CN109851154A - A2/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus and its control method - Google Patents
A2/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus and its control method Download PDFInfo
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- CN109851154A CN109851154A CN201811584402.5A CN201811584402A CN109851154A CN 109851154 A CN109851154 A CN 109851154A CN 201811584402 A CN201811584402 A CN 201811584402A CN 109851154 A CN109851154 A CN 109851154A
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 81
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 239000011574 phosphorus Substances 0.000 title claims abstract description 76
- 238000000034 method Methods 0.000 title claims abstract description 70
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 60
- 238000011084 recovery Methods 0.000 title claims abstract description 58
- 239000010802 sludge Substances 0.000 claims abstract description 72
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 230000008569 process Effects 0.000 claims abstract description 26
- 238000000855 fermentation Methods 0.000 claims abstract description 16
- 230000004151 fermentation Effects 0.000 claims abstract description 16
- 239000010865 sewage Substances 0.000 claims abstract description 14
- 239000011777 magnesium Substances 0.000 claims abstract description 11
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 claims abstract description 9
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 62
- 159000000003 magnesium salts Chemical class 0.000 claims description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 42
- 239000000243 solution Substances 0.000 claims description 37
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 33
- 230000003647 oxidation Effects 0.000 claims description 29
- 238000007254 oxidation reaction Methods 0.000 claims description 29
- 239000012266 salt solution Substances 0.000 claims description 25
- 238000003860 storage Methods 0.000 claims description 22
- 238000004062 sedimentation Methods 0.000 claims description 21
- 239000000945 filler Substances 0.000 claims description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 238000007667 floating Methods 0.000 claims description 8
- 239000004743 Polypropylene Substances 0.000 claims description 7
- -1 polypropylene Polymers 0.000 claims description 7
- 229920001155 polypropylene Polymers 0.000 claims description 7
- 239000006228 supernatant Substances 0.000 claims description 7
- 230000001376 precipitating effect Effects 0.000 claims description 6
- 230000001360 synchronised effect Effects 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 208000037534 Progressive hemifacial atrophy Diseases 0.000 claims description 5
- 238000005273 aeration Methods 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 238000012017 passive hemagglutination assay Methods 0.000 claims description 5
- 229920000903 polyhydroxyalkanoate Polymers 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 206010021143 Hypoxia Diseases 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 3
- 230000007954 hypoxia Effects 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- 230000033116 oxidation-reduction process Effects 0.000 claims description 3
- 230000002093 peripheral effect Effects 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 2
- 239000000725 suspension Substances 0.000 claims description 2
- 230000001546 nitrifying effect Effects 0.000 claims 1
- 238000004064 recycling Methods 0.000 abstract description 11
- 230000000694 effects Effects 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 4
- 230000009467 reduction Effects 0.000 abstract description 3
- 230000007547 defect Effects 0.000 abstract 1
- 229910052567 struvite Inorganic materials 0.000 abstract 1
- YUWBVKYVJWNVLE-UHFFFAOYSA-N [N].[P] Chemical compound [N].[P] YUWBVKYVJWNVLE-UHFFFAOYSA-N 0.000 description 9
- 238000012545 processing Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- 229920000388 Polyphosphate Polymers 0.000 description 1
- 229920000037 Polyproline Polymers 0.000 description 1
- GCXJOXWDAVFSAF-UHFFFAOYSA-N [Pb].[P].[N] Chemical compound [Pb].[P].[N] GCXJOXWDAVFSAF-UHFFFAOYSA-N 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000010840 domestic wastewater Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- DJFBJKSMACBYBD-UHFFFAOYSA-N phosphane;hydrate Chemical compound O.P DJFBJKSMACBYBD-UHFFFAOYSA-N 0.000 description 1
- 239000001205 polyphosphate Substances 0.000 description 1
- 235000011176 polyphosphates Nutrition 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000009938 salting Methods 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
本发明涉及A2/O‑BCO工艺氮磷回收实时控制装置及其控制方法，属于活性污泥法污水处理技术领域。本发明针对A2/O工艺固有缺陷、BCO的优点和磷资源回收的需求，将A2/O‑BCO双污泥系统与污泥发酵回收氮磷工艺相结合，在污泥发酵液中加入镁，以鸟粪石形式回收磷，不仅可以减少剩余污泥的产量，而且还能对其进行资源化利用，回收后将得到一种高效缓释肥，既能实现氮磷的同步去除，又能回收污泥中的氮磷资源；实时控制装置让反应更精确，处理效果更稳定，回收效率更高，操作简单，运行管理方便，实现资源的高效回收利用以及污泥减量。
The invention relates to a real-time control device for nitrogen and phosphorus recovery in an A2/O - BCO process and a control method thereof, belonging to the technical field of activated sludge method sewage treatment. Aiming at the inherent defects of the A 2 /O process, the advantages of BCO and the demand for phosphorus resource recovery, the present invention combines the A 2 /O-BCO double sludge system with the process of sludge fermentation to recover nitrogen and phosphorus, and adds in the sludge fermentation liquid. Magnesium, recovering phosphorus in the form of struvite can not only reduce the output of excess sludge, but also make resource utilization of it. It can recover nitrogen and phosphorus resources in sludge; the real-time control device makes the reaction more accurate, the treatment effect is more stable, the recovery efficiency is higher, the operation is simple, the operation and management are convenient, and the efficient recycling of resources and sludge reduction can be achieved.
Description
Technical field
The present invention relates to A2/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus and its control method, belong to activated sludge process
Technical field of sewage, suitable for the processing of sanitary sewage, the recycling field of nitrogen phosphor resource.
Background technique
The excessive emissions of the elements such as nitrogen phosphorus lead to the major reason of water eutrophication, it is raw to industrial and agricultural production and the people
Living constitute seriously threatens.A2/ O has simple structure, hydraulic detention time as simplest synchronous denitrogen dephosphorus technology
It is short, design operation experience is mature, control complexity is small and is not likely to produce the series of advantages such as sludge bulking, be China's town sewage
The main process of factory, but it is unstable due to its synchronous denitrification dephosphorizing performance, need us to change for the deficiency of its technique
It makes and optimizes.
In addition, phosphor resource is the valuable source of industrial and agricultural development.And unlike nitrogen resource, phosphor resource is not to take it
Nexhaustible not to the utmost, phosphorus is a kind of non-renewable resources.Tellurian phosphor resource is limited, and in quality and can be exploited
Property aspect all declining, verified minable phosphate ore and exploited by present coefficient of mining, estimated that lasting exploitation is no more than 100
Year.Therefore, the Sustainable Use Problems of phosphorus are gravely put in face of common people, are realized from the links in production, life
The artificial recycling of phosphorus is at the international hot research problem in terms of environmental and resource management.For sewage treatment, grind
Hair has both the waste water dephosphorization new technology of recycling, extremely urgent.
And process for removing nitrogen and phosphor from sewage is by phosphorus from being transferred in excess sludge in sewage to the removal of phosphorus, although to sewage
In phosphorus have a preferable removal effect, but phosphorus causes the very big wasting of resources with excess sludge disposition, does not meet at present
Minimizing, recycling and the innoxious principle of specific resistance to filtration.
Summary of the invention
Not in place, serious waste of resources is handled for existing excess sludge, recovery of nitrogen and phosphorus low efficiency, utilization rate be not high to ask
Topic, the present invention pass through in A2Increase nitrogen and phosphorus recovery device after/O-BCO technique, proposes a kind of A2/ O-BCO technique recovery of nitrogen and phosphorus system
On the one hand system real-time control apparatus and its control method reduce the discharge of excess sludge, realize sludge reduction；On the other hand high
Nitrogen phosphor resource in effect recycling excess sludge, realizes resource utilization.And the presence of real-time control apparatus, allow fermentation process and nitrogen
Phosphorus removal process is more controllable, ensure that the high efficiente callback of resource, also significantly reduces the burden of operation, operation and management.
Technical scheme is as follows:
A2/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that including raw water water tank, A2/ O reactor, centre
Sedimentation basin, phosphorus recovery system, intermediate water tank, goes out water tank, real-time control system, the real-time control system packet at BCO reactor
Include computer, process controller；；The phosphorus recovery system include TP sensor, TN sensor, pH sensor, magnesium salts sensor,
Lye adds case, lye adds pump, ammonia nitrogen solution dosing tank, ammonia nitrogen solution add pump, magnesium salt solution dosing tank, magnesium salt solution are thrown
Add storage mud tank, fermentor, the recovery of nitrogen and phosphorus tank, liquid reserve tank of pump and sequential connection；The A2/ O reactor is by anaerobic zone, anoxic
Area and aerobic zone, which are linked in sequence, to be formed, and the BCO reactor includes the biological contact oxidation pond being linked in sequence, settling zone；
The outlet of the raw water water tank and the A2The anaerobic zone of/O reactor is connected, the A2The aerobic zone of/O reactor
It is connected with the import in intermediate sedimentation pond, the water outlet in the intermediate sedimentation pond is connected with the import of intermediate water tank, and the centre is heavy
The mud mouth in shallow lake pond respectively with the A2The anaerobic zone of/O reactor and storage mud tank are connected；The outlet of the intermediate water tank connects
Biological contact oxidation pond, the settling zone are separately connected out water tank, storage mud tank, water tank and the A out2/ O reactor lacks
The connection of oxygen area；
The lye, which adds case and adds to pump with lye by variable-frequency governor I, to be connected, and the lye adds pump, pH sensor
It is all connected to fermentor；The ammonia nitrogen solution dosing tank adds pump with ammonia nitrogen solution by variable-frequency governor II and is connected, the magnesium
Salting liquid dosing tank adds pump with magnesium salt solution by variable-frequency governor III and is connected, and the ammonia nitrogen solution adds pump, magnesium salt solution
Pump, TP sensor, TN sensor, magnesium salts sensor is added to be connected with recovery of nitrogen and phosphorus tank；The TP sensor, TN sensor,
PH sensor, magnesium salts sensor are separately connected computer, and the computer is connected with process controller, the process controller point
It Lian Jie not variable-frequency governor I, variable-frequency governor II, variable-frequency governor III.
Further, which is additionally provided with air blower, the air blower pass through respectively flow meter I, flow meter II with it is aerobic
Area, biological contact oxidation pond are connected, and are respectively arranged with aeration head in aerobic zone, biological contact oxidation pond.
Further, the mud mouth in the intermediate sedimentation pond passes through return sludge pump, mud valve I and the A respectively2/ O is anti-
The anaerobic zone and storage mud tank for answering device are connected.
Further, the settling zone is connected by mud valve IV with storage mud tank.
Further, the fermentor, recovery of nitrogen and phosphorus pot bottom are respectively equipped with mud valve II, mud valve III.
Further, the settling zone is equipped with overflow port, is equipped with polypropylene suspension filler in the biological contact oxidation pond.
Further, the A2Anaerobic zone, the anoxic zone of/O reactor are equipped with blender I, are equipped in the fermentor
Blender III, the recovery of nitrogen and phosphorus tank is interior to be equipped with blender II.
Above-mentioned A2The control method of/O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that the following steps are included:
1) returned sludge that the sanitary sewage in raw water water tank is sent through intake pump and intermediate sedimentation pond through return sludge pump
Enter A together2The anaerobic zone of/O reactor is sufficiently mixed reaction under the action of blender I；
2) anoxic zone is subsequently entered, while being entered completely and solid there are also the BCO reactor nitrification that water tank flows out is gone out
The nitrification liquid of liquid separation；
3) aerobic zone is proceeded immediately to, turn-on flow rate meter I further inhales phosphorus, while the N that stripping denitrification process generates2；
4) mixed liquor of aerobic zone is then entered into intermediate sedimentation pond and carries out mud-water separation, using centre water inlet peripheral effluent
The method of operation；A part of precipitating sludge is set to flow back into A through return sludge pump2The anaerobic zone of/O reactor, remaining sludge are logical
It crosses mud valve I and enters storage mud tank；
5) supernatant in intermediate sedimentation pond enters intermediate water tank, and the biological of BCO reactor is entered through intermediate intake pump
Oxidation pond sets floating stuffing in biological contact oxidation pond, adjusts flow meter II, guarantees that filler be in fluidized state, completion ammonia nitrogen
Oxidation；
6) settling zone of biological contact oxidation pond is subsequently entered, supernatant is discharged through overflow port, into water tank out, falls off
Biomembrane from bottom mud valve IV enter storage mud tank；A part of be discharged enters A through nitrification liquid reflux pump in water tank out2/ O is anti-
The anoxic zone of device is answered, provides electron acceptor, remainder direct emission for denitrification dephosphorization；
7) sludge stored up in mud tank fully enters fermentor, and the pH value in pH sensor online acquisition fermentor passes through meter
The operation of calculation machine, obtains real time control variables, controls variable-frequency governor I by process controller, adjustment lye adds pump and adds
The amount of NaOH solution, so that pH stablizes 10.0；
8) fermentation liquid enters recovery of nitrogen and phosphorus tank after, and TP sensor, TN sensor, magnesium salts sensor online acquisition nitrogen phosphorus return
TP, TN, magnesium salt concentrations in closed cans obtain real time control variables by the operation of computer, control frequency conversion by process controller
Governor II adjustment ammonia nitrogen solution adds the amount for adding ammonia nitrogen solution that pumps, control variable-frequency governor III adjustment magnesium salt solution adds
Pump adds the amount of magnesium salt solution so that N:P:Mg=3:1:1.6 (nitrogen, phosphorus, magnesium molar ratio be 3:1:1.6), it is final to take out life
At guanite, surplus solution enters liquid reserve tank.
Further, in step 1), anaerobic reaction time 1.2h, 8 000mg/L of sludge concentration；Denitrifying Phosphate Accumulating Organisms
(DPAOs) phosphorus is discharged simultaneously using easily biodegradable organics synthesis internal carbon source (PHAs) in raw water, most of organic matter is gone
It removes；
In step 2), hypoxia response time 6.0h, sludge concentration 2500mg/L, DPAOs using PHAs electron donor, with
NO3 -- N is electron acceptor synchronous denitrification dephosphorizing.
Further, in step 3), aerobic reaction time 1.2h, turn-on flow rate meter I guarantee dissolved oxygen 2.0-2.5mg/L,
Oxidation-reduction potential ORP is 50-80mV；
In step 5), the material of floating stuffing is polypropylene, specific surface area 1000m2/m3, filling rate 50~55%；It adjusts
Flow meter II makes dissolved oxygen 3.0-3.5mg/L, guarantees that filler is in fluidized state, hydraulic detention time 2-3h completes ammonia nitrogen
Oxidation；
In step 7), 10 000mg/L-12 000mg/L of sludge concentration, fermentation time 7d in fermentor.
Magnesium is added in sludge fermentation liquid in the present invention, and the method that phosphorus is recycled in the form of guanite (ammonium magnesium phosphate) not only can be with
The yield of excess sludge is reduced, and resource utilization can also be carried out to it, a kind of slow-release fertilizer will be obtained after recycling, finally
Realize the purpose to turn waste into wealth.BCO occupied area is small, and nitrification effect is stablized, and BCO unit cells type is that more cell compartments are thoroughly mixed formula
The pattern combined with pulling flow type is easy to control each section of aeration quantity according to ammonia nitrogen loading, saves operation and maintenance energy from many aspects
Consumption.The present invention is directed to A2The demand of the advantages of/O technique inherent shortcoming, BCO and reclamation of phosphorus resource propose a kind of recovery of nitrogen and phosphorus system
It unites real-time control apparatus and method, the system is by A2The bis- sludge systems of/O-BCO are combined with sludge fermentation recycling nitrogen phosphorus technique,
Not only it had been able to achieve the synchronous removal of nitrogen phosphorus, but also the nitrogen phosphor resource in sludge can be recycled；Real-time control apparatus makes reaction more accurate, processing
Effect is more stable, and recovery efficiency is higher, easy to operate, and operational management is convenient, realizes high efficiente callback utilization and the sludge of resource
Decrement.
The present invention is in A2Increase nitrogen and phosphorus recovery device after/O-BCO technique, the pH value in online acquisition fermentor is adjusted in real time
The dosage of whole NaOH solution reaches best ferment effect so that pH stablizes 10.0 or so；In online acquisition recovery of nitrogen and phosphorus tank
The concentration of TN, TP and magnesium salts, the dosage of real-time control ammonia nitrogen solution and magnesium salt solution, control N, P, Mg molar ratio is 3:
1:1.6 promotes the quality of guanite while improving recovery of nitrogen and phosphorus rate.
The method of the present invention is compared with the prior art, have the advantage that
1) nitrifier of short sludge age polyP bacteria, denitrifying bacterium and long sludge age realizes separation, allows each optimal
It is grown in environment, is conducive to the stabilization of system.
2) technique Prepositive denitrification provides condition for denitrification dephosphorization, realizes " carbon is dual-purpose ", solves low C/N sewage
The problem of middle carbon source lacks.
3) pH value in pH sensor online acquisition fermentor adjusts adding for NaOH in real time, makes the pH value in fermentor
Stable always 10.0 or so guarantee optimal ferment effect.
4) TN sensor, TP sensor, in magnesium salts sensor online acquisition recovery of nitrogen and phosphorus tank TN, TP, magnesium salts concentration, it is real
When adjustment recovery of nitrogen and phosphorus tank in TN and magnesium salts concentration so that the molar ratio of N, P, Mg are maintained at 3:1:1.6, as much as possible time
Receive phosphor resource.
5) real-time control system structure is simple, and precisely, management service is convenient for control, and labor intensity is low.
6) sludge that not only can handle the present apparatus can also handle other sludge, go back while realizing sludge reduction
It is able to achieve recycling.
Detailed description of the invention
Fig. 1 is A2The schematic diagram of/O-BCO technique recovery of nitrogen and phosphorus system real-time control apparatus；
In figure: 1- raw water water tank, 2-A2/ O reactor, 3- intermediate sedimentation pond, 4-BCO reactor, 5- phosphorus recovery system, 6-
Real-time control system, 7- intake pump, the anaerobic zone 8-, the anoxic zone 9-, the aerobic zone 10-, 11- intermediate water tank, the centre 12- intake pump,
13- biological contact oxidation pond, the settling zone 14-, 15- go out water tank, 16- return sludge pump, 17- mud valve I, and 18- stores up mud tank,
19- fermentor, 20- recovery of nitrogen and phosphorus tank, 21- mud valve II, 22- mud valve III, 23- liquid reserve tank, 24- lye add case, 25- ammonia
Nitrogen solution dosing tank, 26- computer, 27- process controller, 28- variable-frequency governor II, 29- variable-frequency governor I, 30-TP sensing
Device, 31-TN sensor, 32-pH sensor, 33- lye add pump, and 34- ammonia nitrogen solution adds pump, 35- flow meter II, and 36- is stirred
Mix device I, 37- nitrification liquid reflux pump, 38- air blower, 39- aeration head, 40- variable-frequency governor III, 41- magnesium salt solution adds pump,
42- magnesium salts sensor, 43- magnesium salt solution dosing tank, 44- mud valve IV, 45- blender II, 46- blender III, 47- flowmeter
Ⅰ。
Specific embodiment
1. as shown in Figure 1, A2/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, raw water water tank 1, A2/ O reactor 2, in
Between sedimentation basin 3, intermediate water tank 11, biological contact oxidation pond 13, settling zone 14, storage mud tank 18, fermentor 19, recovery of nitrogen and phosphorus tank 20
And real-time control system connection composition.
A2/ O reactor 2 is linked in sequence by anaerobic zone 8, anoxic zone 9 and aerobic zone 10 and is formed.A2The anaerobic zone of/O reactor 2
8 and anoxic zone 9 be equipped with blender I 36, aerobic zone 10 and 13 bottom of biological contact oxidation pond are equipped with aeration head 39, lead to respectively
Cross the regulation of air blower 38 and flow meter I 47, the realization of flow meter II 35 to dissolved oxygen.
The partial sludge in intermediate sedimentation pond 3 connects 8 bottom of anaerobic zone by return sludge pump 16, and another part sludge passes through
Mud valve I 17 enters storage mud tank 18, and water outlet enters intermediate water tank 11, squeezes into biological contact oxidation pond by intermediate charging pump 12
13。
Floating stuffing is equipped in biological contact oxidation pond 13, material is polypropylene, by opening air blower 38 and flowmeter
II 35 regulation dissolved oxygens make filler be in fluidized state, and guarantee substrate and microorganism come into full contact with, and main function is to complete ammonia
Nitrogen oxidation.
Settling zone 14 is equipped with overflow port, and bottom is equipped with mud valve IV 44, and connects storage mud tank 18 by pipeline.
Floating stuffing material is polypropylene, specific surface area 1000m in biological contact oxidation pond2/m3, filling rate 50-55%,
Dissolved oxygen 3.0-3.5mg/L, filler are in fluidized state, and hydraulic detention time 2-3h, main function is to complete ammonium oxidation.
Ammonia nitrogen solution dosing tank 25 is connect with variable-frequency governor II 28, and variable-frequency governor II and ammonia nitrogen solution add pump 34 and connect
It connects.Magnesium salt solution dosing tank 43 is connect with variable-frequency governor III 40, and variable-frequency governor III adds pump 41 with magnesium salt solution and connect.pH
Sensor 32, TN sensor 31, TP sensor 30 and magnesium salts sensor 42 are connect with computer 26, variable-frequency governor I, II, III
It is connect with controller.
Sludge in storage mud tank 18 fully enters fermentor 19, is equipped with blender III 46 and pH sensor 32 in fermentor,
Mixing speed 120rmp/min adjusts the pump speed that lye adds pump 33 by variable-frequency governor I 29, controls NaOH dosage.Alkali
The NaOH solution that liquid dosing tank adds 1mol/L adjusts pH, and value control is 10.0 or so, sludge concentration 10000-12000mg/
L, sludge fermentation time 7d.
Lye dosing tank 24 is connect with variable-frequency governor I 29, and variable-frequency governor I adds pump 33 with lye and connect, and controls alkali
Liquid dosage.It is equipped with blender II 45, TN sensor 31, TP sensor 30 and magnesium salts sensor 42 in recovery of nitrogen and phosphorus tank 20, stirs
Mix speed 120rmp/min, mixing time 90min.1g/L is added respectively by ammonia nitrogen solution dosing tank and magnesium salt solution dosing tank
Ammonia nitrogen solution and 1g/L magnesium salt solution so that N:P:Mg=3:1:1.6.
Fermentation liquid enters recovery of nitrogen and phosphorus tank 20, is equipped with blender II 45 in recovery of nitrogen and phosphorus tank, passes through variable-frequency governor II 28
The pump speed that ammonia nitrogen solution adds pump 34 is adjusted, ammonia nitrogen dosage is controlled；Magnesium salt solution is adjusted by variable-frequency governor III 40 to add
The pump speed of pump 41 controls magnesium salts dosage；The guanite formed in recovery of nitrogen and phosphorus tank 20 is recycled by mud valve III, and solution enters
Liquid reserve tank 23.
Sanitary sewage enters A2After/O reactor, completed under the plug-flow effect of anaerobic zone 8, anoxic zone 9, aerobic zone 10 same
Walk denitrogenation dephosphorizing.Mud-water separation is realized in intermediate sedimentation pond 3, obtains supernatant and precipitating sludge respectively, and supernatant, which enters to have, to be hanged
In the BCO reactor 4 of floating filler, the oxidation of ammonia nitrogen is completed under aerobic condition；Nitrification liquid enters settling zone 14 and carries out muddy water again
Separation, the biomembrane to fall off are emitted into storage mud tank 18, and nitrification liquid is back to anoxic zone 9 and provides electron acceptor for denitrification dephosphorization；
The precipitating sludge a part in intermediate sedimentation pond 3 is back to the biomass that anaerobic zone 8 remains stable in reactor, another part precipitating
Mud discharging extremely storage mud tank 18.
Sludge enters fermentor 19 in storage mud tank 18, and the pH value in 32 online acquisition fermentor of pH sensor passes through calculating
The operation of machine 26, obtains real time control variables, controls variable-frequency governor I 29 by process controller 27, adjustment lye adds pump
33 add the amount of NaOH solution, and control carries out sludge fermentation, the nitrogen and phosphorus of dissolution under the conditions of Optimal pH.Fermentation liquid enters nitrogen phosphorus
Recycling can 20, the concentration of TN, TP and magnesium salts in TN, TP, magnesium salts sensor online acquisition recovery of nitrogen and phosphorus tank, passes through computer 26
Operation obtain real time control variables, by process controller 27 control variable-frequency governor II 28 adjust ammonia nitrogen solution add pump
34 add the amount of ammonia nitrogen solution, control variable-frequency governor III 40 adjusts magnesium salt solution and adds the amount that pump 41 adds magnesium salt solution,
So that the molar ratio of N, P, Mg are 3:1:1.6, guarantee the formation of guanite, the phosphorus in recycling fermentation liquid as much as possible.
2.A2The control method of/O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus is as follows:
1) sanitary sewage in raw water water tank 1 enters together with the returned sludge that return sludge pump 16 is sent through intake pump 7
A2The anaerobic zone 8 of/O reactor 2, return sludge ratio 100% are sufficiently mixed reaction, anaerobic reaction under the action of blender I 36
Time 1.2h, 8 000mg/L of sludge concentration or so；DPAOs synthesizes internal carbon source (PHAs) using the easily biodegradable organics in raw water
Phosphorus is discharged simultaneously, most of organic matter is removed.
2) anoxic zone 9 is subsequently entered, while what is entered also nitrifies the nitrification completely and being separated by solid-liquid separation through BCO reactor 4
Liquid, mixed liquid recycle ratio 300%, hypoxia response time 6.0h, sludge concentration 2500mg/L or so；DPAOs is using PHAs electronics
Donor, with NO3 -- N is electron acceptor synchronous denitrification dephosphorizing.
3) aerobic zone 10, aerobic reaction time 1.2h are proceeded immediately to, turn-on flow rate meter 47 guarantees dissolved oxygen 2.0-
2.5mg/L, oxidation-reduction potential ORP are 50-80mV；The stage, main function was further suction phosphorus without nitrification, was blown simultaneously
The N that de- denitrification process generates2。
4) mixed liquor enters the progress of intermediate sedimentation pond 3 mud-water separation, using the method for operation of intermediate water inlet peripheral effluent, sinks
Form sediment time 1.5-2.0h；A part of precipitating sludge flows back into A through return sludge pump 162The anaerobic zone 8 of/O reactor 2, another portion
Excess sludge is divided to enter storage mud tank 18 by mud valve 17.
5) water outlet of secondary sedimentation tank 3 enters intermediate water tank 11, enters BCO reactor 4 through intermediate lift pump 12, inside sets outstanding
Floating filler, material is polypropylene, specific surface area 1000m2/m3, filling rate 50-55%；Adjusting flowmeter 35 makes three lattice dissolved oxygens
3.0-3.5mg/L guarantees that filler is in fluidized state, and hydraulic detention time 2-3h completes the oxidation of ammonia nitrogen.
6) settling zone 14 is subsequently entered, supernatant is discharged through overflow port, and the biomembrane to fall off enters from bottom mud valve 44
Store up mud tank 18；A part water outlet enters A through nitrification liquid reflux pump 372The anoxic zone 9 of/O reactor 2, provides for denitrification dephosphorization
Electron acceptor, another part direct emission.
7) sludge stored up in mud tank 18 fully enters fermentor 19, the pH in 32 online acquisition fermentor 19 of pH sensor
Value, by the operation of computer 26, obtains real time control variables, controls variable-frequency governor I 29 by process controller 27, adjusts
Whole lye adds the amounts that pump 33 adds NaOH solution, so that pH stablizes 10.0 or so, 10 000mg/L-12 of sludge concentration
000mg/L, fermentation time 7d.
8) fermentation liquid enters recovery of nitrogen and phosphorus tank 20 after, and TP sensor 30, TN sensor 31, magnesium salts sensor 42 are adopted online
Collect TP, TN, magnesium salt concentrations in recovery of nitrogen and phosphorus tank 20, real time control variables is obtained by the operation of computer 26, process is excessively program-controlled
The control of device 27 adjustment of variable-frequency governor II 28 ammonia nitrogen solution processed adds pump 34 and adds the amount of ammonia nitrogen solution, control variable-frequency governor
III 40 adjusts magnesium salt solution and adds the amount that pump 41 adds magnesium salt solution, so that the molar ratio of N, P, Mg are 3:1:1.6.It generates
Guanite takes out, and surplus solution enters liquid reserve tank 23.
3. Application Example:
Using the actual domestic wastewater of students' dormitory area septic tank in certain campus, influent quality is as follows: COD (168.5 ±
20.5)mg/L、NH4 +-N(65.6±23.4)mg/L、NO3 --N(0.3±0.3)mg/L、NO2 --N(0.13±0.1)mg/L、TP
(6.5 ± 0.5) mg/L belongs to typical low C/N sewage.After the present apparatus is handled, effluent quality is as follows: COD (29.0 ±
10.5)mg/L、NH4 +-N(1.0±0.5)mg/L、NO3 --N(4.0±0.5)mg/L、NO2 --N(0.3±0.1)mg/L、TP(0.3
± 0.1) mg/L can reach level-one A standard.
Controlling pH is 10.0 or so, and excess sludge ferments after 7d, and TP concentration is respectively 35.2mg/L in solution, is returned through nitrogen phosphorus
After closed cans processing, water outlet TP concentration is respectively 3.2mg/L, and the rate of recovery of phosphorus is more than 90%.The guanite partial size of formation is in 2.0-
3.2mm, purity is 80% or more.In addition, excess sludge is fermented, after recovery of nitrogen and phosphorus processing, sludge quantity reduces 50% or so.
It can be seen that present invention process not only embodies many advantages of double sludge denitrification dephosphorization technique, but also make system certainly
The excess sludge of body is disposed and resource utilization.
Claims (10)
1.A2/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that including raw water water tank (1), A2/ O reactor (2),
Intermediate sedimentation pond (3), phosphorus recovery system (5), intermediate water tank (11), goes out water tank (15), real-time control system at BCO reactor (4)
It unites (6), the real-time control system includes computer (26), process controller (27)；The phosphorus recovery system (5) includes that TP is passed
Sensor (30), TN sensor (31), pH sensor (32), magnesium salts sensor (42), lye add case (24), lye adds pump
(33), ammonia nitrogen solution dosing tank (25), ammonia nitrogen solution add pump (34), magnesium salt solution dosing tank (43), magnesium salt solution and add pump
(41) and be linked in sequence storage mud tank (18), fermentor (19), recovery of nitrogen and phosphorus tank (20), liquid reserve tank (23)；The A2/ O is anti-
It answers device (2) to be linked in sequence by anaerobic zone (8), anoxic zone (9) and aerobic zone (10) to form, the BCO reactor (4) includes sequence
The biological contact oxidation pond (13) of connection, settling zone (14)；
The outlet of the raw water water tank (1) and the A2The anaerobic zone of/O reactor is connected, the A2The aerobic zone of/O reactor with
The import in intermediate sedimentation pond is connected, and the water outlet in the intermediate sedimentation pond is connected with the import of intermediate water tank (11), the centre
The mud mouth of sedimentation basin (3) respectively with the A2The anaerobic zone of/O reactor and storage mud tank (18) are connected；The intermediate water tank
(11) outlet connects biological contact oxidation pond (13), and the settling zone (14) is separately connected out water tank (15), storage mud tank
(18), water tank and the A out2The anoxic zone (9) of/O reactor (2) connects；
The lye, which adds case (24) and adds pump (33) with lye by variable-frequency governor I (29), to be connected, the lye add pump,
PH sensor (32) is all connected to fermentor (19)；The ammonia nitrogen solution dosing tank (25) passes through variable-frequency governor II (28) and ammonia
Nitrogen solution adds pump (34) and is connected, and the magnesium salt solution dosing tank (43) is added by variable-frequency governor III (40) with magnesium salt solution
It pumps (41) to be connected, the ammonia nitrogen solution adds pump (34), magnesium salt solution adds pump (41), TP sensor (30), TN sensor
(31), magnesium salts sensor (42) is connected with recovery of nitrogen and phosphorus tank (20)；The TP sensor (30), TN sensor (31), pH are passed
Sensor (32), magnesium salts sensor (42) are separately connected computer (26), and the computer is connected with process controller, the process
Controller is separately connected variable-frequency governor I, variable-frequency governor II, variable-frequency governor III.
2. A according to claim 12/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that the device is also set
Have air blower (38), the air blower passes through flow meter I (47), flow meter II (35) and aerobic zone (10), biological respectively
Oxidation pond (13) is connected, and is respectively arranged with aeration head in aerobic zone (10), biological contact oxidation pond (13).
3. A according to claim 12/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that the centre is heavy
The mud mouth in shallow lake pond (3) passes through return sludge pump (16), mud valve I (17) and the A respectively2The anaerobic zone (8) of/O reactor
And storage mud tank (18) is connected.
4. A according to claim 12/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that the settling zone
(14) it is connected by mud valve IV (44) with storage mud tank (18).
5. A according to claim 12/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that the fermentor
(19), recovery of nitrogen and phosphorus tank (20) bottom is respectively equipped with mud valve II (21), mud valve III (22).
6. A according to claim 12/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that the settling zone
(14) it is equipped with overflow port, is equipped with polypropylene suspension filler in the biological contact oxidation pond (13).
7. A according to claim 12/ O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that the A2/ O is anti-
It answers the anaerobic zone of device, anoxic zone to be equipped with blender I, blender III is equipped in the fermentor, is set in the recovery of nitrogen and phosphorus tank
There is blender II.
8. such as A of any of claims 1-72The control method of/O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus,
It is characterized in, comprising the following steps:
1) sanitary sewage in raw water water tank (1) is sent through intake pump (7) and intermediate sedimentation pond (3) through return sludge pump (16)
Returned sludge enters A together2The anaerobic zone (8) of/O reactor, is sufficiently mixed reaction under the action of blender I (36)；
2) it subsequently enters anoxic zone (9), while the BCO reactor (4) for going out water tank (15) outflow there are also warp entered has nitrified
Nitrification liquid that is complete and being separated by solid-liquid separation；
3) it proceeds immediately to aerobic zone (10), turn-on flow rate meter I (47), further inhales phosphorus, while stripping denitrification process generates
N2；
4) mixed liquor of aerobic zone is then entered into intermediate sedimentation pond (3) and carries out mud-water separation, using centre water inlet peripheral effluent
The method of operation；A part of precipitating sludge is set to flow back into A through return sludge pump (16)2The anaerobic zone (8) of/O reactor, it is remaining
Sludge enters storage mud tank (18) by mud valve I (17)；
5) supernatant of intermediate sedimentation pond (3) enters intermediate water tank (11), enters BCO reactor (4) through intermediate intake pump (12)
Biological contact oxidation pond (13), floating stuffing is set in biological contact oxidation pond, adjusts flow meter II (35), guarantees that filler is in
Fluidized state completes the oxidation of ammonia nitrogen；
6) settling zone (14) of biological contact oxidation pond (13) is subsequently entered, supernatant is discharged through overflow port, into water tank out
(15), the biomembrane to fall off enters storage mud tank (18) from bottom mud valve IV (44)；A part is discharged through nitrifying in water tank out
Liquid reflux pump (37) enters A2The anoxic zone (9) of/O reactor, provides electron acceptor for denitrification dephosphorization, remainder is directly arranged
It puts；
7) sludge stored up in mud tank (18) fully enters fermentor (19), in pH sensor (32) online acquisition fermentor (19)
PH value obtains real time control variables by the operation of computer (26), controls variable-frequency governor I by process controller (27)
(29), adjustment lye adds the amount that pump (33) adds NaOH solution, so that pH stablizes 10.0；
8) fermentation liquid enters recovery of nitrogen and phosphorus tank (20) after, and TP sensor (30), TN sensor (31), magnesium salts sensor (42) exist
Line acquires TP, TN, magnesium salt concentrations in recovery of nitrogen and phosphorus tank (20), obtains real time control variables by the operation of computer (26), passes through
Cross process controller (27) control variable-frequency governor II (28) adjustment ammonia nitrogen solution add pump (34) add ammonia nitrogen solution amount, control
Variable-frequency governor III (40) adjustment magnesium salt solution processed adds the amount that pump (41) adds magnesium salt solution, so that the molar ratio of N, P, Mg
Final to take out the guanite generated for 3:1:1.6, surplus solution enters liquid reserve tank (23).
9. A according to claim 82The control method of/O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that
In step 1), anaerobic reaction time 1.2h, 8 000mg/L of sludge concentration；DPAOs is synthesized using the easily biodegradable organics in raw water
Internal carbon source discharges phosphorus simultaneously, and most of organic matter is removed；
In step 2), hypoxia response time 6.0h, sludge concentration 2500mg/L, DPAOs are using PHAs electron donor, with NO3 --N
For electron acceptor synchronous denitrification dephosphorizing.
10. A according to claim 82The control method of/O-BCO technique recovery of nitrogen and phosphorus real-time control apparatus, characterized in that
In step 3), aerobic reaction time 1.2h, turn-on flow rate meter I guarantee that dissolved oxygen 2.0-2.5mg/L, oxidation-reduction potential ORP are
50-80mV；
In step 5), the material of floating stuffing is polypropylene, specific surface area 1000m2/m3, filling rate 50~55%；Adjust flow
Meter II makes dissolved oxygen 3.0-3.5mg/L, guarantees that filler is in fluidized state, hydraulic detention time 2-3h completes the oxygen of ammonia nitrogen
Change；
In step 7), 10 000mg/L-12 000mg/L of sludge concentration, fermentation time 7d in fermentor.
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