CN107129046B - A2Improved process for water treatment of/O-BCO - Google Patents

A2Improved process for water treatment of/O-BCO Download PDF

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CN107129046B
CN107129046B CN201710542802.9A CN201710542802A CN107129046B CN 107129046 B CN107129046 B CN 107129046B CN 201710542802 A CN201710542802 A CN 201710542802A CN 107129046 B CN107129046 B CN 107129046B
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bco
water treatment
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CN107129046A (en
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张淼
张颖
黄棚兰
何成达
吴军
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Yangzhou University
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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
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • 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
    • 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
    • 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
    • C02F3/308—Biological phosphorus removal
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

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  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

A2An improved process for water treatment of/O-BCO, which belongs to the technical field of biological sewage treatment. According to the invention, by increasing the starvation treatment of the falling biomembrane after the oxidation reaction of the sludge and the ammonia nitrogen, and then performing secondary adsorption of the residual organic matters, nitrogen and phosphorus, the negative influence of the organic matters on the nitrification process can be reduced, the contribution proportion of the organic matters in the denitrification dephosphorization process is increased, the enrichment degree of nitrifying bacteria and DPAOs is favorably improved, the denitrification dephosphorization potential of denitrifying phosphorus accumulating bacteria is stimulated, and the possibility is provided for the complete nitrification of the high ammonia nitrogen load sewage and the high TN removal rate.

Description

A2Improved process for water treatment of/O-BCO
Technical Field
The invention belongs to the technical field of biological sewage treatment.
Background
With the continuous development of sewage treatment technology, the denitrification and dephosphorization process is in a wide range, wherein the denitrification and dephosphorization technology provides a new idea for the synchronous denitrification and dephosphorization of sewage with low carbon-nitrogen ratio (C/N). DEPHANOX, A2N、A2The double-sludge denitrification dephosphorization process of NSBR and the like becomes the research focus of a plurality of scholars, but the process surpasses NH carried by sludge4 +N does not undergo a nitration step to give an effluent NH4 +The concentration of N is higher, the organic matters are not efficiently utilized, and a large amount of slow biodegradation organic matters in anaerobic effluent cause the mass propagation of heterotrophic bacteria in a biological membrane system, so that the nitrification efficiency is reduced, and the popularization and the application of the system are limited.
A2The proposal of the/O-BCO process alleviates the problems to a certain extent, uses nitrification as final effluent to reduce NH of the effluent4 +The concentration of N is increased, and the removal rate of TN is improved; a. the2the/O reactor does not undertake nitrification, and the return sludge does not contain NO3 -the-N can ensure better anaerobic state and longer anoxic zoneThe carbon source is fully utilized; BCO cells in multi-cell series can be based on NH4 +The aeration quantity is flexibly adjusted by N load, and the operation cost is reduced; the corridor-type structure is beneficial to the reconstruction of a new sewage treatment plant and an old sewage treatment plant. Because the organic matters have obvious influence on the enrichment of nitrifying bacteria and denitrifying phosphorus accumulating bacteria (DPAOs), particularly, although the COD concentration of a BCO unit is not high (<50 mg/L), but the enrichment degree of nitrifying bacteria in different chambers is greatly influenced by COD, so that the nitrogen and phosphorus removal efficiency in practical engineering is unstable, and therefore, the optimization of the flora structure is the key for further improving the nitrogen and phosphorus removal efficiency.
In fact, the organic matter remained in the BCO unit is basically refractory organic matter, and the traditional biological treatment method is difficult to realize in order to further reduce COD from 50 mg/L. The investment and operation cost of the treatment methods such as activated carbon adsorption, chemical oxidation, electrochemical oxidation and the like for treating low-concentration organic matters is relatively high, and many scholars at home and abroad turn to activated sludge with low cost and rich sources, and the method has the advantages of simple operation, strong adsorption efficiency and selectivity and no pollution, and is an economic and effective pretreatment method.
Disclosure of Invention
For existing A2The invention aims to provide an improved A which can improve the enrichment degree of nitrifying bacteria and denitrifying phosphorus-accumulating bacteria, realize efficient and stable nitrogen and phosphorus removal and high-standard discharge of effluent2the/O-BCO process.
The technical scheme of the invention is as follows: passing the sewage through a sewage treatment system A provided with an anaerobic zone, an anoxic zone and an aerobic zone2the/O reactor carries out synchronous denitrification and dephosphorization treatment, the discharged water after the denitrification and dephosphorization treatment carries out primary layering treatment, and part of the precipitated sludge after the primary layering treatment flows back to the reactor A2Anaerobic zone maintenance of the/O reactor A2Stable biomass in the/O reactor; the other part of the precipitated sludge after the first layering treatment and the biomembrane dropped after the ammonia nitrogen oxidation reaction are subjected to hunger treatment and then are mixed with the supernatant of the first layering treatment to carry out secondary adsorption of residual organic matters, nitrogen and phosphorus, and the mixture is subjected to secondary layering treatmentAfter layer treatment, supernatant obtained after the second layer treatment enters a BCO reactor, the oxidation reaction of ammonia nitrogen is carried out under aerobic condition, and partial nitrified liquid is taken and refluxed to A2The anoxic zone of the/O reactor provides an electron acceptor for denitrifying phosphorus removal.
According to the invention, by increasing the starvation treatment of the falling biomembrane after the oxidation reaction of the sludge and the ammonia nitrogen, and then performing secondary adsorption of the residual organic matters, nitrogen and phosphorus, the negative influence of the organic matters on the nitrification process can be reduced, the contribution proportion of the organic matters in the denitrification dephosphorization process is increased, the enrichment degree of nitrifying bacteria and DPAOs is favorably improved, the denitrification dephosphorization potential of denitrifying phosphorus accumulating bacteria is stimulated, and the possibility is provided for the complete nitrification of the high ammonia nitrogen load sewage and the high TN removal rate.
Compared with the prior art, the method of the invention has the following advantages:
1) compare with original A2The improved process only needs to add structures for hunger treatment and secondary adsorption of the sludge, and the treated sludge can quickly adsorb organic matters in the secondary adsorption and simultaneously adsorb a small amount of nitrogen and phosphorus by carrying out the hunger treatment on the sludge, so that the nitrogen and phosphorus removal effect is further enhanced.
2) The operation flow is simple, the operation and management are convenient, the competition of organic matters in the nitrification process on DO is weakened, the high enrichment of nitrifying bacteria is promoted, the biological activity of DPAOs is indirectly enhanced, and the removal rate of ammonia nitrogen and TN is improved.
3) By adopting the process, the residual sludge discharged by the system is utilized to adsorb low-concentration organic matters, no additional sludge is needed, the optimal configuration of the organic matters and the resource utilization of the residual sludge are realized, a new direction is expected to be brought to flora enrichment and deep degradation of the organic matters, and the COD of the effluent can even reach the III-class water body standard (COD is less than 20 mg/L) of the surface water.
4) The improved mode of sludge adsorption is not only suitable for a double-sludge system, but also provides ideas for the optimized operation of other nitrogen and phosphorus removal processes, and can promote the research of sludge resource and the industrialization process thereof.
5) The residual sludge after secondary adsorption can be used for recovering organic matters (such as anaerobic fermentation), and simultaneously can be used for recovering nitrogen and phosphorus by adding chemical reagents (such as phosphate, magnesium salt or alkali salt); the method gets rid of the dilemma of low C/N ratio sewage treatment effect caused by carbon source shortage, and simultaneously reduces the COD concentration of the effluent, thereby meeting the discharge requirement of higher standard.
Further, reflux into A2The sludge reflux ratio of the anaerobic zone of the/O reactor is 100%, during anaerobic reaction, A2The sludge concentration in the/O reactor is 8000 +/-100 mg/L, and the anaerobic reaction time is 1.2 +/-0.5 h. DPAOs synthesize internal carbon Sources (PHAs) by using easily degradable organic matters in raw water, and release phosphorus, so that most of the organic matters are removed.
The reflux ratio of the nitrifying liquid is 300 percent, and during the anoxic reaction, A2The sludge concentration in the/O reactor is 2500 +/-100 mg/L, and the anoxic reaction time is 6.0 +/-0.5 h. The reflux ratio of the nitrifying liquid is designed to provide sufficient electron acceptors for the denitrification and phosphorus removal process, and higher synchronous denitrification and phosphorus removal effects can be obtained by longer anoxic reaction time.
In A2When the aerobic reaction is carried out in the/O reactor, the dissolved oxygen is 2.0-2.5 mg/L, the aerobic reaction time is 1.2 +/-0.5 h, and the oxidation-reduction potential ORP is 50-80 mV. The stage does not carry out nitration, and the main function is to further absorb phosphorus and simultaneously blow off N generated in the denitrification process2。
In order to fully adsorb, part of the precipitate after the second layering treatment can be circularly adsorbed by organic matters, nitrogen and phosphorus. On one hand, the stable biomass of the adsorption unit is maintained through sludge circulation, and on the other hand, the retention time of sludge is increased to strengthen the adsorption effect.
The amount of dissolved oxygen during the starvation treatment is 3.0mg/L +/-0.5 mg/L, and the starvation treatment time is 1.0-3.0 h. The sludge is in a hungry state by a short-time aeration mode, the sludge reduction is realized while the resource utilization of the residual sludge is realized, the operation is simple, and the operation and the management are convenient.
The sludge discharge ratio of the secondary layering treatment is 0.1-0.2, and the sludge retention time is 5-10 days. Through the renewal of mud in order to guarantee good adsorption effect, adsorption efficiency is high and the operation effect is stable.
In addition, the suspension filling is put into the BCO reactorThe specific surface area of the material and the suspended filler is 1000 +/-50 m2/m3And the filling rate of the suspended filler in the BCO reactor is 50-55%. Because of the higher specific surface area, the surface biological quantity of the filler is high, the nitration efficiency is high-efficient and stable, and the impact resistance is strong.
And during the oxidation reaction of the ammonia nitrogen, the dissolved oxygen is 3.0-3.5 mg/L, the filler is in a fluidized state, and the hydraulic retention time is 2-3 h. Besides the good completion of ammonia nitrogen oxidation reaction, the three chambers can respectively and flexibly adjust the aeration quantity, thereby further saving energy and reducing consumption.
Drawings
FIG. 1 is a schematic diagram of a structure of the process of the present invention.
Detailed Description
Firstly, equipment preparation:
as shown in fig. 1, the apparatus has: 1-raw water tank; 2-a water inlet pump; 3-A2an/O reactor; 4-a stirring device; 5-A2An anaerobic zone of the/O reactor; 6-A2An anoxic zone of the/O reactor; 7-A2An aerobic zone of the/O reactor; 8-an aerator; 9-an intermediate sedimentation tank; 10-a secondary sedimentation tank; 11-an intermediate water tank; 12-an intermediate lift pump; 13-BCO reactor; 14-a precipitation zone; 15-suspended fillers; 16-an overflow port; 17, 22, 27-flow meter; 18-a blower; 19-nitrifying liquid reflux pump; 20-sludge reflux pump; 21-a mud storage pool; 23-a sludge circulating pump; 24, 25, 26-mud valve; 28-water outlet tank.
The water outlet of the raw water tank 1 is connected with the water inlet A through a water inlet pump 22On the water inlet of the/O reactor 3.
A2the/O reactor 3 is composed of an anaerobic zone 5, an anoxic zone 6 and an aerobic zone 7 which are connected in sequence.
A2The anaerobic zone 5 and the anoxic zone 6 of the/O reactor 3 are both provided with a stirring device 4, the bottom of the aerobic zone 7 and the bottom of the BCO reactor 13 are both provided with aeration heads 8, and the regulation and control of the dissolved oxygen are realized through a blower 18, a flowmeter 17 and a flowmeter 27 respectively.
A2The water outlet of the aerobic zone 7 of the/O reactor 3 is connected with the water inlet of the intermediate sedimentation tank 9 through a pipeline.
Part of the sludge of the intermediate sedimentation tank 9Is connected with A through a sludge reflux pump 202The other part of sludge enters a sludge storage tank 21 through a sludge discharge valve 24 at the bottom of the anaerobic zone 5 of the/O reactor 3, and the effluent of the intermediate sedimentation tank 9 is connected with a secondary sedimentation tank 10.
Partial sludge of the secondary sedimentation tank 10 enters the sludge storage tank 21 through the sludge discharge valve 25, the other part of sludge is directly discharged, and the supernatant of the secondary sedimentation tank 10 is connected with the intermediate water tank 11 and is pumped into the BCO reactor 13 through the intermediate lift pump 12.
The water outlet of the BCO reactor 13 is connected with the sedimentation zone 14, the sedimentation zone 14 is provided with an overflow port 16, the bottom of the sedimentation zone 14 is provided with a sludge discharge valve 26, and the sludge discharge valve is connected with a sludge storage tank 21 through a pipeline. An overflow port 16 of the settling zone 14 is connected with an effluent water tank 28 and is connected with A through a nitrification reflux pump 192An anoxic zone 6 of the/O reactor 3.
A suspended filler 15 is arranged in the BCO reactor 13, the material is polypropylene, and the specific surface area is 1000 +/-50 m2/m3And the filling rate of the suspended filler in the BCO reactor is 50-55%. The filler is in a fluidized state by starting the blower 18 and the flowmeter 27 to regulate and control dissolved oxygen, so that the substrate is ensured to be fully contacted with microorganisms, and the main function is to complete ammonia nitrogen oxidation.
The sludge storage tank 21 receives the sludge discharged from the intermediate sedimentation tank 9, the secondary sedimentation tank 10 and the sedimentation zone 14 or the fallen biological films, and the sludge is subjected to a transient hungry state by regulating and controlling dissolved oxygen by starting the blower 18 and the flow meter 22.
II, treatment process:
1. the domestic sewage in the raw water tank 1 enters the sewage tank A through the water inlet pump 2 and the return sludge sent by the sludge return pump 202Anaerobic zone 5 of the/O reactor 3, the sludge reflux ratio being 100%, in order to maintain A2The stable biomass in the/O reactor is fully mixed and reacted under the action of a stirring device 4, the anaerobic reaction time is 1.2 h, and the sludge concentration is about 8000 mg/L; DPAOs synthesize internal carbon Sources (PHAs) by using easily degradable organic matters in raw water, and release phosphorus, so that most of the organic matters are removed.
2. The mixed liquid after the anaerobic reaction enters an anoxic zone 6, and simultaneously, nitrified liquid which is completely nitrified and subjected to solid-liquid separation by a BCO reactor 13 enters the anoxic zone, and the nitrified liquid is nitrifiedThe liquid reflux ratio is 300 percent, the anoxic reaction time is 6.0 h, and the sludge concentration is about 2500 mg/L; DPAOs with PHAs as electron donors and NO3 -and-N is an electron acceptor for synchronous nitrogen and phosphorus removal.
3. The mixed liquid after the anoxic reaction enters an aerobic zone 7, the aerobic reaction time is 1.2 h, a flowmeter 17 is started to ensure that the dissolved oxygen is 2.0-2.5 mg/L, and the oxidation-reduction potential ORP is 50-80 mV; the stage does not carry out nitration, and the main function is to further absorb phosphorus and simultaneously blow off N generated in the denitrification process2。
4. The intermediate sedimentation tank 9 is used for separating mud from water, and adopts an operation mode of water outlet at the periphery of intermediate water inlet, and the sedimentation time is 1.5-2.0 h; a part of the precipitated sludge is returned to A through a sludge return pump 202The other part of the residual sludge in the anaerobic zone 5 of the/O reactor 3 enters a sludge storage tank 21 through a sludge discharge valve 24.
5. The sludge in the sludge storage tank 21 is aerated by the blower 18 and the flowmeter 22, dissolved oxygen is about 3.0mg/L, and after the sludge is subjected to hunger treatment for 1.0-3.0 h, the sludge is pumped into the secondary sedimentation tank 10 by the sludge circulating pump 23 to realize rapid adsorption of residual organic matters, nitrogen and phosphorus.
6. The sedimentation time in the secondary sedimentation tank 10 is 0.5-1.0 h. One part of the sludge after adsorption returns to the sludge storage tank 21 through the sludge discharge valve 25 for recycling, the other part is discharged periodically, the sludge discharge ratio is 0.1-0.2, and the sludge retention time is 5-10 d.
7. The effluent of the secondary sedimentation tank 10 enters an intermediate water tank 11, enters a BCO reactor 13 through an intermediate lift pump 12, and is adjusted by a flow meter 27 to ensure that the three-grid dissolved oxygen is 3.0-3.5 mg/L, so that the filler is in a fluidized state, and the hydraulic retention time is 2-3 h, thereby completing the oxidation of ammonia nitrogen.
8. The water body after the reaction in the BCO reactor 13 then enters the sedimentation zone 14, and the fallen biological membrane enters the sludge storage tank 21 from the bottom sludge discharge valve 26 for starvation treatment; supernatant in the settling zone 14 enters an effluent water tank 28 through an overflow port 16, and a part of effluent enters A through a nitrifying liquid reflux pump 192An anoxic zone 6 of the/O reactor 3 provides an electron acceptor for denitrifying phosphorus removal, and the other part is directly discharged.
Third, application example:
example 1:
adopt the actual domestic sewage of students' dormitory district manure pit in certain campus, the quality of water of intaking is as follows: COD (180.3)+30.5）、NH4 +-N（51.2+10.3）、NO3 --N（0.5+0.2）、NO2 --N（0.12+0.1）、TP（5.5+1.4) mg/L, which belongs to typical low C/N sewage. Improvement A2After the/O-BCO process is debugged and stably operated for 45 d, compared with the prior art, the percentage content of DPAOs is increased by 4.5%, the total amount of nitrobacteria (including ammonia oxidizing bacteria AOB and nitrite oxidizing bacteria NOB) in three chambers is increased by 5.3%, 3.2% and 1.8%, and the enrichment degree of functional bacteria is increased.
Raw water enters A2The concentration of COD, TN and TP in the effluent of the intermediate sedimentation tank is 43.5, 15.7 and 0.45 mg/L after the/O reactor is subjected to anaerobic, anoxic and aerobic plug flow processes. After the rest sludge is subjected to aeration starvation treatment for 1.5 h in the sludge storage tank, the rest sludge is rapidly adsorbed in a secondary sedimentation tank for 0.5h, the COD concentration is reduced from 43.5 mg/L to 19 mg/L, simultaneously the TN and TP concentrations are respectively reduced by 1.2 and 0.3 mg/L, and the COD and NH of the final effluent of the system4 +The concentrations of indexes such as-N, TN, TP and the like are respectively 18.5, 0.8, 13.4 and 0.12mg/L, which are superior to the first-level A discharge standard, wherein the effluent COD reaches the III-class water body discharge standard of surface water.
Example 2:
by modifying A2The mixed wastewater of the actual domestic sewage and certain landfill leachate is treated by the/O-BCO process, and NH is fed into the mixed wastewater4 +The concentration of-N is 100-120 mg/L, the C/N of inlet water is about 4.5, and NH of system outlet water4 +Concentration of-N, TN was 4.5mg/L and 20mg/L, respectively, NH4 +The concentration of N reaches the first-level A emission standard, and the removal rate can reach 83% at most although the concentration of TN does not reach the standard. Because the components of the landfill leachate are complex, the microbial flora of the system is difficult to adapt to the water quality change in a short time, and the removal effect is still to be improved. It is believed that the improvement A is obtained by2On the premise of long-term optimized operation of the/O-BCO process and further improvement of the enrichment degree of functional bacteria, the system can obtain higher NH4 +-N andTN removal rate.
Therefore, the process disclosed by the invention not only reflects the advantages of the double-sludge denitrification dephosphorization technology, but also enables the residual sludge of the system to be treated and recycled, reduces the concentration of organic matters entering the BCO unit, weakens the negative influence of the organic matters on the enrichment of nitrifying bacteria, strengthens the nitrification and denitrification dephosphorization effects, provides possibility for the complete nitrification and high TN removal rate of high ammonia nitrogen load sewage, and enables the effluent to meet the discharge requirement of a higher standard.

Claims (9)

1. A2The improved water treatment process of/O-BCO is characterized by that the sewage is passed through A equipped with anaerobic zone, anoxic zone and aerobic zone2the/O reactor carries out synchronous denitrification and dephosphorization treatment, the discharged water after the denitrification and dephosphorization treatment carries out primary layering treatment, and part of the precipitated sludge after the primary layering treatment flows back to the reactor A2Anaerobic zone maintenance of the/O reactor A2Stable biomass in the/O reactor; the method is characterized in that: starving the other part of the precipitated sludge subjected to the first layering treatment and a biomembrane falling off after ammonia nitrogen oxidation reaction, mixing the starved part of the precipitated sludge and the supernatant subjected to the first layering treatment, performing secondary adsorption of residual organic matters, nitrogen and phosphorus, performing secondary layering treatment, feeding the supernatant subjected to the secondary layering treatment into a BCO reactor, performing ammonia nitrogen oxidation reaction under aerobic condition, and taking part of nitrified liquid to flow back to A2The anoxic zone of the/O reactor provides an electron acceptor for denitrifying phosphorus removal.
2. The improved process of water treatment of claim 1, wherein: reflux into A2The sludge reflux ratio of the anaerobic zone of the/O reactor is 100%, during anaerobic reaction, A2The sludge concentration in the/O reactor is 8000 +/-100 mg/L, and the anaerobic reaction time is 1.2 +/-0.5 h.
3. The improved process of water treatment of claim 1, wherein: the reflux ratio of the nitrifying liquid is 300 percent, and during the anoxic reaction, A2The sludge concentration in the/O reactor is 2500 +/-100 mg/L, and the anoxic reaction time is 6.0 +/-0.5h。
4. The improved process of water treatment of claim 1, wherein: in A2When the aerobic reaction is carried out in the/O reactor, the dissolved oxygen is 2.0-2.5 mg/L, the aerobic reaction time is 1.2 +/-0.5 h, and the oxidation-reduction potential ORP is 50-80 mV.
5. The improved process of water treatment of claim 1, wherein: and (4) circularly adsorbing organic matters, nitrogen and phosphorus by using part of precipitates after the secondary layering treatment.
6. The improved process of water treatment according to claim 1 or 5, wherein: the amount of dissolved oxygen during the starvation treatment is 3.0mg/L +/-0.5 mg/L, and the starvation treatment time is 1.0-3.0 h.
7. The improved process of water treatment of claim 1, wherein: the sludge discharge ratio of the secondary layering treatment is 0.1-0.2, and the sludge retention time is 5-10 days.
8. The improved process of water treatment of claim 1, wherein: suspending filler is put into the BCO reactor, and the specific surface area of the suspending filler is 1000 +/-50 m2/m3And the filling rate of the suspended filler in the BCO reactor is 50-55%.
9. The improved process of water treatment according to claim 1 or 8, wherein: the dissolved oxygen during the ammonia nitrogen oxidation reaction is 3.0-3.5 mg/L, the filler is in a fluidized state, and the hydraulic retention time is 2-3 h.
CN201710542802.9A 2017-07-05 2017-07-05 A2Improved process for water treatment of/O-BCO Active CN107129046B (en)

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