CN102701441B - Method for regulating and controlling nitrogen proportion of partial nitrosation effluent of low-ammonia-nitrogen continuous stirred-tank reactor (CSTR) at normal temperature - Google Patents
Method for regulating and controlling nitrogen proportion of partial nitrosation effluent of low-ammonia-nitrogen continuous stirred-tank reactor (CSTR) at normal temperature Download PDFInfo
- Publication number
- CN102701441B CN102701441B CN2012101527501A CN201210152750A CN102701441B CN 102701441 B CN102701441 B CN 102701441B CN 2012101527501 A CN2012101527501 A CN 2012101527501A CN 201210152750 A CN201210152750 A CN 201210152750A CN 102701441 B CN102701441 B CN 102701441B
- Authority
- CN
- China
- Prior art keywords
- ammonia nitrogen
- nitrogen
- cstr
- hrt
- control
- 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.)
- Active
Links
Images
Classifications
-
- Y02W10/12—
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Activated Sludge Processes (AREA)
Abstract
The invention provides a method for regulating and controlling nitrogen proportion of partial nitrosation effluent of low-ammonia-nitrogen continuous stirred-tank reactor (CSTR) at normal temperature and belongs to the field of municipal wastewater treatment and recycling. The starting is performed in a four-stage mode, and 80%-100% of ammoxidation load in the low-ammonia-nitrogen operation period of sequencing batch reactor activated sludge process (SBR) serves as initial ammoxidation load of the CSTR to confirm hydraulic retention time (HRT) of the CSTR. DO/ALR serves as an iconic parameter for maintaining a nitrosation system, and a value of the iconic parameter is recommended to be not greater than 1.0 mgO2/gNd and is regarded as the regulating and controlling standard of the DO and the HRT. First, the HRT is constant, the DO is controlled singly, if the proportion is not reached or the ammoxidation load is not enough, the DO and the HRT can be regulated and controlled synchronously. The NO2--N/NH4+-N and ammonia-nitrogen oxidation rate (a)/nitrite nitrogen generating rate (b) and nitrite nitrogen generating rate (b)/nitrate nitrogen generating rate (c) of the effluent are compared. If an average value of the proportions of the effluent under the different working conditions is in a range of 1-1.32:1, when b/a is greater than 0.9 and more approximates to 1.0, b/c is greater, and the working condition is more suitable for long-term operation of the system. The NO2--N/NH4+-N of the effluent of the CSTR is guaranteed to be in a range of 1-1.32:1 so as to meet the water feeding requirement of an anaerobic oxidation technology.
Description
Technical field
The invention belongs to municipal sewage treatment and resource utilization field.Be specifically related to the part nitrosification process stabilizing operation of Continuous Flow hybrid fully (CSTR) reactor for treatment low ammonia nitrogen waste water under the normal temperature condition and the method for the suitable water outlet proportion of control, make CSTR under the condition of higher nitrosification rate, obtain the water outlet that nitrite nitrogen/ammonia nitrogen is 1 ~ 1.32:1, to satisfy the water inlet demand of anaerobic ammonia oxidation process.
Background technology
The problem of controlling nitrate pollution in the dirty waste water is one of the important topic in present water pollution control field, and studies the hot issue that novel energy-saving and cost-reducing denitrogenation of waste water technology has become the water pollution control field.
Traditional is nitrated---and denitrification process is ripe and be most widely used a wastewater biological denitrificaion technology, but the problem of its existence also highlights day by day: the time that nitration reaction needs is long and dissolved oxygen content that consume is many; Denitrification process needs additional carbon, a little less than the capacity of resisting impact load, need carry out acid-base neutralisation etc.Part nitrosification---Anammox (Anammox) technology is only compared with the traditional biological denitrification process 50% ~ 60% NH
4 +-N is oxidizing to nitrite nitrogen (NO
2 --N), prevent nitrate nitrogen (NO
3 --N) generation in the Anammox reactor, need not additional carbon under anaerobic condition, directly be the NO of 1 ~ 1.32:1 with ratio
2 --N and NH
4 +-N is converted into N
2Discharge into the atmosphere, realize the removal of nitrogen.Advantages such as it is few that it has oxygen-consumption, need not additional carbon, and sludge yield is low and receive the favor and the concern of more and more researchers.
Part nitrosification technology is to realize the key point of Anammox autotrophic denitrification, is required to be the water inlet that Anammox provides nitrite nitrogen/ammonia nitrogen 1-1.32:1.But because the own characteristic of ammonia oxidation bacteria (AOB), normal temperature, low NH
4 +The desirable growing environment of-N waste water and AOB has big gap, so the more difficult stable maintenance of nitrite nitrogen accumulation effect under this envrionment conditions.Intermittent activated sludge process is mainly adopted in the research of nitrosification technology in recent years, and less for the research of complete hybrid Continuous Flow (CSTR) technology.Owing to do not have characteristics such as the interior no specific indication parameter of concentration gradient and reactor in the CSTR reactor, need to be resolved hurrily so how to keep nitrosification effect and this problem of control constant water outlet proportion of system.
Summary of the invention
The object of the present invention is to provide the method for CSTR part nitrosification process stabilizing under a kind of normal temperature condition, efficient operation, guarantee that based on the principle of dissolved oxygen (DO) or DO and the dual control of hydraulic detention time (HRT) CSTR obtains the water outlet that nitrite nitrogen/ammonia nitrogen is 1 ~ 1.32:1 under the condition of higher nitrosification rate.
Operation method provided by the present invention is under normal temperature condition, is research object with the low ammonia nitrogen concentration waste water of human configuration, mainly realizes efficient, the steady running of CSTR part nitrosation reaction device by the synchronization control of DO or HRT and DO.
Concrete steps are as follows:
Step 1: the CSTR reactor is built
Set gradually water tank, aeration tank and settling tank according to intaking to the order of water outlet.Sewage pumps into the aeration tank by intake pump from water tank, and the aeration tank water outlet is communicated to the settling tank pipe core through pipeline, by sludge reflux pump the mud in the settling tank is drawn back to the aeration tank.
Aeration rate is controlled by spinner-type flowmeter, in the complete hybrid reaction tank DO, pH and temp probe is set, and the parameter in the reaction tank is monitored.Water inlet and return flow meter are set, are convenient to the regulation and control of HRT.
Step 2: CSTR reactor start-up
CSTR starts employing quadravalence segmented mode and starts.Inoculation aeration tank, municipal sewage plant nitrifying sludge, the control sludge concentration is at 3000-4000mg/L, and temperature is at 17-25 ℃.
Fs, nitrated performance strain adopts the SBR mode to move, control influent ammonium concentration 100-120mg/L, pH is 7.70-8.00, DO is 2.0-3.0mg/L, the cycle of carrying out experiment, promptly every 30min water sampling are once measured ammonia nitrogen, nitrite and nitrate concentration.Ammonia nitrogen residue be less than influent ammonia nitrogen 10% before, stop aeration, determine the reaction times, the control sedimentation time is at 0.5-1h, draining, and determine the SBR cycle with this.Calculate the ammonia nitrogen oxidation load in the one-period, when ammonia nitrogen oxidation load (ALR) reaches 0.20kgN/kgMLSS/d when above, think that the mud nitrification activity is higher, the end of this stage enters next stage.
Subordinate phase the unloading phase of the high ammonia nitrogen nitrosification of SBR, adopts the SBR mode to move, control influent ammonium concentration 180.0 ~ 250.0mg/L, and pH is 7.70 ~ 8.00, DO is 0.50 ~ 0.90mg/L, suppresses the growth of NOB with high free ammonia (FA).Determine the SBR cycle by cycle experiment, the ammonia nitrogen residue be less than influent ammonia nitrogen 10% before stop aeration, prevent that the nitrite that will accumulate because of extended aeration is beneficial to NOB propagation by further oxidation.The control sedimentation time is at 0.5-1h.Reach more than 90% when continuous 7 cycles of reactor nitrosification rate (nitrite nitrogen of the nitrite nitrogen/generation of generation, nitrate nitrogen sum), think that the nitrosation reaction device starts successfully, enters next stage.
Phase III, SBR hangs down the ammonia nitrogen nitrosification laundering period, adopt the SBR mode to move, the control influent ammonium concentration is 70.0 ~ 90.0mg/L, pH is 7.60 ~ 7.90, and DO concentration is 0.30 ~ 0.50mg/L, determines the cycle by the cycle experiment, ammonia nitrogen residue be less than influent ammonia nitrogen 10% before stop aeration, sedimentation time 0.4-0.5h.When continuous 10 days nitrosification rates of reactor 90% when above, think that low ammonia nitrogen nitrosification starts successfully, enters next stage.
The quadravalence section, SBR changes the CSTR operation phase.Utilize the ammonia nitrogen oxidation load of SBR and CSTR mud constant, determine the CSTR controlled variable by the SBR controlled variable.Calculating low continuous 10 days of the ammonia nitrogen operating period nitrosification rate of SBR loads in 90% average ammonia nitrogen oxidation when above, the 80%-100% that adopts this value is as CSTR ammonia nitrogen oxidation load ALR, setting the ammonia nitrogen oxidation ratio is 50%-60%, determine the flooding velocity and the HRT of reactor, and initial HRT controls influent ammonium concentration 70.0 ~ 90.0mg/L at 3.0 ~ 9.0h, and pH is 7.60 ~ 7.90, DO is at 0.20 ~ 0.50mg/L in the reactor, and return sludge ratio is 10 ~ 30% of a flooding velocity.
Step 3: single control DO control CSTR water outlet nitrogen ratio strategy
Recommend its value to be not more than 1.0mgO with the significant parameter that DO/ALR maintains as the nitrosification system
2/ gNd regulates and control standard with this as DO and HRT.According to definite ALR of CSTR initial stage, and then definite DO higher limit, DO in codomain, adjusted, with regulation and control water outlet nitrite and ammonia nitrogen ratio.As water outlet NO
2 --N/NH
4 +-N value reduced DO concentration in the reactor, as water outlet NO greater than 1.32 o'clock
2 --N/NH
4 +-N value is less than 1 o'clock, and DO concentration is to till this ratio is in 1 ~ 1.32:1 scope in the augmenting response device.Each DO change is no more than 0.1mg/L, each 3d at least at interval that changes.When water outlet nitrogen ratio reaches 1 ~ 1.32:1, the ammonia nitrogen oxidation is loaded and was reached 0.20kgN/kg MLSS/d in average 7 days when above, think that CSTR part nitrosification nitrogen ratio regulates and control successfully, if DO reaches in limited time, ratio can not reach requirement, perhaps ratio reaches requirement but ammonia nitrogen oxidation load needs further to improve, and then needs synchronization modulation HRT and DO.
By measuring the water outlet nitrogen, though regulation and control DO has advantage of high precision, nitrogen is measured trouble, and does not have real-time operability.By studies show that, can be poor by Inlet and outlet water pH value is done, draw △ pH, utilize △ pH and water outlet nitrite and ammonia nitrogen ratio linear, infer water outlet proportion, and then can quicker, more directly perceived reactor controlled variable DO be adjusted.With x is △ pH, and y is water outlet NO
2 --N/NH
4 +-N ratio is set up the y=ax linear relationship, and a is 1.5 ~ 2.0.
Step 4: two control HRT and DO control CSTR water outlet nitrogen ratio strategy
Be not more than 1.0mg O with DO/ALR
2/ gN d is a standard, reduces HRT and can increase ALR, and the system DO upper limit improves, each HRT reduction amplitude is 0.5 ~ 1.0h, and each the adjustment is no less than 10d at interval, behind the change HRT, calculate the DO higher limit with DO/ALR, in codomain, adjust DO, with regulation and control water outlet nitrite and ammonia nitrogen ratio.Each DO change is no more than 0.1mg/L, each 3d at least at interval that changes.When water outlet nitrogen ratio reaches 1 ~ 1.32:1, the ammonia nitrogen oxidation is loaded and was reached 0.20kgN/kg MLSS/d in average 7 days when above, thinks that CSTR part nitrosification nitrogen ratio regulates and control successfully.
Water outlet NO under the more different HRT
2 --N/NH
4 +-N and ammonia nitrogen rate of oxidation (a)/nitrite nitrogen generating rate (b), nitrite nitrogen generating rate (b)/nitrate nitrogen generating rate (c).If the water outlet proportion average of different operating modes is all between 1 ~ 1.32:1, then when b/a＞0.9 and more near 1.0, and the big more person of b/c, then suitable more operating mode as system's long-time running.
Compare with the treatment process of existing wastewater biological denitrificaion, the present invention has following beneficial effect:
1) compare with traditional nitration denitrification technology, saved aeration rate, its water outlet feeds Anammox technology and need not to add carbon source, greatly reduces the cost of wastewater treatment and has shortened the reaction times, has reduced reactor volume.
2) reactor start-up adopts intermittent operation, constant aerating time, high substrate concn to the mode of hanging down the substrate concn transition, can realize the quick startup of nitrosation reaction device in a short time.
3) by the combined regulating of DO or HRT and DO, obtained stable water outlet proportion, made the realization of part nitrosification technology in continuous flow reactor become possibility.
4) propose the indication parameter of suitable judgement CSTR part nitrosification art breading effect, and provided the relational expression between the two.
Below in conjunction with embodiment the present invention is described further, but protection scope of the present invention is not limited thereto.
Description of drawings
Fig. 1 is complete hybrid Continuous Flow testing apparatus synoptic diagram, wherein 1. water tanks, 2.CSTR reactor, 3. second pond, 4. intake pump, 5. return sludge pump, 6. stirrer, 7. dissolved oxygen on-line determination instrument, 8. dissolved oxygen probe, 9.pH on-line determination instrument, 10.pH probe, 11. ultrasonic quiet adjustable air pumps, 12. aeration rings.
Fig. 2 is that the present invention adopts intermittent operation, constant aerating time, high substrate concn to start the design sketch of reactor to the mode of low substrate concn transition.
Fig. 3 is that the present invention is under constant HRT, by the design sketch of regulation and control DO acquisition stablizing water outlet proportion.
Fig. 4 is that the present invention adopts DO and HRT combined regulating, obtains to stablize the design sketch of water outlet proportion.
Fig. 5 is the match relation curve of CSTR reactor Inlet and outlet water pH difference and water outlet proportion.
Embodiment
Test is a basic water and to wherein adding partial raw water with the low ammonia nitrogen waste water of human configuration, and it is as follows to test concrete water quality: COD＜50mg/L, NH
4 +-N=60.8 ~ 85.0mg/L, NO
2 --N, NO
3 --N＜5.0mg/L, pH=7.70 ~ 8.20, TP＜1.0mg/L.Temperature is 17.0 ~ 23.0 ℃.
Concrete processing is as follows:
As shown in Figure 2, according to step 2, mud initial nitrification better performances, ammonia nitrogen oxidation load is 0.2kgN/kgMLSS/d.Directly enter subordinate phase, control initial ammonia nitrogen concentration at 187.0 ~ 238.0mg/L, pH is 7.80, and DO is 0.40mg/L in the reactor.Guarantee water outlet ammonia nitrogen concentration residue 70.0mg/L, determine that according to periodic test aeration time is 8h, 2 cycles of every day, reach more than 90% through 34 cycles nitrosification rate, then move 7 cycles, the nitrosification rate is all more than 90%, and the nitrosation reaction device starts successfully and enters the phase III.The control influent ammonium concentration is 71.7 ~ 84.6mg/L, determines that according to periodic test aeration time is 5h, moves for 2 cycles every day, operation 10d, and the nitrosification rate is all more than 90%, convertible operation scheme.
As shown in Figure 3, the ammonia nitrogen of low ammonia nitrogen operating period of SBR transforms load for 0.2kgN/kgMLSS/d, is foundation with this value, as water inlet NH
4 +When-N was 75.0mg/L, the amount of removing the part ammonia nitrogen was set at 38mg/L, V=30L, and initial HRT is 3.0h, DO concentration is 0.35mg/L.According to step 3, water outlet NO when DO was 0.35mg/L in the 1st, 2 day
2 --N/NH
4 +-N＜1.0 are so increased DO concentration to 0.45mg/L in the 3rd day, water outlet this moment NO
2 --N/NH
4 +-N is between 1 ~ 1.32:1.And when DO concentration was 0.39mg/L in the 9th day, water outlet proportion was 1.63＞1.32, so should reduce DO concentration.Under HRT=3.0h, move 34d, this stage water outlet NO
2 --N/NH
4 +The time of-N between 1 ~ 1.32:1 is longer than 7d, thinks water outlet NO
2 --N/NH
4 +-N regulates and control successfully, and definite water outlet NO
2 --N/NH
4 +-N between 1 ~ 1.32:1 the time DO/ALR of correspondence be 0.75mgO
2/ g N d＜1.0mgO
2/ g N d has guaranteed stage nitrosification rate average to be 96%.
Embodiment 3
As shown in Figure 4, for improving the ammonia nitrogen oxidation load of reactor, still control constant DO/ALR value and be 0.75mgO
2/ g N d, according to step 4, HRT reduces to 2.5h from the 3.0h in last stage.Take steps three DO density adjusting method is 1.04 in the 53rd ~ 62d water outlet proportion average, thinks that water outlet proportion is regulated and control successfully and should the stage ammonia nitrogen transform load to reach 0.27kgN/(kgMLSSd).Continue to improve the ammonia nitrogen oxidation load of reactor, HRT reduces to 1.5h, three the DO density adjusting method of still taking steps.The 88th ~ 98d water outlet proportion average is 1.18, thinks that water outlet proportion regulates and control successfully, and this stage ammonia nitrogen transforms load and reaches 0.54kgN/(kgMLSSd).
Average nitrite nitrogen rate of rise is respectively with the ratio b/c of the rate of rise of average nitrate nitrogen when HRT is 3.0h, 2.5h and 1.5h: 22.829,13.673 and 16.080, and average nitrite nitrogen rate of rise is respectively with the ratio b/a of average ammonia nitrogen rate of oxidation: 0.913,0.888 and 0.894.Average b/c during HRT=3.0h more approaches 1 at higher and b/a＞0.9, determines that therefore HRT=3.0h is preferably as the secular operation condition of nitrosification system.
Because the interior sludge concentration fluctuation of reactor is bigger during HRT=1.5h, influenced the mensuration of DO, so only the Inlet and outlet water pH value of preceding 70d is measured.The △ pH of reactor and the relation of water outlet proportion roughly satisfy following formula: establishing x is △ pH, and y is water outlet NO
2 --N/NH
4 +-N ratio is carried out match to the two, draws the relational expression of y=1.62467x.When △ pH was in 0.62 ~ 0.81 scope, water outlet proportion was between 1 ~ 1.32:1, if △ pH＜0.62 of observation should increase DO concentration under constant HRT; If △ pH＞0.81 of observation then should reduce DO concentration under constant HRT.
Claims (1)
1. a normal temperature hangs down ammonia nitrogen CSTR part nitrosification water outlet nitrogen ratio regulate and control method, it is characterized in that:
1) CSTR quadravalence section starts: inoculation aeration tank, municipal sewage plant nitrifying sludge, and sludge concentration is at 3000-4000mg/L; Fs, nitrated performance strain adopts the SBR mode to move, control influent ammonium concentration 100-120mg/L, pH is 7.70-8.00, DO is 2.0-3.0mg/L, the residue ammonia nitrogen be less than influent ammonia nitrogen 10% before, stop aeration, determine the reaction times, the control sedimentation time is at 0.5-1h, and draining reaches more than the 0.20kgN/kgMLSS/d up to ammonia nitrogen oxidation load; Subordinate phase the unloading phase of the high ammonia nitrogen nitrosification of SBR, adopts the SBR mode to move, control influent ammonium concentration 180.0～250.0mg/L, pH is 7.70～8.00, and DO is 0.50～0.90mg/L, ammonia nitrogen residue be less than influent ammonia nitrogen 10% before, stop aeration, the control sedimentation time is at 0.5-1h, and draining is up to reactor nitrosification rate, promptly the ratio of the nitrite nitrogen of nitrite nitrogen of Sheng Chenging and generation, nitrate nitrogen sum reached more than 90% in continuous 7 days; Phase III, SBR hangs down the ammonia nitrogen nitrosification laundering period, adopt the SBR mode to move, control influent ammonium concentration 70.0～90.0mg/L, pH is 7.60～7.90, DO is 0.30～0.50mg/L, ammonia nitrogen residue be less than influent ammonia nitrogen 10% before, stop aeration, sedimentation time 0.4-0.5h, draining, up to continuous 10 days nitrosification rates of reactor more than 90%; The quadravalence section, SBR changes the CSTR operation phase, calculating low continuous 10 days of the ammonia nitrogen operating period nitrosification rate of SBR loads in 90% average ammonia nitrogen oxidation when above, the 80%-100% that adopts this value is as CSTR ammonia nitrogen oxidation load ALR, setting the ammonia nitrogen oxidation ratio is 50%-60%, determine the flooding velocity and the HRT of reactor, and initial HRT is at 3.0～9.0h, control influent ammonium concentration 70.0～90.0mg/L, pH is 7.60～7.90, DO is at 0.20～0.50mg/L in the reactor, and return sludge ratio is 10～30% of a flooding velocity;
2) single control DO control CSTR water outlet nitrogen ratio strategy: be not more than 1.0mgO as its value of significant parameter that the nitrosification system maintains with DO/ALR
2/ gN d regulates and control standard with this as DO and HRT; According to definite ALR of CSTR initial stage, and then definite DO higher limit, DO in codomain, adjusted, with regulation and control water outlet nitrite and ammonia nitrogen ratio; Each DO change is no more than 0.1mg/L, each 3d at least at interval that changes; When water outlet nitrite and ammonia nitrogen ratio reach 1～1.32:1, the ammonia nitrogen oxidation is loaded and was reached 0.20kgN/kg MLSS/d in average 7 days when above, think that CSTR part nitrosification water outlet nitrogen ratio regulates and control successfully, if DO reaches in limited time, ratio can not reach requirement, perhaps ratio reaches requirement but ammonia nitrogen oxidation load needs further to improve, and then needs synchronization modulation HRT and DO;
3) two control HRT and DO control CSTR water outlet nitrogen ratio strategy: be not more than 1.0mgO with DO/ALR
2/ gN d is a standard, reduces HRT, can increase ALR, and the system DO upper limit improves, each HRT reduction amplitude is 0.5～1.0h, and each the adjustment is no less than 10d at interval, behind the change HRT, calculate the DO higher limit with DO/ALR, in codomain, adjust DO, with regulation and control water outlet nitrite and ammonia nitrogen ratio; Each DO change is no more than 0.1mg/L, each 3d at least at interval that changes; When water outlet nitrite and ammonia nitrogen ratio reach 1～1.32:1, the ammonia nitrogen oxidation is loaded and was reached 0.20kgN/kg MLSS/d in average 7 days when above, thinks that CSTR part nitrosification water outlet nitrogen ratio regulates and control successfully;
4) different HRT compare with DO combination nitrosification stability: the water outlet NO under the more different HRT
2 --N/NH
4 +-N and ammonia nitrogen rate of oxidation (a)/nitrite nitrogen generating rate (b), nitrite nitrogen generating rate (b)/nitrate nitrogen generating rate (c); If the average water outlet nitrite of different operating modes and ammonia nitrogen ratio be all between 1～1.32:1, then when b/a＞0.9 and more near 1.0, and the big more person of b/c, then suitable more operating mode as system's long-time running.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101527501A CN102701441B (en) | 2012-05-16 | 2012-05-16 | Method for regulating and controlling nitrogen proportion of partial nitrosation effluent of low-ammonia-nitrogen continuous stirred-tank reactor (CSTR) at normal temperature |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101527501A CN102701441B (en) | 2012-05-16 | 2012-05-16 | Method for regulating and controlling nitrogen proportion of partial nitrosation effluent of low-ammonia-nitrogen continuous stirred-tank reactor (CSTR) at normal temperature |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102701441A CN102701441A (en) | 2012-10-03 |
| CN102701441B true CN102701441B (en) | 2013-07-24 |
Family
ID=46894581
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012101527501A Active CN102701441B (en) | 2012-05-16 | 2012-05-16 | Method for regulating and controlling nitrogen proportion of partial nitrosation effluent of low-ammonia-nitrogen continuous stirred-tank reactor (CSTR) at normal temperature |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102701441B (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014043547A1 (en) | 2012-09-13 | 2014-03-20 | D.C. Water & Sewer & Authority | Method and apparatus for nitrogen removal in wastewater treatment |
| CN103058377A (en) * | 2013-01-08 | 2013-04-24 | 北京工业大学 | SBR nitrosation recovery method through utilizing intermittent aeration |
| SG11201507216RA (en) * | 2013-03-14 | 2015-10-29 | D C Water & Sewer Authority | Method and apparatus for maximizing nitrogen removal from wastewater |
| CN103408140B (en) * | 2013-08-14 | 2014-12-10 | 哈尔滨工业大学 | Control method realizing CANON process high-efficiency stable operation |
| CN107879469B (en) * | 2017-11-28 | 2020-05-15 | 苏州诺津环保科技有限公司 | Partial nitrosation starting and controlling method |
| CN110942343A (en) * | 2019-11-22 | 2020-03-31 | 马鞍山钢铁股份有限公司 | Proportioning obtaining method of coal blending |
| CN113772807B (en) * | 2021-10-20 | 2023-03-14 | 广西博世科环保科技股份有限公司 | Method for domesticating and operating ammonia oxidation biofilm reactor |
| CN115010259B (en) * | 2022-08-04 | 2022-10-21 | 江苏海峡环保科技发展有限公司 | Intelligent environment-friendly monitoring data processing method and system |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7332076B2 (en) * | 2004-12-15 | 2008-02-19 | Kouame Yao B | Water disinfection system using simultaneous multiple disinfectants |
| WO2006136173A2 (en) * | 2005-06-24 | 2006-12-28 | Danmarks Tekniske Universitet | Anaerobic microbial degradation of phthalic acid esters |
| CN101323486B (en) * | 2008-07-25 | 2010-12-01 | 贵州大学 | Method for realizing low carbon-nitrogen rate high concentration nitrogen-containing waste water steady biological hitrosation |
| US9422178B2 (en) * | 2009-06-16 | 2016-08-23 | University Of Massachusetts | Wastewater treatment system to reduce sludge generation |
| CN101973671B (en) * | 2010-10-15 | 2012-06-13 | 中国科学院生态环境研究中心 | Method for realizing SBR nitrosation-denitrosation at low temperature by optimally controlling aeration time |
-
2012
- 2012-05-16 CN CN2012101527501A patent/CN102701441B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN102701441A (en) | 2012-10-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102701441B (en) | Method for regulating and controlling nitrogen proportion of partial nitrosation effluent of low-ammonia-nitrogen continuous stirred-tank reactor (CSTR) at normal temperature | |
| CN108439595B (en) | Method for realizing partial shortcut nitrification-Anammox/denitrification of sewage by utilizing sludge fermentation product | |
| CN108545830B (en) | Process for enhancing partial shortcut nitrification anaerobic ammonia oxidation of continuous flow municipal sewage by utilizing sludge fermentation | |
| CN108217950B (en) | Device and method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage | |
| CN107162193B (en) | Device and method for treating domestic sewage by low-oxygen nitrification coupled with short-range denitrification anaerobic ammonia oxidation | |
| CN107265645B (en) | Device and method for treating low-carbon-source urban sewage by continuous-flow A/O dephosphorization series-connection multi-stage A/O autotrophic nitrogen removal process | |
| CN103482765B (en) | Quick starting method for technology for simultaneous denitrification and COD removal under condition of normal-temperature and low-C/N sewage | |
| CN104986856B (en) | Method for treating low-carbon-nitrogen-ratio domestic sewage with partial shortcut nitrification-synchronous sludge fermentation, denitrification and anaerobic ammonium oxidation process | |
| CN107162186B (en) | Device and method for urban sewage anaerobic ammonia oxidation autotrophic nitrogen removal based on granular sludge | |
| CN102101745B (en) | Control device and method for treating sludge digestion liquid through sludge-fermentation-coupled denitrification | |
| CN104291443B (en) | The apparatus and method of half nitrated/part denitrification/Anammox process low ratio of carbon to ammonium municipal effluent | |
| CN103922540B (en) | Application A pthe method of O/ bio-contact oxidation short distance nitration coupling Anammox autotrophic denitrification three device of sludge | |
| CN106946352B (en) | Device and method of integrated anaerobic ammonia oxidation autotrophic nitrogen removal biomembrane reactor | |
| CN109160606B (en) | Method for producing methane and efficiently and deeply denitrifying urban sewage | |
| CN102583745B (en) | Improved in-situ excess sludge decrement control method through cyclic activated sludge technology | |
| CN102786142A (en) | Device and method for partial nitrosation of low carbon municipal sewage | |
| CN113461145A (en) | Device and method for deep denitrification and synchronous sludge reduction of secondary effluent of sewage treatment plant | |
| CN109809560B (en) | Device and method for accurately feeding and controlling carbon source in multi-point water inlet multi-stage A/O process | |
| CN113666496A (en) | Method and device for realizing deep nitrogen and phosphorus removal of low-carbon-nitrogen-ratio domestic sewage by using segmented water inlet double-short-range anaerobic ammonia oxidation process | |
| CN113402021A (en) | Device and method for realizing sewage denitrification and sludge reduction by integrating in-situ sludge hydrolysis acidification and short-cut denitrification anaerobic ammonia oxidation | |
| CN104761056A (en) | Real-time control system and method for short-cut nitrification and coupled double-SBR denitrifying phosphorus removal | |
| CN102701438A (en) | Normal temperature low-ammonia-nitrogen nitrosation starting method | |
| CN108383239B (en) | Integrated biological treatment process for shortcut nitrification anaerobic ammonia oxidation and phosphorus removal under intermittent aeration mode | |
| US20230100166A1 (en) | Device and method for treating urban domestic sewage based on two-stage combined process of partial denitrification-anammox | |
| CN103539257B (en) | Membrane bioreactor domestic sewage treatment nitrosation quick start method |
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 |