CN104445840A - A2/O-MBR composite processing system and method based on efficient utilization of carbon source - Google Patents
A2/O-MBR composite processing system and method based on efficient utilization of carbon source Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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Abstract
The invention relates to an A2/O-MBR composite processing system and method based on efficient utilization of carbon source, and belongs to the technical field of sewage treatment. The A2/O-MBR composite processing system based on efficient utilization of carbon source mainly comprises an anaerobic tank, a first anoxic pond, an aerobic tank, an oxygen elimination tank, a second anoxic pond, and a membrane pool, wherein the anaerobic tank is connected with the first anoxic pond, the first anoxic pond is connected with the aerobic tank; the aerobic tank is connected with the oxygen elimination tank; the oxygen elimination tank is connected with the second anoxic pond; and the second anoxic pond is connected with the membrane pool. The A2/O-MBR composite processing system and method based on efficient utilization of carbon source are aimed for requirements of enhanced nitrogen removal of high discharge standard municipal sewage treatment plant; the efficient utilization of carbon source and the enhanced nitrogen removal are achieved by adding the oxygen elimination tank and the anoxic ponds in the conventional A2/O and MBR composite technology system, and using the oxygen elimination tank to remove the adverse effect of the dissolved oxygen to the technology denitrification in the backflow nitrified liquid, and completely using the inner source nitrification effect of the anoxic pond. The A2/O-MBR composite processing system and method based on efficient utilization of carbon source have the advantages that the utilization ratio of carbon source is high, the effect of denitrification and dephosphorization is good, the water quality of the discharged water is good, the ability to resist impact load is strong the effect of saving energy and reducing consumption is obvious, and the like.
Description
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 (5)
1. the A based on 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).
2. as claimed in claim 1 based on the A of carbon source efficiency utilization
2/ O-MBR multiple treating system, is characterized in that: in described membrane cisterna (6), be provided with membrane module, and membrane module adopts hollow fiber film assembly.
3. as claimed in claim 1 based on the A of carbon source efficiency utilization
2/ O-MBR multiple treating system, is characterized in that: in described anaerobic pond (1), the first anoxic pond (2), the second anoxic pond (5) and the oxygen pond (4) that disappears, arrange underwater scooter or agitator respectively.
4. as claimed in claim 1 based on the A of carbon source efficiency utilization
2/ O-MBR multiple treating system, is characterized in that: described Aerobic Pond (3) adopts micro-pore aeration system, and membrane cisterna (6) adopts perforated pipe aerating regulation system.
5. the A based on 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.
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| 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 |
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| CN109879421A (en) * | 2019-03-07 | 2019-06-14 | 北控水务(中国)投资有限公司 | It is a kind of based on multipoint water feeding and multi-mode operation can intensified anti-nitrated denitrification dephosphorization system |
| CN110066072A (en) * | 2019-05-16 | 2019-07-30 | 中国市政工程华北设计研究总院有限公司 | Sewage treatment optimizes operating system under a kind of maximum discharge standard |
| CN110066072B (en) * | 2019-05-16 | 2024-01-05 | 中国市政工程华北设计研究总院有限公司 | Sewage treatment optimizing operation system under high emission standard |
| CN112093899A (en) * | 2020-07-30 | 2020-12-18 | 同济大学 | Method and system for biological nitrogen and phosphorus removal of sewage |
| CN112093899B (en) * | 2020-07-30 | 2022-03-22 | 同济大学 | Method and system for biological nitrogen and phosphorus removal of sewage |
| CN112110615A (en) * | 2020-10-12 | 2020-12-22 | 北京安国水道自控工程技术有限公司 | Upgrading and reforming treatment process and system for urban sewage plant |
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