipal effluent enters the anoxic denitrification pond after grid, sand setting and just heavy pre-treatment, transfer under the part in anoxic with returned sluge that comes from second pond (reflux ratio 0.5) and the macro-mixing liquid (internal reflux ratio 4) that comes from the aerobic nitrification pond and to mix, the hydraulic detention time in anoxic denitrification pond is 1.0 hours, and stirring intensity is: 100s
-1Mixed solution in the anoxic denitrification pond enters aerobic nitrification pond (plug flow reactor), hydraulic detention time is 6 hours, DO is controlled to be 2～3mg/L, enter second pond from the effusive mixing liquid in aerobic nitrification pond, sedimentation time is 2.0 hours, supernatant liquor enters follow-up low voltage electric field electrochemical reactor, is 45 peace/m in current density
2, voltage is that oxidation was discharged after 1.0 hours under 5.2 volts the condition.
After testing, water inlet (following data are all in mean value, and intaking is the settling pit water outlet) mean value is NH
3-N 20mg/l, NO
3-N, NO
2-N is zero, TN-N 25mg/l, water outlet NH
3-N 0.1mg/l, NO
3-N, NO
2-N is zero, TN-N 0.2mg/l.
Embodiment 2
The somewhere municipal effluent enters the anoxic denitrification pond after grid, sand setting and just heavy pre-treatment, transfer under the part in anoxic with returned sluge that comes from second pond (reflux ratio 1.0) and the macro-mixing liquid (internal reflux ratio 5) that comes from the aerobic nitrification pond and to mix, the hydraulic detention time in anoxic denitrification pond is 1.5 hours, and stirring intensity is: 130s
-1Mixed solution in the anoxic denitrification pond enters aerobic nitrification pond (plug flow reactor), hydraulic detention time is 8 hours, DO is controlled to be 2～3mg/L, enter second pond from the effusive mixing liquid in aerobic nitrification pond, sedimentation time is 2.5 hours, supernatant liquor enters follow-up low voltage electric field electrochemical reactor, is 30 peace/m in current density
2, voltage is that oxidation was discharged after 2.5 hours under 5.7 volts the condition.
After testing, water inlet (following data are all in mean value, and intaking is the settling pit water outlet) mean value is NH
3-N 24mg/l, NO
3-N, NO
2-N is zero, TN-N 30mg/l, water outlet NH
3-N 0.15mg/l, NO
3-N, NO
2-N is zero, TN-N 0.25mg/l.
Embodiment 3
The somewhere municipal effluent enters the anoxic denitrification pond after grid, sand setting and just heavy pre-treatment, mix under anoxia condition with returned sluge that comes from second pond (reflux ratio 1.5) and the macro-mixing liquid (internal reflux ratio 6) that comes from the aerobic nitrification pond, the hydraulic detention time in anoxic denitrification pond is 2.0 hours, and stirring intensity is: 200s
-1Mixed solution in the anoxic denitrification pond enters aerobic nitrification pond (plug flow reactor), hydraulic detention time is 10 hours, DO is controlled to be 2～3mg/L, enter second pond from the effusive mixing liquid in aerobic nitrification pond, sedimentation time is 2.5 hours, supernatant liquor enters follow-up low voltage electric field electrochemical reactor, is 50 peace/m in current density
2, voltage is that oxidation was discharged after 2 hours under 5.7 volts the condition.
After testing, water inlet (following data are all in mean value, and intaking is the settling pit water outlet) mean value is NH
3-N 30mg/l, NO
3-N, NO
2-N is zero, TN-N 35mg/l, water outlet NH
3-N 0.2mg/l, NO
3-N, NO
2-N is zero, TN-N 0.4mg/l.
Claims (3)
1, a kind of total nitrogen of urban sewage deep treatment method, it is characterized in that after adopting common biological denitrification apparatus to carry out denitrogenation processing municipal effluent, further carry out electrochemical treatment with the low voltage electric field electrochemical reactor, the current density of control electrochemical reactor is 30-50A/m
2, hydraulic detention time is 1-4 hour.
2, total nitrogen of urban sewage deep treatment method according to claim 1 is characterized in that the step that described employing biological denitrification apparatus carries out biological denitrificaion is as follows:
(1) municipal effluent is sent into anoxic denitrification pond (1) after the pre-treatment of grid, sand setting and necessity such as just heavy, mix under anoxia condition with returned sluge that comes from second pond (3) and the backflow mixed liquor that comes from aerobic nitrification pond (2), under the effect of denitrification heterotrophic bacterium, with the water inlet in organism as carbon source and electron donor, come from nitrate radical in the macro-mixing liquid in aerobic nitrification pond or nitrite anions as electron acceptor(EA), carry out denitrification, nitrate radical or nitrite ion reduction becoming nitrogen are overflowed; The hydraulic detention time in anoxic denitrification pond (1) is 0.75～2.0 hour, and stirring intensity is: 100-200s
-1
(2) mixed solution in anoxic denitrification pond (1) enters aerobic nitrification pond (2), and under the condition of aerobic, heterotrophic bacterium is degraded organism effectively, simultaneously organonitrogen is converted into ammonia nitrogen; From the nitrifier of nourishing one's nature at low COD and BOD, high NH
3Under the condition of-N concentration and aerobic, effectively transform NH
3-N is to nitrate nitrogen;
(3) mixed solution of aerobic nitrification pond (2) enters second pond (3), and precipitation is carried out mud-water separation, and sedimentation time is 2.0～2.5 hours; Precipitating sludge is partly refluxed to anoxic denitrification pond (1) as required, and the rest part precipitating sludge is an excess sludge discharge;
(4) supernatant liquor of second pond (3) enters low voltage electric field electrochemical reactor (4) and carries out electrochemical treatment.
3, total nitrogen of urban sewage deep treatment method according to claim 2, it is characterized in that described aerobic nitrification pond (2) employing plug flow reactor or suspension fiber packed-bed reactor, when adopting plug flow reactor, controlling reaction time is 5-10 hour, dissolved oxygen 〉=1mg/L in the solution; When adopting the suspension fiber packed column reactor, controlling reaction time is 3～7 hours, dissolved oxygen 〉=2mg/L in the solution, and the filler rate of adding is 20-60%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101102588A CN100366552C (en) | 2005-11-10 | 2005-11-10 | Process for depth treating total nitrogen of urban sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101102588A CN100366552C (en) | 2005-11-10 | 2005-11-10 | Process for depth treating total nitrogen of urban sewage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1792897A true CN1792897A (en) | 2006-06-28 |
| CN100366552C CN100366552C (en) | 2008-02-06 |
Family
ID=36804571
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005101102588A Expired - Fee Related CN100366552C (en) | 2005-11-10 | 2005-11-10 | Process for depth treating total nitrogen of urban sewage |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100366552C (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102134148A (en) * | 2011-04-27 | 2011-07-27 | 安徽南风环境工程技术有限公司 | O/A/O process for treating high-concentration ammonia nitrogen wastewater |
| CN101746871B (en) * | 2008-12-08 | 2012-06-20 | 中国地质大学（北京） | Electrochemical method for removing nitrate from drinking water source |
| CN107915319A (en) * | 2017-12-21 | 2018-04-17 | 纤化（上海）生物化工股份有限公司 | The processing unit and method of a kind of nitrogenous effluent |
| CN108249551A (en) * | 2017-12-29 | 2018-07-06 | 海天水务集团股份公司 | A kind of processing method for removing sewage total nitrogen |
| CN108285205A (en) * | 2018-01-22 | 2018-07-17 | 中国水产科学研究院南海水产研究所 | A kind of nitration denitrification type biological flocculation cultural method |
| CN109292974A (en) * | 2018-12-10 | 2019-02-01 | 北京博诚立新环境科技股份有限公司 | A kind of underground water and water-bearing layer soil in-situ anaerobic organism restorative procedure |
| CN109704463A (en) * | 2019-02-26 | 2019-05-03 | 沧州市供水排水集团有限公司 | A kind of AAO process spent water treatment plant carbon source optimizing dosing system |
| CN115108690A (en) * | 2022-08-09 | 2022-09-27 | 北京交通大学 | Anaerobic ammonia oxidation treatment system for treating high ammonia nitrogen and high COD wastewater |
| CN115403145A (en) * | 2022-08-30 | 2022-11-29 | 上海师范大学 | VBBR (viable but basic biofilm reactor) -based urban sewage deep denitrification process taking nitrogen-containing organic wastewater as carbon source |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2338333Y (en) * | 1998-04-29 | 1999-09-15 | 广东威达医疗器械(集团)公司 | Equipment for scale-removing, scale-proof, sterilization and algae-killing for circulating water |
| CN2401539Y (en) * | 1999-11-29 | 2000-10-18 | 韩庆生 | Electronic water processing device |
| CN2438708Y (en) * | 2000-08-02 | 2001-07-11 | 揭西县中大新材料有限公司 | Circulating water antiscaling & removing scale sterilizing & aquatic plants-removing processor |
| CN2454365Y (en) * | 2000-11-20 | 2001-10-17 | 武文军 | Low-voltage electric-field type electronic water treatment apparatus |
| FI115904B (en) * | 2002-01-25 | 2005-08-15 | Bcde Group Waste Man Ltd Oy | Method and apparatus for removing contaminants from waste water by electroplating |
-
2005
- 2005-11-10 CN CNB2005101102588A patent/CN100366552C/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101746871B (en) * | 2008-12-08 | 2012-06-20 | 中国地质大学（北京） | Electrochemical method for removing nitrate from drinking water source |
| CN102134148A (en) * | 2011-04-27 | 2011-07-27 | 安徽南风环境工程技术有限公司 | O/A/O process for treating high-concentration ammonia nitrogen wastewater |
| CN107915319A (en) * | 2017-12-21 | 2018-04-17 | 纤化（上海）生物化工股份有限公司 | The processing unit and method of a kind of nitrogenous effluent |
| CN108249551A (en) * | 2017-12-29 | 2018-07-06 | 海天水务集团股份公司 | A kind of processing method for removing sewage total nitrogen |
| CN108285205A (en) * | 2018-01-22 | 2018-07-17 | 中国水产科学研究院南海水产研究所 | A kind of nitration denitrification type biological flocculation cultural method |
| CN109292974A (en) * | 2018-12-10 | 2019-02-01 | 北京博诚立新环境科技股份有限公司 | A kind of underground water and water-bearing layer soil in-situ anaerobic organism restorative procedure |
| CN109292974B (en) * | 2018-12-10 | 2022-03-29 | 北京博诚立新环境科技股份有限公司 | In-situ anaerobic biological remediation method for underground water and aquifer soil |
| CN109704463A (en) * | 2019-02-26 | 2019-05-03 | 沧州市供水排水集团有限公司 | A kind of AAO process spent water treatment plant carbon source optimizing dosing system |
| CN109704463B (en) * | 2019-02-26 | 2024-03-26 | 沧州市供水排水集团有限公司 | Carbon optimization feeding system of AAO process sewage treatment plant |
| CN115108690A (en) * | 2022-08-09 | 2022-09-27 | 北京交通大学 | Anaerobic ammonia oxidation treatment system for treating high ammonia nitrogen and high COD wastewater |
| CN115403145A (en) * | 2022-08-30 | 2022-11-29 | 上海师范大学 | VBBR (viable but basic biofilm reactor) -based urban sewage deep denitrification process taking nitrogen-containing organic wastewater as carbon source |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100366552C (en) | 2008-02-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100366552C (en) | Process for depth treating total nitrogen of urban sewage | |
| CN102718363B (en) | Coking wastewater comprehensive treatment method and system thereof | |
| CN106927628A (en) | Light electrolysis-Fenton-EGSB-A/O-BCO-BAF-coagulating treatment pharmacy waste water technique | |
| CN101434445A (en) | Processing system and operation method for phosphor-containing organic wastewater | |
| CN104176824B (en) | A kind of ammonium nitrate wastewater biochemical treatment apparatus and operation method | |
| CN108585350A (en) | A kind of town sewage treatment system up to standard to IV class water of surface water | |
| CN101423265A (en) | Ion-exchange denitrification and phosphorus removal advanced treatment method | |
| CN102527330A (en) | Preparation method of modified clinoptilolite ion exchanger | |
| CN101734826B (en) | Process method for treating coking wastewater | |
| CN101423314A (en) | High efficiency denitrification, phosphorus removal and phosphorus resource recovery composite for urban sewage | |
| CN110894125A (en) | Sewage treatment process for recycling N-methyl pyrrolidone | |
| CN110104873A (en) | Municipal wastewater advanced treatment apparatus and its method | |
| CN102491597B (en) | Method for treating high-concentration nitrogenous organic wastewater | |
| Aziz et al. | Municipal landfill leachate treatment techniques: an overview | |
| CN110342750A (en) | Sewage treatment device and process for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal | |
| CN210481144U (en) | Sewage treatment device for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal | |
| CN101891352A (en) | Ultrasonic-assisting nitrogen and phosphorus removing process | |
| CN109851160B (en) | Advanced sewage treatment method | |
| CN216614109U (en) | Device for relieving ion exchanger pollution | |
| JPH0698356B2 (en) | Organic wastewater treatment method | |
| CN103303995A (en) | Method for carrying out advanced treatment on waste water by utilizing diatomite | |
| CN104944678A (en) | Process for treating comprehensive high-concentration and high-salt refractory wastewater | |
| CN107226592A (en) | A kind of lead salt produces the handling process of waste water | |
| CN204779236U (en) | High-efficient low-cost processing system of coking wastewater | |
| CN1280210C (en) | Carbon source denitrogenation inside cells for sewage |
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 | ||
| ASS | Succession or assignment of patent right |
Owner name: SHANGHAI YANGCHEN INVESTMENT CO., LTD. Free format text: FORMER OWNER: FUDAN UNIVERSITY Effective date: 20091030 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20091030 Address after: 10C, 555 Xujiahui Road, Shanghai, China Patentee after: Shanghai Yong Sun Investement Co., Ltd. Address before: No. 220, Handan Road, Shanghai Patentee before: Fudan University |
|
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080206 Termination date: 20131110 |