CN116589096A - Multi-mode AAO-MBR (anaerobic-anoxic-oxic-Membrane biological reactor) technical process control system and method - Google Patents
Multi-mode AAO-MBR (anaerobic-anoxic-oxic-Membrane biological reactor) technical process control system and method Download PDFInfo
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- 239000012528 membrane Substances 0.000 title claims abstract description 79
- 238000004886 process control Methods 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 196
- 239000010802 sludge Substances 0.000 claims abstract description 86
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 74
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 73
- 238000005273 aeration Methods 0.000 claims abstract description 58
- 238000009826 distribution Methods 0.000 claims abstract description 33
- 239000010865 sewage Substances 0.000 claims abstract description 32
- 230000001276 controlling effect Effects 0.000 claims abstract description 27
- 238000012544 monitoring process Methods 0.000 claims abstract description 27
- 238000012545 processing Methods 0.000 claims abstract description 22
- 230000001105 regulatory effect Effects 0.000 claims abstract description 19
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 15
- 238000010992 reflux Methods 0.000 claims description 77
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 47
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 47
- 229910052698 phosphorus Inorganic materials 0.000 claims description 47
- 239000011574 phosphorus Substances 0.000 claims description 47
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 claims description 37
- 239000003795 chemical substances by application Substances 0.000 claims description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 21
- 229910052760 oxygen Inorganic materials 0.000 claims description 21
- 239000001301 oxygen Substances 0.000 claims description 21
- 230000000813 microbial effect Effects 0.000 claims description 14
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 12
- 239000002028 Biomass Substances 0.000 claims description 11
- 239000011259 mixed solution Substances 0.000 claims description 10
- 238000013461 design Methods 0.000 claims description 8
- 239000003814 drug Substances 0.000 claims description 6
- 244000005700 microbiome Species 0.000 claims description 5
- 230000007812 deficiency Effects 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 238000005261 decarburization Methods 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 14
- 238000005065 mining Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 9
- 238000004364 calculation method Methods 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 238000005192 partition Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 230000004075 alteration Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 241000219000 Populus Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
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- 230000009286 beneficial effect Effects 0.000 description 1
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- 238000005262 decarbonization Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000002207 metabolite Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004445 quantitative analysis Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
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Classifications
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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
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/003—Downstream control, i.e. outlet monitoring, e.g. to check the treating agents, such as halogens or ozone, leaving the process
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- 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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- Life Sciences & Earth Sciences (AREA)
- 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)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a multimode AAO-MBR technical process control system and a method, wherein the system comprises the following steps: the control equipment, the monitoring component and the AAO biochemical tank and the MBR membrane tank are communicated; the monitoring component collects the water inflow and sewage parameters of the AAO biochemical tank; the control equipment comprises a processing component and a regulating and controlling component, wherein the processing component receives and analyzes the data of the monitoring component and feeds back an adjustment instruction to the regulating and controlling component; the water inlet distribution module in the regulation and control assembly controls water inlet distribution to the anaerobic zone and the first anoxic zone, the aeration module controls aeration amount entering each aerobic zone, the backflow module controls the MBR membrane pond to flow back to the first aerobic zone, the first aerobic zone to the first anoxic zone and the first anoxic zone to the anaerobic zone, the carbon source module feeds carbon source to each anoxic zone, the dephosphorization reagent module feeds dephosphorization reagent to the second aerobic zone, and the sludge discharge module controls the MBR membrane pond to discharge sludge. The scheme maximizes the processing capacity of the mining multi-mode AAO-MBR process system and achieves the lowest external consumption.
Description
Technical Field
The invention relates to the technical field of sewage biological treatment, in particular to a multi-mode AAO-MBR (anaerobic-anoxic-oxic-Membrane biological reactor) technical process control system and method.
Background
In recent years, the requirements of the total sewage amount, the effluent standard and the environmental friendliness of each place are continuously improved, but the land resources are more and more tensioned, and the multi-mode AAO+MBR process with higher denitrification efficiency and land saving is receiving more and more attention.
The process has the characteristics of high sludge concentration, long sludge age and low sludge load, so that nutrient substances in a system are relatively lacking, microorganisms have strong endogenous denitrification effect, excessive carbon sources penetrate through an anoxic zone to enter an aerobic zone, and the phenomena of waste of the carbon sources and aeration quantity and the like are caused. Longer sludge age is unfavorable for biological dephosphorization of the system, and secondary release of phosphorus in an aerobic zone is easy to cause, so that the adding amount of chemical dephosphorization agents is increased. In addition, excessive reagent addition and higher sludge concentration can accelerate membrane pollution, affect the service life of a membrane module and reduce water yield.
In the traditional operation control, a process data feedback decision mechanism is lacked, and the operation condition cannot be scientifically and accurately regulated. Under the condition of lacking calculation and analysis of a process control system, the effluent reaches the standard by increasing the aeration rate and the reflux ratio of each stage of the blower, increasing the external carbon source and the dephosphorization agent and the cleaning frequency of the membrane component, thereby reducing the service life of the equipment, increasing the labor intensity, remarkably increasing the running cost of sewage treatment and being unfavorable for the efficient, stable and sustainable running of a water plant.
Thus, precise control over wastewater treatment processes is a hotspot of current research. As disclosed in patent CN111547848A, a partition control and point-feed enhanced nitrogen and phosphorus removal (a/O/a) -MBR integrated process and a system device thereof, wherein the system sequentially performs anaerobic phosphorus release treatment, aerobic phosphorus absorption and nitrification treatment, precipitation effluent, denitrification and MBR nitrification and decarbonization treatment on low C/N ratio domestic sewage according to time sequence, and performs partition control on the phosphorus removal and denitrification processes to realize spatial separation of phosphorus removal bacteria and nitrifying bacteria; meanwhile, the problem of adding carbon sources is solved by adopting a mode of water inlet at different points. The defects of the prior art are that reasonable regulation and control cannot be performed in real time according to the water quality condition of inflow water and the water quality condition of a biochemical system along the way, and the treatment capacity of the submerged excavating system cannot be maximized to realize the lowest external consumption.
As in patent CN110790381a, a full-flow intelligent control system based on an AAO sewage treatment process is provided, where the full-flow intelligent control system includes a data acquisition module, a real-time control module for grouping an intake pump, a real-time control module for aeration of an aerobic tank, a control module for controlling an internal reflux pump, a real-time control module for adding a carbon source, a real-time control module for adding a dephosphorizing agent, and a real-time control module for controlling a sludge pump. The prior art cannot be suitable for a complex reflow process, and is lack of quantitative analysis for real-time regulation and control of the process.
Therefore, how to design the water quality condition capable of being monitored in real time and reasonably quantitatively analyze and regulate the water quality condition so as to maximize the processing capacity of the multi-mode AAO+MBR process system and minimize the external consumption is a problem to be solved by the technicians in the field.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a multi-mode AAO-MBR process control system and a multi-mode AAO-MBR process control method, which regulate and control according to the real-time water quality condition of water inflow and the water quality condition in biochemical treatment, regulate and control the operation working conditions of the multi-mode AAO+MBR process in real time, solve the problems of unscientific water inflow proportion distribution, excessive or insufficient aeration quantity of a blower, excessive or insufficient reflux ratio of each level, unreasonable carbon source addition quantity and point positions, improve the accuracy, high efficiency, automaticity and stability of process operation, maximize the processing capacity of the submerged technology, and realize the lowest external consumption.
In a first aspect, the present invention provides a multi-mode AAO-MBR process control system, comprising: the system comprises control equipment, a monitoring assembly, an AAO biochemical tank and an MBR membrane tank, wherein the AAO biochemical tank is communicated with the MBR membrane tank;
the AAO biochemical tank comprises an anaerobic zone, an anoxic zone and an aerobic zone which are sequentially arranged, wherein the number of the anoxic zone and the aerobic zone is at least two, each anoxic zone is arranged in a crossing way with each aerobic zone, the anoxic zone and the aerobic zone which are adjacent to the anaerobic zone are respectively a first anoxic zone and a first aerobic zone, and the anoxic zone and the aerobic zone which are adjacent to the MBR membrane tank are respectively a second anoxic zone and a second aerobic zone;
the monitoring component collects the water inflow of the AAO biochemical tank and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank;
the control equipment comprises a processing component and a regulating and controlling component, wherein the processing component receives and analyzes the data of the monitoring component and feeds back an adjustment instruction to the regulating and controlling component;
the regulation and control assembly comprises a water inlet distribution module, an aeration module, a reflux module, a carbon source module, a dephosphorization medicament module and a sludge discharge module, wherein the water inlet distribution module controls water inlet distribution to the anaerobic zone and the first anoxic zone, the aeration module controls aeration amount entering each aerobic zone, the reflux module controls the MBR membrane pond to flow back to the first aerobic zone, the first aerobic zone to the first anoxic zone and the first anoxic zone to the anaerobic zone, the carbon source module feeds a carbon source to each anoxic zone, the dephosphorization medicament module feeds a dephosphorization medicament to the second aerobic zone, and the sludge discharge module controls the MBR membrane pond to discharge sludge.
Further, BOD/TP in the anaerobic zone is more than or equal to 17, BOD/TN in the anoxic zone is more than or equal to 4, the water inlet ratio of the anaerobic zone is 50% -70%, the reflux ratio of the first anoxic zone to the anaerobic zone is 100% -200%, the reflux ratio of the first aerobic zone to the first anoxic zone is 300% -500%, and the reflux ratio of the MBR membrane pond to the first aerobic zone is 400% -600%.
Further, the sewage parameters of each zone in the AAO biochemical tank comprise the inlet BOD concentration of the AAO biochemical tank, the concentration and total phosphorus concentration of the sludge mixture discharged by the AAO-MBR, the residual sludge discharged by the AAO-MBR, the outlet BOD concentration of the anaerobic zone, the reflux ratio of the first anoxic zone to the anaerobic zone, the outlet nitrate nitrogen concentration of the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the C/N value of the first anoxic zone, the carbon source adding concentration of the first anoxic zone and the denitrification rate of the first anoxic zone;
the water inlet distribution module controls water inlet distribution to the anaerobic zone and the first anoxic zone, and specifically comprises the following steps:
the treatment component receives and analyzes the water inflow flow of the AAO biochemical tank, the water inflow BOD concentration of the AAO biochemical tank, the sludge mixed liquor concentration and the total phosphorus concentration discharged by the AAO-MBR, the residual sludge quantity discharged by the AAO-MBR, the water outflow BOD concentration of the anaerobic zone, the reflux ratio of the first anoxic zone to the anaerobic zone, the water nitrate nitrogen concentration discharged by the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the C/N value of the first anoxic zone and the carbon source adding concentration of the first anoxic zone, and feeds back an adjustment instruction to the water inflow distribution module to control the water inflow distribution ratio to the anaerobic zone and the first anoxic zone.
Further, a relational formula for controlling the water distribution ratio to the anaerobic zone and the first anoxic zone is as follows:
β 2 ＝1-β 1
wherein beta is 1 To distribute the proportion of water into the anaerobic zone, alpha 1 P is the total phosphorus concentration of the sludge mixed solution discharged by the AAO-MBR and is the phosphorus content in the sludge in the anaerobic zone 0 The total phosphorus concentration of supernatant liquid in the sludge mixed solution discharged by AAO-MBR, X 0 For the concentration of the sludge mixed solution discharged by the AAO-MBR, delta X is the residual sludge discharged by the AAO-MBR, R 3 The reflux ratio of the first anoxic zone to the anaerobic zone is Q is the inflow water flow of the AAO biochemical tank, Z 0 BOD concentration, Z of the inflow water of the AAO biochemical tank 1-go out BOD concentration, X of effluent from anaerobic zone 2-1 The concentration of nitrate nitrogen in the effluent water of the first anoxic zone, f is the C/N value of the first anoxic zone, beta 2 To distribute the proportion of water into the first anoxic zone, X 3-1 R is the concentration of nitrate nitrogen in the effluent water of the first aerobic zone 2 Z is the reflux ratio of the first aerobic zone to the first anoxic zone External throwing 1 Adding concentration E into the carbon source of the first anoxic zone 1 For the denitrification rate of the first anoxic zone, H is the carbon source deficiency coefficient, and when f is more than or equal to 4, H=0, and when f is less than 4, H=1-f/4.
Further, the two anoxic zones are arranged, and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank further comprise TN concentration of the AAO-MBR effluent, reflux ratio of the MBR membrane tank to the first aerobic zone, nitrate nitrogen concentration of the effluent of the second aerobic zone, ammonia nitrogen concentration of the effluent of the second aerobic zone, denitrification rate of the second anoxic zone, nitrate nitrogen concentration of the effluent of the anaerobic zone, volume of the first anoxic zone, sludge concentration of the first anoxic zone, decarburization speed of the first anoxic zone and design temperature of the first anoxic zone.
Further, the carbon source module adds a carbon source to each anoxic zone, specifically including:
the processing component receives the TN concentration of the AAO-MBR effluent collected by the monitoring component, analyzes the relation between the TN concentration of the AAO-MBR effluent and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank, and has the following relation formula:
if the TN concentration of the AAO-MBR effluent is higher than a preset value, feeding back an adjustment instruction to the carbon source module, and controlling the carbon source feeding to the first anoxic zone and the second anoxic zone, wherein the method specifically comprises the following steps:
the TN concentration of the AAO-MBR effluent is higher than a preset value, ifAdding carbon source into the first anoxic zone;
determining the amount of carbon source added to the first anoxic zone by analyzing the concentration of the nitric oxide in the first anoxic zone, wherein the relationship formula between the concentration of the nitric oxide in the first anoxic zone and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank is as follows:
determining the carbon source adding amount to the second anoxic zone by combining a TN concentration relation formula of the AAO-MBR effluent and a set denitrification rate of the second anoxic zone;
wherein Y is TN TN concentration, X of AAO-MBR effluent 5-1 The concentration of the nitrate nitrogen in the effluent water of the second aerobic zone is Y 5-2 advances Ammonia nitrogen concentration of the second aerobic zone, E 2 For the denitrification rate of the second anoxic zone, beta 2 To distribute the proportion of water into the first anoxic zone, X 3-1 R is the concentration of nitrate nitrogen in the effluent water of the first aerobic zone 2 Z is the reflux ratio of the first aerobic zone to the first anoxic zone 0 BOD concentration, X of inflow water of AAO biochemical tank 2-1 in The concentration of nitrate nitrogen and X of the inlet water of the first anoxic zone 1-1 The concentration of nitrate nitrogen and beta of effluent water of an anaerobic zone 1 In order to distribute the water into the anaerobic zone, Q is the water inflow of the AAO biochemical tank, V A1 For the volume of the first anoxic zone, S A1 For the sludge concentration of the first anoxic zone, R 1 Is an MBR membraneReflux ratio of pool to first aerobic zone, R 2 R is the reflux ratio of the first aerobic zone to the first anoxic zone 3 K is the reflux ratio of the first anoxic zone to the anaerobic zone de(20) Is the denitrification rate at 20 ℃, and T is the design temperature of the AAO biochemical tank and the MBR membrane tank.
Further, the two aerobic areas are arranged, and the sewage parameters of each area in the AAO biochemical tank and the MBR membrane tank comprise the reflux ratio of the MBR membrane tank to the first aerobic area, the reflux ratio of the first aerobic area to the first anoxic area, the ammonia nitrogen concentration in the water inlet of the first aerobic area, the ammonia nitrogen concentration in the water outlet of the first aerobic area and the microbial biomass in the water outlet of the first aerobic area, the ammonia nitrogen concentration in the water inlet of the second aerobic area, the ammonia nitrogen concentration in the water outlet of the second aerobic area and the microbial biomass in the water outlet of the second aerobic area, the water inlet TP concentration in the AAO biochemical tank, the water outlet TP concentration in the AAO biochemical tank, the residual sludge discharged by the AAO-MBR and the phosphorus content in the sludge in the second aerobic area;
the aeration module controls the aeration quantity entering each aerobic zone, and specifically comprises the following steps:
the treatment assembly receives and analyzes the water inflow rate of the AAO biochemical tank, the reflux ratio of the MBR membrane tank to the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the water inflow ammonia nitrogen concentration of the first aerobic zone, the water outflow ammonia nitrogen concentration of the first aerobic zone and the water outflow microbial biomass of the first aerobic zone, and feeds back an adjustment instruction to the aeration module to control the aeration amount to the first aerobic zone;
the treatment assembly receives and analyzes the AAO biochemical tank water inflow rate, the backflow ratio of the MBR membrane tank to the first aerobic zone, the second aerobic zone water inflow ammonia nitrogen concentration, the second aerobic zone water outlet ammonia nitrogen concentration and the second aerobic zone water outlet microbial biomass acquired by the monitoring assembly, and feeds back an adjustment instruction to the aeration module to control the aeration amount to the second aerobic zone;
the dephosphorization reagent module adds the dephosphorization reagent to the second aerobic zone, and specifically comprises:
the treatment component receives and analyzes the AAO biochemical tank water inflow flow, the AAO biochemical tank water inflow TP concentration, the AAO biochemical tank water outflow TP concentration, the AAO-MBR discharged surplus sludge quantity and the phosphorus content in the sludge of the second aerobic zone, and feeds back an adjustment instruction to the phosphorus removal agent module to control the addition of the phosphorus removal agent to the second aerobic zone.
Further, the relation formula for controlling the aeration rate to the first aerobic zone is as follows:
O 1 oxygen ＝0.00457(1+R 1 +R 2 )Q(Y 3-2 advances -Y 3-2 )-0.548△M V2
The relation formula for controlling the aeration amount to the second aerobic zone is as follows:
O 2 oxygen ＝0.00457(1+R 1 )Q(Y 5-2 advances -Y 5-2 )-0.548△M V3
Wherein Q is the inflow water flow of an AAO biochemical tank, R 1 For the reflux ratio of the MBR membrane pool to the first aerobic zone, R 2 For the reflux ratio of the first aerobic zone to the first anoxic zone, O 1 oxygen O is the aeration quantity of the first aerobic zone 2 oxygen Is the aeration quantity of the second aerobic zone, Y 3-2 advances The ammonia nitrogen concentration of the water entering the first aerobic zone, Y 3-2 The ammonia nitrogen concentration of the effluent of the first aerobic zone, Y 5-2 advances The ammonia nitrogen concentration of the water entering the second aerobic zone is Y 5-2 The ammonia nitrogen concentration of the effluent water of the second aerobic zone, delta M v2 For the water microbial mass of the first aerobic zone, deltaM v3 The microbial biomass of the second aerobic zone.
Further, the relation formula for controlling the addition of the dephosphorization reagent to the second aerobic zone is as follows:
wherein M is Dephosphorization In order to add the total amount of the dephosphorization reagent to the second aerobic zone, Q is the inflow water flow of the AAO biochemical tank, alpha 2 For the phosphorus content in the sludge of the second aerobic zone, deltaX is the residual sludge discharged by AAO-MBR, gamma is the adding mole ratio of the dephosphorization agent, delta is the effective content of Al salt in the dephosphorization agent, TP Feeding in And TP Out of Respectively the concentrations of inflow and outflow water TP of the AAO biochemical tank.
In a second aspect, the present invention also provides a multi-mode AAO-MBR process control method, which adopts the multi-mode AAO-MBR process control system as described above, and specifically includes the following steps:
starting a multi-mode AAO-MBR process control system;
the monitoring component collects the water inflow of the AAO biochemical tank and the sewage parameters of each area in the AAO biochemical tank;
the processing component receives and analyzes the data of the monitoring component, and feeds back an adjustment instruction to the regulation and control component, so that the sewage parameters of the AAO biochemical tank are maintained in a preset interval.
The invention provides a multimode AAO-MBR technical process control system and a multimode AAO-MBR technical process control method, which at least comprise the following beneficial effects:
(1) The operation conditions of the multi-mode AAO+MBR process are regulated in real time, the problems that the water inlet proportion is scientifically distributed, the aeration amount of a blower and the reflux ratio of each level are too large or insufficient, the carbon source addition amount and the point position are unreasonable are solved, the processing capacity of the submerged technology is maximized, and the lowest external consumption is realized.
(2) By combining the change of the quality of the inlet water, reasonable inlet water distribution proportion is considered, and the high-efficiency utilization of the inlet water carbon source is improved; through the control equipment, the uniformity of water distribution is realized, and the control precision is improved.
(3) The accurate calculation of the adding point position and the adding amount of the external carbon source is realized by combining the influences of the differences of sludge concentrations of different functional partitions, the design pool capacity and the denitrification rate; in the system control, the influence of secondary phosphorus release caused by long mud age is considered, and the stability of the yielding water TP is ensured to reach the standard.
(4) The mud discharge control system is effectively combined with membrane pollution control, so that the effects of effective early warning of membrane pollution, prolonged service life, energy conservation and consumption reduction are realized.
(5) The aeration gas quantity is controlled based on the change of the ammonia nitrogen concentration along the aerobic zone, so that the nitrification efficiency is improved, the aeration gas quantity is reduced, and the energy consumption is reduced; meanwhile, the high-dissolved oxygen reflux liquid brought by excessive aeration is reduced to enter the anoxic zone, so that the waste of carbon sources is caused.
Drawings
FIG. 1 is a block diagram of a multi-mode AAO-MBR process control system provided by the invention;
FIG. 2 is a flow chart of a method for controlling a multi-mode AAO-MBR process according to the present invention.
Reference numerals illustrate: the device comprises a 1-AAO biochemical tank, a 2-MBR membrane tank, a 3-control device, a 4-monitoring component, a 5-regulation component, a 6-intelligent water distribution weir, a 7-blower, an 8-pressure transmitter, a 9-electric air regulating valve, a 10-thermal type gas flowmeter, a 11-MBR membrane tank to a first aerobic zone reflux pump, a 12-first aerobic zone to a first anoxic zone reflux pump, a 13-first anoxic zone to an anaerobic zone reflux pump, a 14-flowmeter, a 15-carbon source adding component, a 16-dephosphorization reagent adding component, a 17-sludge pump, a 18-sludge concentration meter, a 19-BOD meter, a 20-nitrogen nitrate meter, a 21-ammonia nitrogen meter, a 22-dissolved oxygen meter, a 23-MBR membrane component, a 24-treatment component, a 25-anaerobic zone, a 26-first anoxic zone, a 27-first aerobic zone, a 28-second anoxic zone and a 29-second aerobic zone.
Detailed Description
In order to better understand the above technical solutions, the following detailed description will be given with reference to the accompanying drawings and specific embodiments.
As shown in fig. 1, the present invention provides a multi-mode AAO-MBR process control system, comprising: the control device 3, the monitoring component 4, the AAO biochemical tank 1 and the MBR membrane tank 2, wherein the AAO biochemical tank 1 is communicated with the MBR membrane tank 2;
the AAO biochemical tank 1 comprises an anaerobic zone 25, an anoxic zone and an aerobic zone which are sequentially arranged, wherein the number of the anoxic zone and the aerobic zone is at least two, each anoxic zone and each aerobic zone are alternately arranged, the anoxic zone and the aerobic zone which are adjacent to the anaerobic zone 25 are respectively a first anoxic zone 26 and a first aerobic zone 27, and the anoxic zone and the aerobic zone which are adjacent to the MBR membrane tank 2 are respectively a second anoxic zone 28 and a second aerobic zone 29;
the monitoring component 4 collects the water inflow of the AAO biochemical tank 1 and the sewage parameters of each zone in the AAO biochemical tank 1 and the MBR membrane tank 2;
the control device 3 comprises a processing component 24 and a regulating and controlling component 5, wherein the processing component 24 receives and analyzes the data of the monitoring component 4 and feeds back an adjustment instruction to the regulating and controlling component 5;
the regulation and control assembly 5 comprises a water inlet distribution module, an aeration module, a reflux module, a carbon source module, a dephosphorization agent module and a sludge discharge module, wherein the water inlet distribution module controls water inlet distribution to the anaerobic zone 25 and the first anoxic zone 26, the aeration module controls aeration amount entering each aerobic zone, the reflux module controls the MBR membrane tank 2 to reflux the first aerobic zone 27, the first aerobic zone 27 to the first anoxic zone 26 and the first anoxic zone 26 to the anaerobic zone 25, the carbon source module feeds carbon source to each anoxic zone, the dephosphorization agent module feeds dephosphorization agent to the second aerobic zone 29, and the sludge discharge module controls the MBR membrane tank 2 to discharge sludge.
The monitoring assembly 4 comprises a sludge concentration meter 18, a BOD meter 19, a nitrate nitrogen meter 20, an ammonia nitrogen meter 21 and a dissolved oxygen meter 22. The sludge concentration meter 18 is respectively arranged in the anaerobic zone 25, the first anoxic zone 26, the second anoxic zone 28, the first aerobic zone 27, the second aerobic zone 29 and the MBR membrane tank 2. The BOD meter 19 is disposed in the anaerobic zone 25, and the nitrate nitrogen meter 20 is disposed in the first anoxic zone 26 and the first aerobic zone 27. The ammonia nitrogen meters 21 are arranged in the first aerobic zone 27 and the second aerobic zone 29, and a plurality of ammonia nitrogen meters 21 can be arranged in each aerobic zone. The dissolved oxygen meter 22 is disposed in the first aerobic zone 27 and the second aerobic zone 29.
The carbon source adding assembly 15 comprises a carbon source storage tank and two paths of carbon source adding pipelines, wherein a carbon source adding pump, an electromagnetic valve flowmeter and an automatic control valve are arranged, and the two paths of carbon source adding pipelines are respectively communicated with the first anoxic zone 26 and the second anoxic zone 28.
The dephosphorization agent feeding assembly 16 comprises a dephosphorization agent storage tank and a dephosphorization agent feeding pipeline, wherein the dephosphorization agent storage tank is provided with a dephosphorization agent feeding pump, an electromagnetic valve flowmeter and a self-control valve, and the dephosphorization agent feeding pipeline is communicated with the middle section of the second aerobic zone 29.
The starting end of the sludge pump 17 is connected with a sludge accumulation groove at the tail end of the MBR membrane tank 2, and the tail end of the sludge pump 17 is communicated with the sludge storage tank. An MBR membrane module 23 is arranged in the MBR membrane tank 2 and is used for realizing mud-water separation. When the sludge concentration of the membrane tank is more than 12g/L or the average water pressure variation of the MBR membrane module 23 for continuous 24 hours is more than 4kPa, the sludge discharge module starts the sludge discharge pump 17 until the sludge concentration of the membrane tank is recovered to 8-10g/L and the water pressure is recovered to be normal.
The water inflow distribution components in the AAO biochemical tank 1 realize water inflow distribution of the anaerobic zone 25 and the first anoxic zone 26 through the intelligent water distribution weir 6. The blast aeration assembly comprises a blast blower 7, an aeration pipeline (not shown in the figure), a pressure transmitter 8, a thermal type gas flowmeter 10 and an electric air regulating valve 9, wherein the blast blower 7 is connected with the aeration pipeline, the aeration pipeline is provided with the pressure transmitter 8, the thermal type gas flowmeter 10 and the electric air regulating valve 9, and the tail end of the aeration pipeline is communicated with a first aerobic zone 27 and a second aerobic zone 29. The reflux in the AAO biochemical tank 1 is divided into three levels altogether, wherein the first level is that the MBR membrane tank 2 flows back to the first aerobic zone reflux pump 11 through the MBR membrane tank to enter the first aerobic zone 27, the second level is that the first aerobic zone 27 flows back to the first anoxic zone reflux pump 12 through the first aerobic zone 27 to enter the first anoxic zone 26, and the third level is that the first anoxic zone 26 flows back to enter the first anoxic zone 26 through the first anoxic zone 26 to the anaerobic zone reflux pump 13. The reflux of each stage is provided with a corresponding flow meter 14.
Wherein BOD/TP in the anaerobic zone is more than or equal to 17, BOD/TN in the anoxic zone is more than or equal to 4, the water inlet ratio of the anaerobic zone is 50% -70%, the reflux ratio of the first anoxic zone to the anaerobic zone is 100% -200%, the reflux ratio of the first aerobic zone to the first anoxic zone is 300% -500%, and the reflux ratio of the MBR membrane tank 2 to the first aerobic zone is 400% -600%. Wherein BOD is biochemical oxygen demand, TP is total phosphorus, namely the sum of phosphorus in inorganic state and organic state in sewage, and TN is total nitrogen, namely the sum of nitrogen in inorganic state and organic state in sewage.
The sewage parameters of each zone in the AAO biochemical tank 1 comprise the inlet BOD concentration of the AAO biochemical tank 1, the concentration and total phosphorus concentration of sludge mixed liquor discharged by the AAO-MBR, the residual sludge discharged by the AAO-MBR, the outlet BOD concentration of the anaerobic zone, the reflux ratio of the first anoxic zone to the anaerobic zone, the outlet nitrate nitrogen concentration of the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the C/N value of the first anoxic zone, the carbon source adding concentration of the first anoxic zone and the denitrification rate of the first anoxic zone;
the water inlet distribution module controls water inlet distribution to the anaerobic zone 25 and the first anoxic zone 26, and specifically comprises:
the processing component 24 receives and analyzes the inflow water flow of the AAO biochemical tank, the inflow BOD concentration of the AAO biochemical tank, the concentration and total phosphorus concentration of the sludge mixed solution discharged by the AAO-MBR, the residual sludge discharged by the AAO-MBR, the outflow BOD concentration of the anaerobic zone, the reflux ratio of the first anoxic zone to the anaerobic zone, the outflow nitrate nitrogen concentration of the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the C/N value of the first anoxic zone and the carbon source adding concentration of the first anoxic zone, and feeds back an adjustment instruction to the inflow water distribution module to control the inflow water distribution proportion to the anaerobic zone 25 and the first anoxic zone 26.
The relationship formula for controlling the distribution ratio of water to the anaerobic zone 25 and the first anoxic zone 26 is as follows:
β 2 ＝1-β 1
wherein beta is 1 To distribute the proportion of water into the anaerobic zone, alpha 1 P is the total phosphorus concentration of the sludge mixed solution discharged by the AAO-MBR and is the phosphorus content in the sludge in the anaerobic zone 0 The total phosphorus concentration of supernatant liquid in the sludge mixed solution discharged by AAO-MBR, X 0 For the concentration of the sludge mixed solution discharged by the AAO-MBR, delta X is the residual sludge discharged by the AAO-MBR, R 3 The reflux ratio of the first anoxic zone to the anaerobic zone is Q is the inflow water flow of the AAO biochemical tank, Z 0 BOD concentration, Z of the inflow water of the AAO biochemical tank 1-go out BOD concentration, X of effluent from anaerobic zone 2-1 The concentration of nitrate nitrogen in the effluent water of the first anoxic zone, f is the C/N value of the first anoxic zone, beta 2 To distribute the proportion of water into the first anoxic zone, X 3-1 R is the concentration of nitrate nitrogen in the effluent water of the first aerobic zone 2 Z is the reflux ratio of the first aerobic zone to the first anoxic zone External throwing 1 Adding concentration E into the carbon source of the first anoxic zone 1 For the denitrification rate of the first anoxic zone, H is the carbon source deficiency coefficient, and when f is more than or equal to 4, H=0, and when f is less than 4, H=1-f/4.
When the actual carbon source is added for regulation and control, factors such as the volume, the residence time and the like of the anoxic zone are fully considered, and an upper limit alarm value for removing the nitrate nitrogen in the current state of the anoxic zone is set, so that the waste of the carbon source is avoided.
The anaerobic zone is divided into two areas, and the sewage parameters of each area in the AAO biochemical tank and the MBR membrane tank further comprise TN concentration of the AAO-MBR effluent, reflux ratio of the MBR membrane tank to the first aerobic zone, nitrate nitrogen concentration of the effluent of the second aerobic zone, ammonia nitrogen concentration of the effluent of the second aerobic zone, denitrification rate of the second anaerobic zone, nitrate nitrogen concentration of the effluent of the anaerobic zone, volume of the first anaerobic zone, sludge concentration of the first anaerobic zone, decarburization speed of the first anaerobic zone and design temperature of the first anaerobic zone.
The carbon source module adds the carbon source to each anoxic zone, and specifically comprises:
the processing component receives the TN concentration of the AAO-MBR effluent collected by the monitoring component, analyzes the relation between the TN concentration of the AAO-MBR effluent and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank, and has the following relation formula:
if the TN concentration of the AAO-MBR effluent is higher than a preset value, feeding back an adjustment instruction to the carbon source module, and controlling the carbon source feeding to the first anoxic zone and the second anoxic zone, wherein the method specifically comprises the following steps:
the TN concentration of the AAO-MBR effluent is higher than a preset value, ifAdding carbon source into the first anoxic zone, if ∈10->The carbon source in the first anoxic zone is judged to be sufficient, and R can be automatically increased 2 And f is close to 4, so that the utilization rate of the carbon source is improved.
Determining the amount of carbon source added to the first anoxic zone by analyzing the concentration of the nitric oxide in the first anoxic zone, wherein the relationship formula between the concentration of the nitric oxide in the first anoxic zone and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank is as follows:
determining the carbon source adding amount to the second anoxic zone by combining a TN concentration relation formula of the AAO-MBR effluent and a set denitrification rate of the second anoxic zone;
the second anoxic zone lacks a carbon source provided by the inlet water, mainly uses endogenous metabolites to carry out denitrification, and the inlet water nitrate nitrogen concentration is the outlet water nitrate nitrogen concentration X of the first aerobic zone 3-1 The method comprises the steps of carrying out a first treatment on the surface of the The second anoxic zone is endogenous only, E 2 Typically 25%; e after adding external carbon source 2 The value of (2) is changed along with the change of the value of C/N in the second anoxic zone, such as C/N=2, E in the second anoxic zone 2 Taking a value of 0.3-0.4, E when C/N=3 in the second anoxic zone 2 Taking a value of 0.4-0.6, E when C/N=3.5 in the second anoxic zone 2 The value is 0.6-0.7.
Wherein Y is TN TN concentration, X of AAO-MBR effluent 5-1 The concentration of the nitrate nitrogen in the effluent water of the second aerobic zone is Y 5-2 advances Ammonia nitrogen concentration of the second aerobic zone, E 2 For the denitrification rate of the second anoxic zone, beta 2 To distribute the proportion of water into the first anoxic zone, X 3-1 R is the concentration of nitrate nitrogen in the effluent water of the first aerobic zone 2 Z is the reflux ratio of the first aerobic zone to the first anoxic zone 0 BOD concentration, X of inflow water of AAO biochemical tank 2-1 in The concentration of nitrate nitrogen and X of the inlet water of the first anoxic zone 1-1 The nitrate nitrogen concentration in the effluent of the anaerobic zone can be theoretically considered as 0, beta 1 In order to distribute the water into the anaerobic zone, Q is the water inflow of the AAO biochemical tank, V A1 Is the first defectVolume of oxygen zone, S A1 For the sludge concentration of the first anoxic zone, R 1 For the reflux ratio of the MBR membrane pool to the first aerobic zone, R 2 R is the reflux ratio of the first aerobic zone to the first anoxic zone 3 K is the reflux ratio of the first anoxic zone to the anaerobic zone de(20) Is the denitrification rate at 20 ℃, and T is the design temperature of the AAO biochemical tank and the MBR membrane tank.
Considering that excessive carbon sources can exist in each anoxic zone, organic matters penetrate into the aerobic zone at the rear end, and the aeration quantity of the aerobic zone is used for oxidizing the organic matters preferentially, so that the related data of dissolving poplar in the aerobic zone still needs to be regulated and controlled in time.
The sewage parameters of each zone in the AAO biochemical tank 1 and the MBR membrane tank 2 comprise the reflux ratio of the MBR membrane tank to the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the ammonia nitrogen concentration of the first aerobic zone water inlet, the ammonia nitrogen concentration of the first aerobic zone water outlet and the microbial biomass of the first aerobic zone water outlet, the ammonia nitrogen concentration of the second aerobic zone water inlet, the ammonia nitrogen concentration of the second aerobic zone water outlet and the microbial biomass of the second aerobic zone water outlet, the water TP concentration of the AAO biochemical tank, the residual sludge discharged by the AAO biochemical tank 1 and the phosphorus content in the sludge of the second aerobic zone;
the aeration module controls the aeration quantity entering each aerobic zone, and specifically comprises the following steps:
the processing component 24 receives and analyzes the AAO biochemical tank water inflow rate, the backflow ratio of the MBR membrane tank to the first aerobic zone, the backflow ratio of the first aerobic zone to the first anoxic zone, the first aerobic zone water inflow ammonia nitrogen concentration, the first aerobic zone water outlet ammonia nitrogen concentration and the first aerobic zone water outlet microorganism amount acquired by the monitoring component 4, and feeds back an adjustment instruction to the aeration module to control the aeration amount to the first aerobic zone;
the processing component 24 receives and analyzes the AAO biochemical tank water inflow rate, the backflow ratio of the MBR membrane tank to the first aerobic zone, the second aerobic zone water inlet ammonia nitrogen concentration, the second aerobic zone water outlet ammonia nitrogen concentration and the second aerobic zone water outlet microorganism amount acquired by the monitoring component 4, and feeds back an adjustment instruction to the aeration module to control the aeration amount to the second aerobic zone;
the biological phosphorus removal is realized mainly by removing phosphorus-rich sludge, and the phosphorus content and the sludge discharge amount of the phosphorus-rich sludge have great influence on the biological phosphorus removal.
The dephosphorization reagent module adds a dephosphorization reagent to the second aerobic zone 29, and specifically includes:
the processing component 24 receives and analyzes the AAO biochemical tank water inflow flow, the AAO biochemical tank water inflow TP concentration, the AAO biochemical tank water outflow TP concentration, the residual sludge discharged by the AAO biochemical tank and the phosphorus content in the sludge in the second aerobic zone, and feeds back an adjustment instruction to the phosphorus removal agent module to control the addition of the phosphorus removal agent to the second aerobic zone.
The relation formula for controlling the aeration quantity to the first aerobic zone is as follows:
O 1 oxygen ＝0.00457(1+R 1 +R 2 )Q(Y 3-2 advances -Y 3-2 )-0.548△M V2
The relation formula for controlling the aeration amount to the second aerobic zone is as follows:
O 2 oxygen ＝0.00457(1+R 1 )Q(Y 5-2 advances -Y 5-2 )-0.548△M V3
Wherein Q is the inflow water flow of an AAO biochemical tank, R 1 For the reflux ratio of the MBR membrane pool to the first aerobic zone, R 2 For the reflux ratio of the first aerobic zone to the first anoxic zone, O 1 oxygen O is the aeration quantity of the first aerobic zone 2 oxygen Is the aeration quantity of the second aerobic zone, Y 3-2 advances The ammonia nitrogen concentration of the water entering the first aerobic zone, Y 3-2 The ammonia nitrogen concentration of the effluent of the first aerobic zone, Y 5-2 advances The ammonia nitrogen concentration of the water entering the second aerobic zone is Y 5-2 The ammonia nitrogen concentration of the effluent water of the second aerobic zone, delta M v2 For the water microbial mass of the first aerobic zone, deltaM v3 The microbial biomass of the second aerobic zone.
Considering that excessive carbon sources are added in each anoxic zone, organic matters penetrate into the aerobic zone, and the aeration quantity of the aerobic zone preferentially oxidizes the organic matters, so that the dissolved oxygen data of the aerobic zone still needs to be timely regulated and controlled; the minimum accuracy of the aeration intelligent control system for regulating and controlling the aeration quantity is regulated and controlled according to the air-water ratio of 0.5:1, namely the air quantity is regulated and controlled according to the 0.5:1 of increasing or reducing N times.
The relation formula for controlling the addition of the dephosphorization reagent to the second aerobic zone is as follows:
wherein M is Dephosphorization In order to add the total amount of the dephosphorization reagent to the second aerobic zone, Q is the inflow water flow of the AAO biochemical tank, alpha 2 For the phosphorus content in the sludge of the second aerobic zone, deltaX is the residual sludge discharged by AAO-MBR, gamma is the adding mole ratio of the dephosphorization agent, delta is the effective content of Al salt in the dephosphorization agent, TP Feeding in And TP Out of Respectively the concentrations of inflow and outflow water TP of the AAO biochemical tank.
As shown in fig. 2, the present invention further provides a multi-mode AAO-MBR process control method, which adopts the multi-mode AAO-MBR process control system as described above, and specifically includes the following steps:
starting a multi-mode AAO-MBR process control system;
the monitoring component 4 collects the water inflow of the AAO biochemical tank 1 and the sewage parameters of each area in the AAO biochemical tank 1;
the processing component 24 receives and analyzes the data of the monitoring component 4, and feeds back an adjustment instruction to the regulating and controlling component 5, so that the sewage parameters of the AAO biochemical tank 1 are maintained in a preset interval.
In a specific embodiment, the relevant parameters are set, and the designed sewage treatment scale is 60000m 3 And/d, the BOD of the inflow water of the AAO biochemical tank is 150mg/L, the TN is 60mg/L, the TP is 5mg/L, the SS is 180mg/L, the TN of the outflow water of the MBR membrane tank is less than or equal to 15mg/L, the TP is less than or equal to 0.5mg/L, the nitrification rate of the aerobic zone is=90% under ideal conditions, and E is sufficient when the carbon is sufficient 1 ＝80％，E 2 =25%, BOD removal rate of 80% in anaerobic zone and first anoxic zone, phosphorus content alpha in sludge of anaerobic zone and first anoxic zone is 1.5%, R 1 ＝400％、R 2 ＝400％、R 3 ＝100％。
TN is total nitrogen, and all nitrogen-containing compounds in the water body. SS is the concentration of solid suspended matter, E 2 Is a second anoxic zoneDenitrification rate.
Through preliminary calculation, the residual sludge discharged by AAO-MBR is DeltaX= 10162.935kg/d, the phosphorus discharge amount of an MBR membrane tank is 152.44kg/d, and when a carbon source and a phosphorus removal agent are not added initially, water beta is fed into an anaerobic zone 1 65% of the water beta entering the first anoxic zone 2 35 percent, calculated TN of the effluent is 12.5mg/L, and the concentration X of the nitrate nitrogen in the effluent of the first aerobic zone 3-1 15.53mg/L, and the concentration X of the nitrate nitrogen in the effluent water of the first anoxic zone 2-1 The TP concentration of effluent water of the MBR membrane tank is 2.5mg/L and is 8.16 mg/L. At this time, the effluent TN and TP do not reach the standard, and operation regulation and control are needed;
according to the along-the-way water quality data, the C/N=1.06 of the first anoxic zone is calculated, the carbon source deficiency coefficient is 0.74, and the carbon source is seriously deficient. According to calculation, when the carbon source adding amount of the first anoxic zone is 3960kg/d and the water inlet proportion is not changed, the water outlet TN is 8.8mg/L. The adding amount of the dephosphorization agent is 2961.3kg/d according to the 10 percent PAC solution; however, after calculation and comprehensive iterative analysis, the optimal adjustment measure is that the water inlet beta of the anaerobic zone 1 50% of the water beta entering the first anoxic zone 2 50%, the adding amount of the dephosphorization agent is unchanged, the adding amount of the carbon source can be reduced to 3240kg/d, and the TN of the effluent is still 8.8mg/L;
according to the change of the along-path ammonia nitrogen concentration, the oxygen demand of the first aerobic zone is 525.9kg/h, and the oxygen demand of the second aerobic zone is 29.8kg/h.
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the invention. It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof.
Claims (10)
1. A multi-mode AAO-MBR process control system, comprising: the system comprises control equipment, a monitoring assembly, an AAO biochemical tank and an MBR membrane tank, wherein the AAO biochemical tank is communicated with the MBR membrane tank;
the AAO biochemical tank comprises an anaerobic zone, an anoxic zone and an aerobic zone which are sequentially arranged, wherein the number of the anoxic zone and the aerobic zone is at least two, each anoxic zone is arranged in a crossing way with each aerobic zone, the anoxic zone and the aerobic zone which are adjacent to the anaerobic zone are respectively a first anoxic zone and a first aerobic zone, and the anoxic zone and the aerobic zone which are adjacent to the MBR membrane tank are respectively a second anoxic zone and a second aerobic zone;
the monitoring component collects the water inflow of the AAO biochemical tank and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank;
the control equipment comprises a processing component and a regulating and controlling component, wherein the processing component receives and analyzes the data of the monitoring component and feeds back an adjustment instruction to the regulating and controlling component;
the regulation and control assembly comprises a water inlet distribution module, an aeration module, a reflux module, a carbon source module, a dephosphorization medicament module and a sludge discharge module, wherein the water inlet distribution module controls water inlet distribution to the anaerobic zone and the first anoxic zone, the aeration module controls aeration amount entering each aerobic zone, the reflux module controls the MBR membrane pond to flow back to the first aerobic zone, the first aerobic zone to the first anoxic zone and the first anoxic zone to the anaerobic zone, the carbon source module feeds a carbon source to each anoxic zone, the dephosphorization medicament module feeds a dephosphorization medicament to the second aerobic zone, and the sludge discharge module controls the MBR membrane pond to discharge sludge.
2. The multi-mode AAO-MBR process control system of claim 1, wherein BOD/TP in the anaerobic zone is greater than or equal to 17, BOD/TN in the anoxic zone is greater than or equal to 4, the anaerobic zone has a water inlet ratio of 50% -70%, a reflux ratio of the first anoxic zone to the anaerobic zone is 100% -200%, a reflux ratio of the first aerobic zone to the first anoxic zone is 300% -500%, and a reflux ratio of the MBR membrane pool to the first aerobic zone is 400% -600%.
3. The multi-mode AAO-MBR process control system of claim 1 or 2, wherein the wastewater parameters of each zone in the AAO biochemical tank comprise an AAO biochemical tank inlet BOD concentration, an AAO-MBR discharged sludge mixed liquor concentration and total phosphorus concentration, an AAO-MBR discharged residual sludge amount, an anaerobic zone outlet BOD concentration, a reflux ratio of the first anoxic zone to the anaerobic zone, a first aerobic zone outlet nitrate nitrogen concentration, a reflux ratio of the first aerobic zone to the first anoxic zone, a first anoxic zone C/N value, a first anoxic zone carbon source addition concentration and a first anoxic zone denitrification rate;
the water inlet distribution module controls water inlet distribution to the anaerobic zone and the first anoxic zone, and specifically comprises the following steps:
the treatment component receives and analyzes the water inflow flow of the AAO biochemical tank, the water inflow BOD concentration of the AAO biochemical tank, the sludge mixed liquor concentration and the total phosphorus concentration discharged by the AAO-MBR, the residual sludge quantity discharged by the AAO-MBR, the water outflow BOD concentration of the anaerobic zone, the reflux ratio of the first anoxic zone to the anaerobic zone, the water nitrate nitrogen concentration discharged by the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the C/N value of the first anoxic zone and the carbon source adding concentration of the first anoxic zone, and feeds back an adjustment instruction to the water inflow distribution module to control the water inflow distribution ratio to the anaerobic zone and the first anoxic zone.
4. The multi-mode AAO-MBR process control system of claim 3 wherein the relationship equation controlling the ratio of water distribution to the anaerobic zone and the first anoxic zone is as follows:
β 2 ＝1-β 1
wherein beta is 1 To distribute the proportion of water into the anaerobic zone, alpha 1 P is the total phosphorus concentration of the sludge mixed solution discharged by the AAO-MBR and is the phosphorus content in the sludge in the anaerobic zone 0 The total phosphorus concentration of supernatant liquid in the sludge mixed solution discharged by AAO-MBR, X 0 For the concentration of the sludge mixed solution discharged by the AAO-MBR, delta X is the residual sludge discharged by the AAO-MBR, R 3 The reflux ratio of the first anoxic zone to the anaerobic zone is Q is the inflow water flow of the AAO biochemical tank, Z 0 BOD concentration, Z of the inflow water of the AAO biochemical tank 1-go out BOD concentration, X of effluent from anaerobic zone 2-1 The concentration of nitrate nitrogen in the effluent water of the first anoxic zone, f is the C/N value of the first anoxic zone, beta 2 To distribute the proportion of water into the first anoxic zone, X 3-1 R is the concentration of nitrate nitrogen in the effluent water of the first aerobic zone 2 Z is the reflux ratio of the first aerobic zone to the first anoxic zone External throwing 1 Adding concentration E into the carbon source of the first anoxic zone 1 For the denitrification rate of the first anoxic zone, H is the carbon source deficiency coefficient, and when f is more than or equal to 4, H=0, and when f is less than 4, H=1-f/4.
5. The multi-mode AAO-MBR process control system of claim 3, wherein the number of anoxic zones is two, and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank further comprise a TN concentration of the AAO-MBR effluent, a reflux ratio of the MBR membrane tank to the first aerobic zone, a nitrate nitrogen concentration of the effluent of the second aerobic zone, an ammonia nitrogen concentration of the influent of the second aerobic zone, a denitrification rate of the second anoxic zone, a nitrate nitrogen concentration of the effluent of the anaerobic zone, a volume of the first anoxic zone, a sludge concentration of the first anoxic zone, a decarburization rate of the first anoxic zone, and a design temperature of the first anoxic zone.
6. The multi-mode AAO-MBR process control system of claim 5, wherein the carbon source module adds a carbon source to each anoxic zone, comprising:
the processing component receives the TN concentration of the AAO-MBR effluent collected by the monitoring component, analyzes the relation between the TN concentration of the AAO-MBR effluent and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank, and has the following relation formula:
if the TN concentration of the AAO-MBR effluent is higher than a preset value, feeding back an adjustment instruction to the carbon source module, and controlling the carbon source feeding to the first anoxic zone and the second anoxic zone, wherein the method specifically comprises the following steps:
the TN concentration of the AAO-MBR effluent is higher than a preset value, ifAdding carbon source into the first anoxic zone;
determining the amount of carbon source added to the first anoxic zone by analyzing the concentration of the nitric oxide in the first anoxic zone, wherein the relationship formula between the concentration of the nitric oxide in the first anoxic zone and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank is as follows:
determining the carbon source adding amount to the second anoxic zone by combining a TN concentration relation formula of the AAO-MBR effluent and a set denitrification rate of the second anoxic zone;
wherein Y is TN TN concentration, X of AAO-MBR effluent 5-1 The concentration of the nitrate nitrogen in the effluent water of the second aerobic zone is Y 5-2 advances Ammonia nitrogen concentration of the second aerobic zone, E 2 For the denitrification rate of the second anoxic zone, beta 2 To distribute the proportion of water into the first anoxic zone, X 3-1 R is the concentration of nitrate nitrogen in the effluent water of the first aerobic zone 2 Z is the reflux ratio of the first aerobic zone to the first anoxic zone 0 BOD concentration, X of inflow water of AAO biochemical tank 2-1 in The concentration of nitrate nitrogen and X of the inlet water of the first anoxic zone 1-1 The concentration of nitrate nitrogen and beta of effluent water of an anaerobic zone 1 In order to distribute the water into the anaerobic zone, Q is the water inflow of the AAO biochemical tank, V A1 For the volume of the first anoxic zone, S A1 For the sludge concentration of the first anoxic zone, R 1 For the reflux ratio of the MBR membrane pool to the first aerobic zone, R 2 R is the reflux ratio of the first aerobic zone to the first anoxic zone 3 K is the reflux ratio of the first anoxic zone to the anaerobic zone de(20) Is the denitrification rate at 20 ℃, and T is the design temperature of the AAO biochemical tank and the MBR membrane tank.
7. The multi-mode AAO-MBR process control system of claim 1 or 2, wherein the number of aerobic zones is two, and the sewage parameters of each zone in the AAO biochemical tank and the MBR membrane tank comprise a reflux ratio of the MBR membrane tank to the first aerobic zone, a reflux ratio of the first aerobic zone to the first anoxic zone, a first aerobic zone influent ammonia nitrogen concentration, a first aerobic zone effluent ammonia nitrogen concentration, and a first aerobic zone effluent microorganism amount, a second aerobic zone influent ammonia nitrogen concentration, a second aerobic zone effluent ammonia nitrogen concentration, and a second aerobic zone effluent microorganism amount, an AAO biochemical tank influent TP concentration, an AAO biochemical tank effluent TP concentration, an AAO-MBR effluent residual sludge amount, and a second aerobic zone sludge phosphorus content;
the aeration module controls the aeration quantity entering each aerobic zone, and specifically comprises the following steps:
the treatment assembly receives and analyzes the water inflow rate of the AAO biochemical tank, the reflux ratio of the MBR membrane tank to the first aerobic zone, the reflux ratio of the first aerobic zone to the first anoxic zone, the water inflow ammonia nitrogen concentration of the first aerobic zone, the water outflow ammonia nitrogen concentration of the first aerobic zone and the water outflow microbial biomass of the first aerobic zone, and feeds back an adjustment instruction to the aeration module to control the aeration amount to the first aerobic zone;
the treatment assembly receives and analyzes the AAO biochemical tank water inflow rate, the backflow ratio of the MBR membrane tank to the first aerobic zone, the second aerobic zone water inflow ammonia nitrogen concentration, the second aerobic zone water outlet ammonia nitrogen concentration and the second aerobic zone water outlet microbial biomass acquired by the monitoring assembly, and feeds back an adjustment instruction to the aeration module to control the aeration amount to the second aerobic zone;
the dephosphorization reagent module adds the dephosphorization reagent to the second aerobic zone, and specifically comprises:
the treatment component receives and analyzes the AAO biochemical tank water inflow flow, the AAO biochemical tank water inflow TP concentration, the AAO biochemical tank water outflow TP concentration, the AAO-MBR discharged surplus sludge quantity and the phosphorus content in the sludge of the second aerobic zone, and feeds back an adjustment instruction to the phosphorus removal agent module to control the addition of the phosphorus removal agent to the second aerobic zone.
8. The multi-mode AAO-MBR process control system of claim 7 wherein the relationship equation governing aeration to the first aerobic zone is as follows:
O 1 oxygen ＝0.00457(1+R 1 +R 2 )Q(Y 3-2 advances -Y 3-2 )-0.548△M V2
The relation formula for controlling the aeration amount to the second aerobic zone is as follows:
O 2 oxygen ＝0.00457(1+R 1 )Q(Y 5-2 advances -Y 5-2 )-0.548△M V3
Wherein Q is the inflow water flow of an AAO biochemical tank, R 1 For the reflux ratio of the MBR membrane pool to the first aerobic zone, R 2 For the reflux ratio of the first aerobic zone to the first anoxic zone, O 1 oxygen O is the aeration quantity of the first aerobic zone 2 oxygen Is the aeration quantity of the second aerobic zone, Y 3-2 advances The ammonia nitrogen concentration of the water entering the first aerobic zone, Y 3-2 The ammonia nitrogen concentration of the effluent of the first aerobic zone, Y 5-2 advances The ammonia nitrogen concentration of the water entering the second aerobic zone is Y 5-2 The ammonia nitrogen concentration of the effluent water of the second aerobic zone, delta M v2 For the water microbial mass of the first aerobic zone, deltaM v3 The microbial biomass of the second aerobic zone.
9. The multi-mode AAO-MBR process control system of claim 7 wherein controlling the addition of the dephosphorization agent to the second aerobic zone is formulated as follows:
wherein M is Dephosphorization In order to add the total amount of the dephosphorization reagent to the second aerobic zone, Q is the inflow water flow of the AAO biochemical tank, alpha 2 For the phosphorus content in the sludge of the second aerobic zone, deltaX is the residual sludge discharged by AAO-MBR, gamma is the adding mole ratio of the dephosphorization agent, delta is the effective content of Al salt in the dephosphorization agent, TP Feeding in And TP Out of Respectively the concentrations of inflow and outflow water TP of the AAO biochemical tank.
10. A multi-mode AAO-MBR process control method, characterized by adopting the multi-mode AAO-MBR process control system according to any one of claims 1-9, comprising the following specific steps:
starting a multi-mode AAO-MBR process control system;
the monitoring component collects the water inflow of the AAO biochemical tank and the sewage parameters of each area in the AAO biochemical tank;
the processing component receives and analyzes the data of the monitoring component, and feeds back an adjustment instruction to the regulation and control component, so that the sewage parameters of the AAO biochemical tank are maintained in a preset interval.
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