CN104445840B - Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method - Google Patents

Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method Download PDF

Info

Publication number
CN104445840B
CN104445840B CN201410843687.5A CN201410843687A CN104445840B CN 104445840 B CN104445840 B CN 104445840B CN 201410843687 A CN201410843687 A CN 201410843687A CN 104445840 B CN104445840 B CN 104445840B
Authority
CN
China
Prior art keywords
pond
anoxic pond
anoxic
oxygen
aerobic
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
Application number
CN201410843687.5A
Other languages
Chinese (zh)
Other versions
CN104445840A (en
Inventor
杨敏
孙永利
郑兴灿
韦启信
范波
陈轶
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Public Works North China Design Studies Zong Yuan Co Ltd
Original Assignee
China Public Works North China Design Studies Zong Yuan Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by China Public Works North China Design Studies Zong Yuan Co Ltd filed Critical China Public Works North China Design Studies Zong Yuan Co Ltd
Priority to CN201410843687.5A priority Critical patent/CN104445840B/en
Publication of CN104445840A publication Critical patent/CN104445840A/en
Application granted granted Critical
Publication of CN104445840B publication Critical patent/CN104445840B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00Multistage treatment of water, waste water, or sewage
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/02Aerobic processes
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/30Aerobic and anaerobic processes
    • C02F3/302Nitrification and denitrification treatment

Abstract

The present invention relates to a kind of A based on carbon source efficiency utilization 2/ O-MBR multiple treating system and method, belong to technical field of sewage.Mainly comprise anaerobic pond, the first anoxic pond, Aerobic Pond, the oxygen pond that disappears, the second anoxic pond and membrane cisterna, wherein anaerobic pond is connected with the first anoxic pond, first anoxic pond is connected with Aerobic Pond, and Aerobic Pond is connected with the oxygen pond that disappears, the oxygen pond that disappears is connected with the second anoxic pond, the second anoxic pond is connected with membrane cisterna.The present invention is directed to the strengthened denitrification demand of maximum discharge standard urban wastewater treatment firm, by traditional A 2disappear oxygen pond and anoxic pond is set up in/O and MBR recombining process system, utilize disappear oxygen pond eliminate backflow nitrification liquid in dissolved oxygen to the disadvantageous effect of technique denitrogenation, and make full use of the endogenous denitrification effect of anoxic pond, realize efficiency utilization and the reinforcing process denitrogenation of carbon source.The present invention has the advantages such as utilization of carbon source efficiency is high, good denitrogenation and dephosphorization effect, effluent quality are good, capacity of resisting impact load is strong, effect of energy is remarkable.

Description

Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method
Technical field
The present invention relates to a kind of A based on carbon source efficiency utilization 2/ O-MBR multiple treating system and method, belong to technical field of sewage.
Background technology
Water-inlet carbon source deficiency is maximum discharge standard urban wastewater treatment firm stably reaching standard and energy-saving and cost-reducing key constraints.According to statistics, China urban wastewater treatment firm water inlet BOD in 2008 5/ TN average is only 3.49, the urban wastewater treatment firm water inlet BOD of 60% 5/ TN is lower than 4.
Along with the enforcement of one-level emission standard A (GB18918-2002), A 2the engineer applied of/O and MBR recombining process in China's maximum discharge standard urban wastewater treatment firm gets more and more, but most existing A 2the problem that carbon source is not efficiently utilized still is there is in/O and MBR recombining process in running, as carried the consumption of dissolved oxygen to anoxic pond carbon source in the nitrification liquid that refluxes, the effect of mud endogenous denitrification is not fully utilized, " carbon is dual-purpose " effect of Denitrifying Phosphorus Removal Technology is not fully utilized, and has a strong impact on low ratio of carbon to ammonium maximum discharge standard urban wastewater treatment firm stably reaching standard and saves energy and reduce the cost.
The oxygen pool technology that disappears solves backflow nitrification liquid to carry dissolved oxygen and enter the important technique measure that anoxic pond causes technique denitrification efficiency to decline, it is one of important channel of maximum discharge standard urban wastewater treatment firm carbon source efficiency utilization, the oxygen-consuming capacity of mud is mainly utilized to eliminate mixed solution dissolved oxygen, avoid backflow nitrification liquid to carry after dissolved oxygen enters anoxic pond and consumption is caused to water-inlet carbon source or additional carbon, and then realize efficiency utilization and the reinforcing process denitrogenation of carbon source.
Mud endogenous denitrification technology is the important measures of low ratio of carbon to ammonium maximum discharge urban wastewater treatment firm strengthened denitrification, is maximum discharge urban wastewater treatment firm stably reaching standard and energy-saving and cost-reducing important channel.Practice shows, under higher sludge concentration and longer hydraulic detention time, the strengthened denitrification ability of mud endogenous denitrification technology can reach 4-9mg/L.Due to A 2the sludge concentration of/O and MBR recombining process system is higher, can be mud endogenous denitrification technology at A 2utilization in/O and MBR recombining process system provides good condition.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, a kind of A based on carbon source efficiency utilization is provided 2/ O-MBR multiple treating system and method, by traditional A 2set up disappear oxygen pond and anoxic pond in/O and MBR multiple treating system, realize efficiency utilization and the reinforcing process denitrogenation of carbon source.
According to technical scheme provided by the invention, the described A based on carbon source efficiency utilization 2/ O-MBR multiple treating system, it is characterized in that: comprise set gradually anaerobic pond, the first anoxic pond, Aerobic Pond, the oxygen pond that disappears, the second anoxic pond and membrane cisterna, the water side of anaerobic pond connects the first anoxic pond, the water side of the first anoxic pond connects Aerobic Pond, the water side of Aerobic Pond connects the oxygen pond that disappears, the disappear water side in oxygen pond connects the second anoxic pond, and the water side of the second anoxic pond connects membrane cisterna; The backflow end of described first anoxic pond be connected the first internal reflux system between anaerobic pond, backflow end and the connection second internal reflux system between the first anoxic pond in the oxygen pond that disappears, the backflow end of membrane cisterna be connected the 3rd internal reflux system between Aerobic Pond,
Further, in described membrane cisterna, be provided with membrane module, membrane module adopts hollow fiber film assembly.
Further, underwater scooter or agitator are set respectively in described anaerobic pond, the first anoxic pond, the second anoxic pond and the oxygen pond that disappears.
Further, described Aerobic Pond adopts micro-pore aeration system, and membrane cisterna adopts perforated pipe aerating regulation system.
The described A based on carbon source efficiency utilization 2/ O-MBR compounding method, is characterized in that, concrete steps are as follows:
A, pretreated sewage enter anaerobic pond together with the mixed solution of the first anoxic pond through the first internal reflux system flowback, under anaerobism agitation condition, stop 1-1.5 hour, and MLSS value is 3-3.5g/L; Wherein the quantity of reflux of the first anoxic pond mixed solution is 1-2 times of pretreated wastewater influent flow;
The anaerobic pond mixed solution of b, step a gained enters the first anoxic pond together with the oxygen pond mixed solution that disappears through the second internal reflux system flowback, and under anoxia stirring condition, stop 3-4 hour, MLSS value is 4.5-6g/L; The oxygen pond mixed-liquor return amount that wherein disappears be wastewater influent flow 1-3 doubly;
First anoxic pond mixed solution of c, step b gained enters Aerobic Pond together with the membrane cisterna mixed solution through the 3rd internal reflux system flowback, under aerobic condition, stop 5-6 hour, and MLSS value is 6-9g/L, and the DO concentration of Aerobic Pond controls at 0.5-1mg/L simultaneously; Wherein membrane cisterna mixed-liquor return amount is 3-5 times of wastewater influent flow;
The Aerobic Pond mixed solution of d, step c gained enters by water side the oxygen pond that disappears, and stopping 30-60 minute, MLSS value is under agitation 6-9g/L;
The water outlet of the oxygen pond mixed solution that disappears of e, steps d gained enters the second anoxic pond by water side, and in the second anoxic pond, stop 4-5 hour under anoxia stirring condition, MLSS value is 6-9g/L;
Second anoxic pond mixed solution of f, step e gained enters membrane cisterna, under aerobic condition, stop 1-2 hour, and MLSS value is 7-11g/L, and the DO concentration of membrane cisterna controls at 5-6mg/L simultaneously;
The membrane cisterna mixed solution of g, step f gained is as water outlet after membrane module filters, and excess sludge drains into sludge treating system.
The present invention has the following advantages and positively effect: (1) the present invention will disappear fine-grained management technology and the existing A such as oxygen pool technology, mud endogenous denitrification technology, Denitrifying Phosphorus Removal Technology 2the organic integration of/O and MBR recombining process system, builds a kind of A based on carbon source efficiency utilization 2/ O and MBR recombining process system, has the advantages such as utilization of carbon source rate is high, good denitrogenation and dephosphorization effect, effect of energy are remarkable.(2) Aerobic Pond presses hypoxemia mode operation (Dissolved Oxygen concentration Control is at 0.5-1mg/L), not only be conducive to reducing the follow-up oxygen pond design hydraulic detention time that disappears, and can be short-cut nitrification and denitrification condition is provided, and then can further improve utilization of carbon source rate and energy conservation and consumption reduction effects.(3) property of the present invention is directed to and workable, can solve existing A 2the deficiency of/O and MBR recombining process system, the engineering design and the operational management that can be China's maximum discharge standard urban wastewater treatment firm provide new approaches, to the stably reaching standard of low ratio of carbon to ammonium, maximum discharge standard sewage treatment plant with energy-saving and cost-reducingly to have important practical significance.
Accompanying drawing explanation
Fig. 1 is A of the present invention 2the schematic diagram of/O-MBR multiple treating system.
Embodiment
Below in conjunction with concrete accompanying drawing, the invention will be further described.
As shown in Figure 1: the described A based on carbon source efficiency utilization 2/ O-MBR multiple treating system comprises anaerobic pond 1, first anoxic pond 2, Aerobic Pond 3, oxygen pond 4, second anoxic pond 5 that disappears, membrane cisterna 6, sewage 7, film water outlet 8, first internal reflux system 9, second internal reflux system 11, the 3rd internal reflux system 10, excess sludge 12 etc.
As shown in Figure 1, the present invention includes set gradually anaerobic pond 1, first anoxic pond 2, Aerobic Pond 3, disappear oxygen pond 4, second anoxic pond 5 and membrane cisterna 6, the water side of anaerobic pond 1 connects the first anoxic pond 2, the water side of the first anoxic pond 2 connects Aerobic Pond 3, the water side of Aerobic Pond 3 connects the oxygen pond 4 that disappears, the water side that the water side in oxygen pond 4 connects the second anoxic pond 5, second anoxic pond 5 that disappears connects membrane cisterna 6; The backflow end of described first anoxic pond 2 be connected the first internal reflux system 9 between anaerobic pond 1, disappear the backflow end in oxygen pond 4 and connection second internal reflux system 11 between the first anoxic pond 2, the backflow end of membrane cisterna 6 be connected the 3rd internal reflux system 10 between Aerobic Pond 3.
Modular membrane module is provided with in described membrane cisterna 6; Described membrane module adopts hollow fiber film assembly, and its magnitude setting should be determined according to Designing Sewage Treatment Plant scale and membrane flux, and the cleaning of membrane module adopts on-line cleaning mode and off-line cleaning way to combine.
The hydraulic flow state of described anaerobic pond 1, first anoxic pond 2 and Aerobic Pond 3 should design by cycling stream, and the hydraulic flow state of disappear oxygen pond and the second anoxic pond can be pulling flow type, completely mixed flow or cycling stream.
In described anaerobic pond 1, first anoxic pond 2, second anoxic pond 5 and the oxygen pond 4 that disappears, underwater scooter or agitator are set respectively.
Described Aerobic Pond 3 adopts micro-pore aeration system, and membrane cisterna 6 adopts perforated pipe aerating regulation system, the practicable independent control of two cover aerating systems, and membrane cisterna should adopt intermission aeration mode, to reduce membrane cisterna aeration energy consumption.
The useful volume in the described oxygen pond 4 that disappears should be determined according to the maximum reflux ratio of membrane cisterna mixed solution and the disappear maximum reflux ratio sum of oxygen pond mixed solution and sludge concentration etc.
Embodiment one: a kind of A based on carbon source efficiency utilization 2/ O and MBR compounding method, comprises the following steps:
A, pretreated sewage 7 enter anaerobic pond 1 together with the first anoxic pond 2 mixed solution refluxed through the first internal reflux system 9, stop 1.5 hours under anaerobism agitation condition, under microorganism (MLSS is 3g/L) effect, carry out anaerobic phosphorus release reaction; Wherein the quantity of reflux of the first anoxic pond mixed solution is 2 times of sewage 7 flooding velocity;
Anaerobic pond 1 mixed solution of b, step a gained enters the first anoxic pond 2 together with oxygen pond 4 mixed solution that disappears refluxed through the second internal reflux system 11, stop 4 hours under anoxia stirring condition, under microorganism (MLSS is 4.5g/L) effect, carry out anti-nitration reaction and denitrification dephosphorization reaction; The oxygen pond mixed-liquor return amount that wherein disappears is 3 times of sewage 7 flooding velocity;
C, step b gained first anoxic pond 2 mixed solution enter Aerobic Pond 3 together with membrane cisterna 6 mixed solution refluxed through the 3rd internal reflux system 10, stop 6 hours under aerobic condition, under microorganism (MLSS is 6g/L) effect, carry out the reaction of nitration reaction, aerobic suction phosphorus reaction and oxidation operation, the DO concentration of Aerobic Pond 3 controls at 1mg/L as far as possible simultaneously; Wherein membrane cisterna 6 mixed-liquor return amount is 5 times of sewage 7 flooding velocity;
D, step c gained Aerobic Pond 3 mixed solution enter the oxygen pond 4 that disappears, and stop 60 minutes under agitation, under microorganism (MLSS is 6g/L) effect, carry out oxygen consumption effect;
The disappear water outlet in oxygen pond 4 of e, steps d gained enters the second anoxic pond 5, stops 5 hours under anoxia stirring condition, carries out endogenous denitrification reaction and strengthened denitrification under microorganism (MLSS is 6g/L) effect;
The water outlet of f, step e gained second anoxic pond 5 enters membrane cisterna 6, stop 2 hours under aerobic condition, under microorganism (MLSS is 7g/L) effect, carry out the reaction of nitration reaction, aerobic suction phosphorus reaction and oxidation operation further, the DO concentration of membrane cisterna 6 controls at 5-6mg/L as far as possible simultaneously;
G, step f gained membrane cisterna 6 mixed solution discharge process system as water outlet by suction pump after membrane filtration, and excess sludge 12 drains into sludge treating system, remainder membrane cisterna mixed solution.
Embodiment two: a kind of A based on carbon source efficiency utilization 2/ O and MBR compounding method, comprises the following steps:
A, pretreated sewage 7 enter anaerobic pond 1 together with the first anoxic pond 2 mixed solution refluxed through the first internal reflux system 9, stop 1 hour under anaerobism agitation condition, under microorganism (MLSS is 3g/L) effect, carry out anaerobic phosphorus release reaction; Wherein the quantity of reflux of the first anoxic pond mixed solution is 1 times of sewage 7 flooding velocity;
Anaerobic pond 1 mixed solution of b, step a gained enters the first anoxic pond 2 together with oxygen pond 4 mixed solution that disappears refluxed through the second internal reflux system 11, stop 3 hours under anoxia stirring condition, under microorganism (MLSS is 6g/L) effect, carry out anti-nitration reaction and denitrification dephosphorization reaction; The oxygen pond mixed-liquor return amount that wherein disappears is 2 times of sewage 7 flooding velocity;
C, step b gained first anoxic pond 2 mixed solution enter Aerobic Pond 3 together with membrane cisterna 6 mixed solution refluxed through the 3rd internal reflux system 10, stop 6 hours under aerobic condition, under microorganism (MLSS is 9g/L) effect, carry out the reaction of nitration reaction, aerobic suction phosphorus reaction and oxidation operation, the DO concentration of Aerobic Pond 3 controls at 1mg/L as far as possible simultaneously; Wherein membrane cisterna 6 mixed-liquor return amount is 4 times of sewage 7 flooding velocity;
D, step c gained Aerobic Pond 3 mixed solution enter the oxygen pond 4 that disappears, and stop 30 minutes under agitation, under microorganism (MLSS is 9g/L) effect, carry out oxygen consumption effect;
The disappear water outlet in oxygen pond 4 of e, steps d gained enters the second anoxic pond 5, stops 5 hours under anoxia stirring condition, carries out endogenous denitrification reaction and strengthened denitrification under microorganism (MLSS is 9g/L) effect;
The water outlet of f, step e gained second anoxic pond 5 enters membrane cisterna 6, stop 2 hours under aerobic condition, under microorganism (MLSS is 11g/L) effect, carry out the reaction of nitration reaction, aerobic suction phosphorus reaction and oxidation operation further, the DO concentration of membrane cisterna 6 controls at 5-6mg/L as far as possible simultaneously;
G, step f gained membrane cisterna 6 mixed solution discharge process system as water outlet by suction pump after membrane filtration, and excess sludge 12 drains into sludge treating system, remainder membrane cisterna mixed solution.
Embodiment three: a kind of A based on carbon source efficiency utilization 2/ O and MBR compounding method, comprises the following steps:
A, pretreated sewage 7 enter anaerobic pond 1 together with the first anoxic pond 2 mixed solution refluxed through the first internal reflux system 9, stop 1.5 hours under anaerobism agitation condition, under microorganism (MLSS is 3g/L) effect, carry out anaerobic phosphorus release reaction; Wherein the quantity of reflux of the first anoxic pond mixed solution is 2 times of sewage 7 flooding velocity;
Anaerobic pond 1 mixed solution of b, step a gained enters the first anoxic pond 2 together with oxygen pond 4 mixed solution that disappears refluxed through the second internal reflux system 11, stop 4 hours under anoxia stirring condition, under microorganism (MLSS is 4.5g/L) effect, carry out anti-nitration reaction and denitrification dephosphorization reaction; The oxygen pond mixed-liquor return amount that wherein disappears is 2 times of sewage 7 flooding velocity;
C, step b gained first anoxic pond 2 mixed solution enter Aerobic Pond 3 together with membrane cisterna 6 mixed solution refluxed through the 3rd internal reflux system 10, stop 5 hours under aerobic condition, under microorganism (MLSS is 7g/L) effect, carry out the reaction of nitration reaction, aerobic suction phosphorus reaction and oxidation operation, the DO concentration of Aerobic Pond 3 controls at 1mg/L as far as possible simultaneously; Wherein membrane cisterna 6 mixed-liquor return amount is 3 times of sewage 7 flooding velocity;
D, step c gained Aerobic Pond 3 mixed solution enter the oxygen pond 4 that disappears, and stop 40 minutes under agitation, under microorganism (MLSS is 7g/L) effect, carry out oxygen consumption effect;
The disappear water outlet in oxygen pond 4 of e, steps d gained enters the second anoxic pond 5, stops 4 hours under anoxia stirring condition, carries out endogenous denitrification reaction and strengthened denitrification under microorganism (MLSS is 7g/L) effect;
The water outlet of f, step e gained second anoxic pond 5 enters membrane cisterna 6, stop 1 hour under aerobic condition, under microorganism (MLSS is 9g/L) effect, carry out the reaction of nitration reaction, aerobic suction phosphorus reaction and oxidation operation further, the DO concentration of membrane cisterna 6 controls at 5-6mg/L as far as possible simultaneously;
G, step f gained membrane cisterna 6 mixed solution discharge process system as water outlet by suction pump after membrane filtration, and excess sludge 12 drains into sludge treating system, remainder membrane cisterna mixed solution.

Claims (2)

1. the A of a carbon source efficiency utilization 2/ O-MBR multiple treating system, it is characterized in that: comprise set gradually anaerobic pond (1), the first anoxic pond (2), Aerobic Pond (3), the oxygen pond (4) that disappears, the second anoxic pond (5) and membrane cisterna (6), the water side of anaerobic pond (1) connects the first anoxic pond (2), the water side of the first anoxic pond (2) connects Aerobic Pond (3), the water side of Aerobic Pond (3) connects the oxygen pond (4) that disappears, the disappear water side in oxygen pond (4) connects the second anoxic pond (5), and the water side of the second anoxic pond (5) connects membrane cisterna (6); The backflow end of described first anoxic pond (2) be connected the first internal reflux system (9) between anaerobic pond (1), disappear oxygen pond (4) backflow end be connected the second internal reflux system (11) between the first anoxic pond (2), the backflow end of membrane cisterna (6) be connected the 3rd internal reflux system (10) between Aerobic Pond (3);
In described membrane cisterna (6), be provided with membrane module, membrane module adopts hollow fiber film assembly;
In described anaerobic pond (1), the first anoxic pond (2), the second anoxic pond (5) and the oxygen pond (4) that disappears, underwater scooter or agitator are set respectively;
Described Aerobic Pond (3) adopts micro-pore aeration system, and membrane cisterna (6) adopts perforated pipe aerating regulation system.
2. the A of a carbon source efficiency utilization 2/ O-MBR compounding method, is characterized in that, concrete steps are as follows:
A, pretreated sewage (7) enter anaerobic pond (1) together with the mixed solution of the first anoxic pond (2) refluxed through the first internal reflux system (9), and under anaerobism agitation condition, stop 1-1.5 hour, MLSS value is 3-3.5g/L; Wherein the quantity of reflux of the first anoxic pond (2) mixed solution is 1-2 times of pretreated sewage (7) flooding velocity;
Anaerobic pond (1) mixed solution of b, step a gained enters the first anoxic pond (2) together with oxygen pond (4) mixed solution that disappears refluxed through the second internal reflux system (11), and under anoxia stirring condition, stop 3-4 hour, MLSS value is 4.5-6g/L; Oxygen pond (4) the mixed-liquor return amount that wherein disappears be sewage (7) flooding velocity 1-3 doubly;
First anoxic pond (2) mixed solution of c, step b gained enters Aerobic Pond (3) together with membrane cisterna (6) mixed solution refluxed through the 3rd internal reflux system (10), 5-6 hour is stopped under aerobic condition, MLSS value is 6-9g/L, and the DO concentration of Aerobic Pond (3) controls at 0.5-1mg/L simultaneously; Wherein membrane cisterna (6) mixed-liquor return amount is 3-5 times of sewage (7) flooding velocity;
Aerobic Pond (3) mixed solution of d, step c gained enters by water side the oxygen pond (4) that disappears, and stopping 30-60 minute, MLSS value is under agitation 6-9g/L;
The water outlet of oxygen pond (4) mixed solution that disappears of e, steps d gained enters the second anoxic pond (5) by water side, and in the second anoxic pond (5), stop 4-5 hour under anoxia stirring condition, MLSS value is 6-9g/L;
Second anoxic pond (5) mixed solution of f, step e gained enters membrane cisterna (6), under aerobic condition, stop 1-2 hour, and MLSS value is 7-11g/L, and the DO concentration of membrane cisterna (6) controls at 5-6mg/L simultaneously;
Membrane cisterna (6) mixed solution of g, step f gained is as water outlet after membrane module filters, and excess sludge (12) drains into sludge treating system.
CN201410843687.5A 2014-12-30 2014-12-30 Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method Active CN104445840B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201410843687.5A CN104445840B (en) 2014-12-30 2014-12-30 Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201410843687.5A CN104445840B (en) 2014-12-30 2014-12-30 Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method

Publications (2)

Publication Number Publication Date
CN104445840A CN104445840A (en) 2015-03-25
CN104445840B true CN104445840B (en) 2016-03-02

Family

ID=52892698

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201410843687.5A Active CN104445840B (en) 2014-12-30 2014-12-30 Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method

Country Status (1)

Country Link
CN (1) CN104445840B (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105948248B (en) * 2016-06-01 2018-10-16 博天环境集团股份有限公司 A kind of biochemical reaction device
CN106882875A (en) * 2017-02-16 2017-06-23 洪胜男 With the system and method for nitrogen phosphorus in membrane technology removal sewage
CN108640420A (en) * 2018-05-09 2018-10-12 广东莞绿环保工程有限公司 A kind for the treatment of process of lithium battery waste liquid
CN112093899B (en) * 2020-07-30 2022-03-22 同济大学 Method and system for biological nitrogen and phosphorus removal of sewage

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003057632A1 (en) * 2002-01-07 2003-07-17 Berliner Wasser Betriebe Biological treatment process involving post-denitrification mechanism and a membrane filter
CN100395197C (en) * 2006-08-15 2008-06-18 北京工业大学 Improved UCT technology and device
CN102557342A (en) * 2011-12-28 2012-07-11 广州市市政工程设计研究院 Process and device for treating sewage through denitrification and dephosphorization by anaerobic-anoxic-oxic-anoxic (AAOA) plus membrane bioreactor (MBR) process
CN202881052U (en) * 2012-10-18 2013-04-17 中联环有限公司 Device for removing phosphorus chemically and forcibly by adopting A2O, membrane separation and cloth filter filtering

Also Published As

Publication number Publication date
CN104445840A (en) 2015-03-25

Similar Documents

Publication Publication Date Title
CN104058555B (en) Based on low ratio of carbon to ammonium municipal effluent denitrification system and the treatment process of Anammox
CN104445840B (en) Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system and method
CN109721156B (en) Device and method for treating late landfill leachate through integration of intermittent aeration/short-range denitrification-anaerobic ammonia oxidation
CN105461061A (en) A<2>/O-biology synchronous nitrogen and phosphorus removal device and method for urban sewage
CN110143725B (en) Device and method for treating urban sewage by using mixed sludge fermentation liquor as carbon source through continuous flow short-cut denitrification coupling anaerobic ammonia oxidation process
CN204058199U (en) A kind of A2/O+ MBR combined sewage water regenerating unit
CN100441524C (en) Constant water level sequencing batch active sludge process and system for treating sewage
CN102674537A (en) Reversed-order SBR (Sequencing Batch Reactor) water processing device and method for enhanced nitrogen removal
CN104030443A (en) Fine management-based municipal sewage enhanced phosphorus and nitrogen removal system and treatment process thereof
CN105858886A (en) Multistage anoxic and oxic coupling MBR sewage treatment technology for enhanced nitrogen and phosphorus removal
CN110759580A (en) Novel advanced sewage treatment process based on enhanced nitrogen and phosphorus removal
CN105293834A (en) Integrated iods reactor
CN201598224U (en) Biological nitrogen and phosphorus removal treatment and filter integrated sewage treatment system
CN101746931A (en) Denitrification dephosphorization biological treatment and filtration integral sewage treatment system and method thereof
CN203999266U (en) Low ratio of carbon to ammonium municipal effluent denitrification system based on Anammox
CN209740813U (en) Anaerobic-aerobic internal circulation sludge in-situ reduction system based on A2/O process
CN204714595U (en) For improveing the integrated sewage disposal pond of AO
CN203794754U (en) Energy-saving type inverted AAO-MBR sewage treatment device
CN204588936U (en) A kind of waste disposal plant of denitrogenation dephosphorizing
CN204356204U (en) Based on the A of carbon source efficiency utilization 2/ O-MBR multiple treating system
CN204251415U (en) Arrange internal reflux mixed solution to disappear the strengthened denitrification system in oxygen pond
CN103936231B (en) A kind of energy-saving inversion A AO-MBR sewage water treatment method
CN202643508U (en) Multistage A-O intensified denitrification dephosphorization constant water level sequencing batch activated sludge treatment sewage system
CN104787991A (en) Composite CAS (conventional activated sludge process)-MBR (membrane bioreactor) sewage treatment system
CN107902759A (en) A kind of intermittent aerating processing method and processing system

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant