CN102053615A - Unsteady-state sectional influent water depth nitrogen and phosphorus removal process control system and control method - Google Patents
Unsteady-state sectional influent water depth nitrogen and phosphorus removal process control system and control method Download PDFInfo
- Publication number
- CN102053615A CN102053615A CN2011100073333A CN201110007333A CN102053615A CN 102053615 A CN102053615 A CN 102053615A CN 2011100073333 A CN2011100073333 A CN 2011100073333A CN 201110007333 A CN201110007333 A CN 201110007333A CN 102053615 A CN102053615 A CN 102053615A
- Authority
- CN
- China
- Prior art keywords
- dissolved oxygen
- control
- section
- reactor
- intake pump
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 69
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 30
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 18
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 17
- 239000011574 phosphorus Substances 0.000 title claims abstract description 17
- 238000004886 process control Methods 0.000 title claims abstract description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 79
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 79
- 239000001301 oxygen Substances 0.000 claims abstract description 79
- 230000008859 change Effects 0.000 claims abstract description 21
- 230000008569 process Effects 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims abstract description 8
- 238000001514 detection method Methods 0.000 claims abstract description 5
- 238000012806 monitoring device Methods 0.000 claims abstract description 4
- 239000010802 sludge Substances 0.000 claims description 27
- 239000010865 sewage Substances 0.000 claims description 25
- 238000010992 reflux Methods 0.000 claims description 15
- 239000003344 environmental pollutant Substances 0.000 claims description 11
- 231100000719 pollutant Toxicity 0.000 claims description 11
- 238000005276 aerator Methods 0.000 claims description 10
- 239000004576 sand Substances 0.000 claims description 8
- 238000012546 transfer Methods 0.000 claims description 7
- 206010002660 Anoxia Diseases 0.000 claims description 5
- 241000976983 Anoxia Species 0.000 claims description 5
- 206010021143 Hypoxia Diseases 0.000 claims description 5
- 230000007953 anoxia Effects 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims description 4
- 238000004088 simulation Methods 0.000 claims description 4
- 238000010835 comparative analysis Methods 0.000 claims description 3
- 239000003814 drug Substances 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 230000002441 reversible effect Effects 0.000 claims description 2
- 230000006872 improvement Effects 0.000 abstract description 11
- 238000012544 monitoring process Methods 0.000 abstract description 2
- 230000000737 periodic effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 24
- 238000005273 aeration Methods 0.000 description 11
- 230000000694 effects Effects 0.000 description 10
- 238000011217 control strategy Methods 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000012851 eutrophication Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 230000002045 lasting effect Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 241001269238 Data 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
- YUWBVKYVJWNVLE-UHFFFAOYSA-N [N].[P] Chemical compound [N].[P] YUWBVKYVJWNVLE-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 230000009514 concussion Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000012937 correction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010840 domestic wastewater Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000013486 operation strategy Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000009418 renovation Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000005316 response function Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 230000003319 supportive effect Effects 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Images
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/02—Total factory control, e.g. smart factories, flexible manufacturing systems [FMS] or integrated manufacturing systems [IMS]
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to an unsteady-state sectional influent water depth nitrogen and phosphorus removal process control system and a control method. An upper PC (Personnel computer) is connected with a PLC (programmable logic controller) through the Ethernet; the PLC is connected with a motor/variable-frequency control cabinet for controlling influent water load dynamic change and constant dissolved oxygen; the control cabinet is connected with an actuating mechanism and a monitoring device; an influent water phase angle change process, a periodic change process and a sine curve wave crest and wave trough change process are contained in the influent water load dynamic change; a dissolved oxygen determinator, a dissolved oxygen sensor, a gas flow meter and an electric valve are contained in the constant dissolved oxygen control; and a monitoring control system comprises a site instrument, a water inflow adjusting pump, an anaerobic/anoxic reactor and a blower. The motor/the variable-frequency control cabinet is connected with a detection device and a power device by a control bus through the PLC controller and the computer; and the improvement of sectional influent water process performance is realized through controlling the influent water load dynamic change and the constant dissolved oxygen under the unsteady-state influent water conditions.
Description
Technical field
The invention belongs to technical field of biological sewage treatment by using, relate to a kind of unstable state advanced nitrogen and phosphorus removal by step feed Process Control System and control method, especially optimize improvement segmental influent technological design and operation control strategy, improve PROCESS FOR TREATMENT effect and stability, improve the device control performance, can realize simultaneously changing the energy-saving method of adjusting operational factor in real time, be applicable to the upgrading or the newly-built technology of building segmental influent technology according to water inlet.
Background technology
Along with the attention of environmental administration of government, though domestic wastewater treatment rate improves constantly, the water eutrophication problem that is caused by nitrogen and phosphorus pollution does not only solve, and serious day by day trend is arranged.Being the denitrogenation dephosphorizing water pollution control technology of purpose with the control eutrophication at present, is the research focus in wastewater treatment in China field.In recent years, although the research of China's municipal effluent denitrification dephosphorization technique has had remarkable progress, but still ubiquity technological process complexity, structures are various, energy consumption and surplus sludge volume is excessive, synchronous denitrification dephosphorizing efficient is low, lack the defectives such as Process Control System that make things convenient for actual effect.The defective of traditional biological denitrification dephosphorization technique and the requirement of sustainable sewage disposal technology impel the develop rapidly of biological carbon and phosphorous removal new technology and technology.Improvement segmental influent denitrification dephosphorization technique is based on the new and effective denitrification dephosphorization technique of Cape Town, RSA university technology (UCT technology) exploitation, it can farthest utilize former water carbon source, have very large competitive edge for China's general low ratio of carbon to ammonium municipal effluent water quality situation, present stage from improving sewerage nitrogen and phosphor removal effect, containment eutrophication problem and all there are major and immediate significance and popularizing application prospect in aspect such as energy-saving and cost-reducing.In addition, increasingly stringent and wastewater treatment in China plant effluent water quality present situation along with China's town sewage emission standard, urban wastewater treatment firm more than 90% is faced with the technical renovation and the upgrading of existing treatment process, for accomplishing especially to settle at one go, reach national town sewage one-level A emission standard in the sewage treatment plant that builds.
Variation and diurnal variation all can present the certain rules characteristics when flow of inlet water of municipal sewage plant and pollutant levels, there is bigger fluctuation range, the highest flow of inlet water of every day can be several times of minimum flow of inlet water, pollutant levels also can reach peak value in the day peak period, therefore sewage treatment plant's technology effluent quality situation also changes thereupon, finally influences per day effluent quality.To this, the Sewage Plant of having built at present is at the bigger design safety factor (DSF) of general employing of design phase in early stage, water factory is moved the negative effect that causes with the fluctuation of alleviating amount of inlet water and water quality, but this has increased the capital cost of waterworks construction undoubtedly, waste part structures capacity increases operation energy consumption during underload.Simultaneously, the control system of water factory's application at present IPC and the PLC collective and distributive type control systems that adopt based on PLC realize adopting the computer centralized distribution control mode more, and sewage treatment plant's production run is carried out decentralised control, the concentrated supervision and management.Compare with world level, the robotization and the informationization technology of China also relatively lag behind, and are mainly reflected in the imbalance and the application level aspect of development.The informationization technology that with the intelligent decision is target is then slow relatively, " information island " phenomenon is still serious, automatic technology and informationization technology lack fusion, a large amount of process datas " is lain " at the scene all quietly, and do not bring into play its due effect, the Sewage Plant control system can only be carried out pre-set control strategy, does not possess the response function at factor real-time change such as practical operation situation such as influent load variations.
Choosing for device nitrogen phosphorus removal effect and organism utilization ratio of each section of improvement segmental influent technology flow of inlet water distribution ratio all has bigger influence, and weather conditions such as different influent qualities, different water outlet standard-required and heavy rain all can adopt best separately flow of inlet water distribution ratio, follow-up like this each section Aerobic Pond aeration energy consumption also changes thereupon, and each section air compressor needs response change to reduce the aeration power cost.In addition, in the prior art, the aerator of most of sewage treatment plants adopts manually control on the spot or simple PID (proportional-integral-differential) control loop.The former mainly be the operations staff by the labor measurement dissolved oxygen DO after with the empirical parameter value relatively, rule of thumb actuators such as valve are carried out condition, the latter is according to the deviate of online detection instrument measured value and setting value, export topworks to by the PID computing and carry out corresponding adjusting, thus the dissolved oxygen concentration of control aeration tank.From present Sewage Plant dissolved oxygen DO control effect, more than two kinds of methods exist certain deficiency.At first, the valve of existing sewage treatment plant generally is non-linear, the dissolved oxygen DO range of control of the realization expection that simple PID control can not be strict, and also serious time delay hysteresis problem causes the huge disturbance of dissolved oxygen concentration in the aeration tank.In addition, artificial control on the spot requires the operations staff must have long-term field adjustable experience, human factor influence is excessive, generally takes bigger redundance guaranteeing the controlling required dissolved oxygen value of microorganism normal growth breeding, thereby causes the waste of aeration energy consumption.
Therefore, demand developing a kind of unstable state advanced nitrogen and phosphorus removal by step feed Process Control System and control method urgently, fully guaranteeing coupling biological sewage treatment new technology, guarantee under the prerequisite of sewage treatment capacity, energy-conservation potentiality of excavating gear as much as possible realize the high handling rate and the high automation controlling level of improvement segmental influent denitrification dephosphorization technique.
Summary of the invention
The objective of the invention is at China different cities sewage treatment plant inflow load the time and a day dynamic rule, a kind of unstable state advanced nitrogen and phosphorus removal by step feed Process Control System and control method are provided, utilize the different influent load Changing Pattern of influent load dynamic change module settings, with the aerobic reactor dissolved oxygen DO is controlled variable, detect dissolved oxygen value in real time and dynamic data information is transferred to the control decision supportive device by network communications technology, sunykatuib analysis by decision support apparatus, produce suitable service condition of corresponding technology and control strategy, determine the optimal operational condition of device, implement the regulation and control motorized valve again, and dissolved oxygen DO is monitored by technology on-line monitoring equipment, detected value is fed back to control system and operational decisions device, device operation strategy is fed back checking and the correction of making a strategic decision, the efficient operation of success and the application of ultimate guarantee improvement segmental influent technology.
The present invention adopts following technological means to realize:
A kind of unstable state advanced nitrogen and phosphorus removal by step feed Process Control System, upper PC is connected with Programmable Logic Controller PLC controller by Ethernet; Programmable PLC controller and the motor that influent load dynamic change control and constant dissolved oxygen DO are controlled the variable frequency control cabinet be connected; Motor the variable frequency control cabinet be connected with topworks and monitoring device; The influent load dynamic change comprises into water phase angle variations flow process, water inlet cycle modified flow and water inlet sinusoidal curve Wave crest and wave trough modified flow; Constant dissolved oxygen DO control comprises dissolved oxygen meter, dissolved oxygen sensor, gas meter and motorized valve; Supervisor control comprise field instrument, inflow regulate pump, anaerobism anoxic reacter, each section air blast.Motor the variable frequency control cabinet be connected with computing machine by the programmable PLC controller with checkout equipment, power-equipment by control bus;
Sewage water tank several intake pumps through being connected with control bus link to each other with the main body reactor; Several anaerobism anoxic reacter and settling basin link to each other successively; Settling basin links to each other with first section anoxic reacter with the sludge reflux pump that is connected with control bus through the mud reverse flow valve; The interior reflux pump of first section anoxic reacter through being connected with control bus is connected with anaerobic reactor; The stirrer that is connected with control bus all is set in three anoxic reacters; Aerobic reactor is provided with sand head aerator and dissolved oxygen sensor, and wherein, sand head aerator is through gas meter, and the motorized valve that is connected with control bus is connected with fan blower, and dissolved oxygen sensor is connected with control bus through dissolved oxygen instrument; Excess sludge is by the discharging of excess sludge discharge valve.
Aforesaid intake pump comprises first section intake pump, second section intake pump, the 3rd section intake pump.
Aforesaid anaerobism anoxic reacter comprise anaerobic reactor, first section anoxic reacter, first section aerobic reactor, second section anoxic reacter, second section aerobic reactor, the 3rd section anoxic reacter, the 3rd section aerobic reactor.
A kind of unstable state advanced nitrogen and phosphorus removal by step feed course control method for use may further comprise the steps:
The dynamic change of control influent load;
The control interface of intake pump, internal circulation pump and sludge reflux pump is connected with control bus; In the peak value and the cycle of intaking dynamic sinusoidal variations law curve computer operation interface setting day; By medicine machine control pollutant levels; Mild when the amount of inlet water variation, three sections intake pump rotating speed ratios remained on 40%: 30%: 30%; If when meeting water yield load rapid increasing of moment, can transfer the rotating speed of big intake pump simultaneously, and increase the rotating speed of sludge reflux pump, to reduce the number of dropouts of washing away to the device active sludge;
Control constant dissolved oxygen DO:
The dissolved oxygen concentration of mixed liquor in first section aerobic reactor of the online detection of dissolved oxygen sensor, measured value shows on dissolved oxygen meter, this measured value after communication transfers to control box with control program in the comparative analysis of dissolved oxygen DO setting value, if measured value is in 1.5 ± 0.5mg/L scope, then control program maintains the original state, and does not carry out any program; If measured value exceeds setting range, then this data-signal transforms through simulation and exports motorized valve to, adjusts valve opening degree, to increase or to reduce the blow rate required of fan blower; Be divided into following three kinds of control situations:
Little when the rotation speed change of intake pump, i.e. the influent load of first section reactor variation is not obvious, and then control box is not done any executive routine, and motorized valve is kept certain open degree or fine setting;
When the rotating speed of intake pump or water inlet pollutant levels continue to increase, cause the influent load of first section reactor constantly to increase, oxygen demand increases in the aerobic reactor, dissolved oxygen concentration reduces, when concentration determination value during less than 1.0mg/L, motorized valve begins to regulate, and opens gradually with 4% stride, in dissolved oxygen concentration returns to 1.5 ± 0.5mg/L scope;
Rotating speed or the lasting reduction of water inlet pollutant levels when intake pump, cause the influent load of first section reactor constantly to reduce, oxygen demand reduces in the aerobic reactor, dissolved oxygen concentration increases, when concentration determination value during greater than 2.0mg/L, motorized valve begins to regulate, and the stride with 4% is closed gradually, in dissolved oxygen concentration returns to .5 ± 0.5mg/L scope.
Improvement advanced nitrogen and phosphorus removal by step feed process control systems compared with prior art has the following advantages under the unstable state water inlet condition that the present invention relates to:
(1) the denitrogenation dephosphorizing performance is good, need not to satisfy national town sewage one-level A emission standard under the additional carbon condition, the municipal effluent water quality situation that is particularly useful for China's low ratio of carbon to ammonium is for China's municipal sewage plant's upgrading or newly-built water factory provide the reliable technique support.
(2) the influent load dynamic change device of Jian Liing can real simulation actual sewage treatment plant influent load dynamic rule, and, improve the reliability and stability of this technology practical engineering application greatly to these reasonable operational factors such as each section flow of inlet water allocation proportion, return sludge ratio and nitrate recirculation ratio of adjusting.
(3) Aerobic Pond dissolved oxygen DO control system can be adjusted the aeration rate of fan blower in real time accordingly according to the influent load variation, guarantee the dissolved oxygen concentration in the Aerobic Pond effectively, avoided the not thorough and excessive energy consumption waste problem that causes of aeration of the not enough caused effect of aeration, realized the process control of online in real time, on the basis that guarantees effluent quality, improve biochemical unit operational efficiency, reduce aeration energy consumption.
Description of drawings
Fig. 1 is the Process Control System figure of improvement advanced nitrogen and phosphorus removal by step feed;
Fig. 2 is improvement segmental influent technology integrated control system figure;
Fig. 3 distributes control strategy for improvement advanced nitrogen and phosphorus removal by step feed technology flow of inlet water;
Fig. 4 is technology water inlet total amount day dynamic rule figure;
Fig. 5 is aerobic reactor dissolved oxygen concentration changing trend diagram (is example with first section aerobic reactor) before and after the control.
Among Fig. 2: 1 is the sewage water tank; 2 is first section intake pump; 3 is second section intake pump; 4 is the 3rd section intake pump; 5 is the anaerobic reactor stirrer; 6 is first section anoxia stirring device; 7 is second section anoxia stirring device; 8 is the 3rd section anoxia stirring device; 9 is No. 1 dissolved oxygen instrument; 10 is No. 2 dissolved oxygen instruments; 11 is No. 3 dissolved oxygen instruments; 12 is anaerobic reactor; 13 is first section anoxic reacter; 14 is first section aerobic reactor; 15 is second section anoxic reacter; 16 is second section aerobic reactor; 17 is the 3rd section anoxic reacter; 18 is the 3rd section aerobic reactor; 19 is No. 1 dissolved oxygen sensor; 20 is No. 2 dissolved oxygen sensors; 21 is No. 3 dissolved oxygen sensors; 22 is No. 1 sand head aerator; 23 is No. 2 sand head aerators; 24 is No. 3 sand head aerators; 25 is No. 1 spinner-type flowmeter; 26 is No. 2 spinner-type flowmeters; 27 is No. 3 spinner-type flowmeters; 28 is No. 1 motorized valve; 29 is No. 2 motorized valves; 30 is No. 3 motorized valves; 31 is No. 1 fan blower; 32 is No. 2 fan blowers; 33 is No. 3 fan blowers; 34 is internal circulation pump: 35 are sludge reflux pump; 36 is the mud recycle control valve; 37 is the excess sludge discharge valve; 38 is settling basin; 39 is control bus; 40 is control box; 41 is computing machine; 50 is host computer; 60 is Programmable Logic Controller; 70 is motor controlling cabinet and variable frequency control cabinet.
Embodiment
Describe the present invention in detail below in conjunction with drawings and Examples:
With the preliminary sedimentation tank water outlet of Beijing sewage treatment plant is research object (COD=119-565mg/L, TN=24.6-79.5mg/L, TP=0.48-13.3mg/L, C/N=1.5-6.4, C/P=35.7-74.5), hydraulic detention time 8-10h, sludge age 8-12d, average sludge concentration 5000 ± 150mg/L, return sludge ratio 0.5-0.75.
Improvement advanced nitrogen and phosphorus removal by step feed process control systems under unsteady state condition as shown in Figure 1, first section intake pump being connected with sewage water tank 12, second section intake pump 3, the 3rd section intake pump 4 are connected with control bus 39; Anaerobic reactor 12, first section anoxic reacter 13, first section aerobic reactor 14, second section anoxic reacter 15, second section aerobic reactor 16, the 3rd section anoxic reacter 17, the 3rd section separate space that aerobic reactor 18 is isolated each other; From settling basin 38 and from settling basin 38 be back to first section anoxic reacter 13 mud external reflux pipeline, be back to the muddy water mixed solution return line of anaerobic reactor 12 and control box 40 and computing machine 41 from first section anoxic reacter 13.
In addition, the useful volume of sewage water tank 1 is 340L, testing selected test model reactor is rectangular reactor, useful volume is 340L, be divided into 13 lattice chamber operations: first lattice chamber is anaerobic reactor 12 (34L), second lattice chamber is first section anoxic reacter 13 (34L), and then three lattice chambers are first section aerobic reactor 14 (68L), are second section anoxic reacter 15 (34L), second section aerobic reactor 16 (68L), the 3rd section anoxic reacter 17 (34L), the 3rd section aerobic reactor 18 (68L) then successively.Settling basin 38 useful volumes are 85L.
Former water enters into 9, the second sections anoxic reacters 15 of anaerobic reactor and the 3rd section anoxic reacter 17 by water inlet pipe through intake pump 2,3,4 respectively; In anaerobic reactor 12, first section anoxic reacter 13, second section anoxic reacter 15, the 3rd section anoxic reacter 17, be separately installed with stirrer 5,6,7,8 and be in suspended state, and stirrer all is connected with control bus 39 to be implemented in the line control switch start and stop by lead to keep mud; First section aerobic reactor 14, second section aerobic reactor 16 and the 3rd section aerobic reactor 18 are respectively equipped with sand head aerator 22,23,24 and dissolved oxygen sensor 19,20,21, wherein three dissolved oxygen sensors are connected with control bus 39 through dissolved oxygen DO detector 9,10,11 respectively, aerator provides aeration by fan blower 31,32,33 respectively, three aerating pipelines are provided with gas meter 25,26,27 and motorized valve 28,29,30 respectively, and motorized valve is connected with control bus 39; Each section anoxic reacter is connected at interval in turn with aerobic reactor; Settling basin 38 bottoms are communicated with by returned sluge operation valve 36 and first section anoxic reacter 13 of sludge reflux pump 35 and anoxic, and excess sludge is by excess sludge discharge operation valve 37 dischargers; First section anoxic reacter 13 is communicated with anaerobic reactor 12 by internal circulation pump 34; Internal circulation pump 34 is connected with control bus through lead with sludge reflux pump 35.
Fig. 2 describes control structure of the present invention in detail, mainly comprises: the host computer PC, industrial control configuration software is installed, and have the function of picture supervision, centralized control, analog quantity demonstration, data acquisition, data-switching, report output printing; Programmable Logic Controller PLC control system is responsible for control strategy, programmed control, time control, program debug etc., comprises into water phase angle variations flow process, water inlet cycle modified flow and three control strategies of water inlet sinusoidal curve Wave crest and wave trough modified flow; Motor controlling cabinet and variable frequency control cabinet; Topworks and monitoring device comprise field instruments such as pH and dissolved oxygen DO, intake pump and sludge reflux pump, reach equipment such as stirrer and fan blower.
Concrete control method and step are:
(1) control influent load dynamic change:
At first, intake pump 2,3,4, the control interface of internal circulation pump 34 and sludge reflux pump 35 is connected with control bus, is convenient to freely set at the computer operation interface rotating speed of every pump.In addition, the peak value and the cycle of day dynamic sinusoidal variations law curve of water inlet can be simulated multiple influent quality water yield Changing Pattern at the computer operation interface setting, to study this process unit capacity of resisting impact load.And for the modeling effort of water quality impact load, pollutant levels can be by independent medicine machine control.The assignment of traffic control measure are: milder when the amount of inlet water variation, when promptly influent load was stablized, three sections intake pump rotating speed ratios can remain on 40%: 30%: 30%; If meet heavy rain and be season water yield load moment when sharply increasing, can transfer big intake pump 3 and 4 or transfer the rotating speed of big intake pump 4 separately simultaneously, and increase the rotating speed of sludge reflux pump 35, to reduce the number of dropouts of washing away to the device active sludge.
Concrete control operation program circuit as shown in Figure 3, at first device starts, select automatic non-manual state, set a section flow of inlet water allocation proportion, then each section water inlet variable be total water inlet variable of changing in time and the product of a section water inlet ratio setting value, improves each section of segmental influent technology flow of inlet water and all is the cycle variation in time thereby draw.Fig. 4 then is the total inflow day dynamic changing curve of realizing according to Fig. 3 control program, and each section inflow Changing Pattern is consistent with total amount.
(2) control constant dissolved oxygen DO:
At water inlet influent load dynamic change control system, assurance device nitrification effect and the feed-forward and feedback control loop developed, mainly comprise dissolved oxygen meter 9,10,11, dissolved oxygen sensor 19,20,21, gas meter 25,26,27 and motorized valve 28,29,30.Be that example illustrates constant dissolved oxygen DO control principle and method with first section aerobic reactor 14 below.
The dissolved oxygen concentration of mixed liquor in first section aerobic reactor of dissolved oxygen sensor 19 online detections 14, measured value shows on dissolved oxygen meter 9, the dissolved oxygen DO setting value comparative analysis of this measured value after communication transfers to control box 40 and in the control program, if measured value is in (1.5 ± 0.5) mg/L scope, then control program maintains the original state, and does not carry out any program; If measured value exceeds setting range, then this data-signal transforms through simulation and exports motorized valve 28 to, adjust valve opening degree, to increase or to reduce the blow rate required of fan blower 31, the effect of gas meter 25 is stable as far as possible aeration rates that are sent in the aerobic reactor 19, to avoid the excessive concussion fluctuation of dissolved oxygen concentration.Based on field adjustable, mainly be divided into following three kinds of control situations:
When the rotation speed change of intake pump 2 little, promptly the influent load of first section reactor 12,13,14 changes not obvious, be not enough to influence the dissolved oxygen concentration in the aerobic reactor 14, then control box is not done any executive routine, and motorized valve 28 is kept certain open degree or fine setting.
When the rotating speed of intake pump 2 or water inlet pollutant levels continue to increase, cause the influent load of first section reactor 12,13,14 constantly to increase, oxygen demand increases in the aerobic reactor 14, dissolved oxygen concentration reduces, when concentration determination value during less than 1.0mg/L, motorized valve 28 beginnings are regulated automatically, open gradually with 4% stride, in dissolved oxygen concentration returns to (1.5 ± 0.5) mg/L scope.
Rotating speed or the lasting reduction of water inlet pollutant levels when intake pump 2, cause the influent load of first section reactor 12,13,14 constantly to reduce, oxygen demand reduces in the aerobic reactor 14, dissolved oxygen concentration increases, when concentration determination value during greater than 2.0mg/L, motorized valve 28 beginnings are regulated automatically, and the stride with 4% is closed gradually, in dissolved oxygen concentration returns to (1.5 ± 0.5) mg/L scope.
Claims (4)
1. unstable state advanced nitrogen and phosphorus removal by step feed Process Control System, upper PC is connected with Programmable Logic Controller PLC controller by Ethernet; It is characterized in that: programmable PLC controller and the motor that influent load dynamic change control and constant dissolved oxygen DO are controlled the variable frequency control cabinet be connected; Motor the variable frequency control cabinet be connected with topworks and monitoring device;
Described influent load dynamic change comprises into water phase angle variations flow process, water inlet cycle modified flow and water inlet sinusoidal curve Wave crest and wave trough modified flow;
Described constant dissolved oxygen DO control comprises dissolved oxygen meter, dissolved oxygen sensor, gas meter and motorized valve;
Described supervisor control comprise field instrument, inflow regulate pump, anaerobism anoxic reacter stirrer, each section air blast.
Described motor the variable frequency control cabinet be connected with computing machine by the programmable PLC controller with checkout equipment, power-equipment by control bus (39);
Sewage water tank (1) several intake pumps through being connected with control bus (39) link to each other with the main body reactor agitator; Several anaerobism anoxic reacter stirrer and settling basin link to each other successively; Settling basin links to each other with first section anoxia stirring device (6) with the sludge reflux pump that is connected with control bus through the mud reverse flow valve; The interior reflux pump of first section anoxic reacter (6) through being connected with control bus is connected with anaerobic reactor (12); The stirrer that is connected with control bus all is set in three anoxic reacters; Aerobic reactor is provided with sand head aerator and dissolved oxygen sensor, and wherein, sand head aerator is through gas meter, and the motorized valve that is connected with control bus is connected with fan blower, and dissolved oxygen sensor is connected with control bus through dissolved oxygen instrument; Excess sludge is by the discharging of excess sludge discharge valve.
2. unstable state advanced nitrogen and phosphorus removal by step feed Process Control System according to claim 1 is characterized in that: described intake pump comprises first section intake pump (2), second section intake pump (3), the 3rd section intake pump (4).
3. unstable state advanced nitrogen and phosphorus removal by step feed Process Control System according to claim 1 is characterized in that: described anaerobism anoxic reacter comprise anaerobic reactor stirrer (5), first section anoxia stirring device (6), first section aerobic reactor (14), second section anoxic reacter (15), second section aerobic reactor (16), the 3rd section anoxic reacter (17), the 3rd section aerobic reactor (18).
4. unstable state advanced nitrogen and phosphorus removal by step feed course control method for use is characterized in that may further comprise the steps:
4.1, dynamic change is controlled to influent load;
4.1.1, intake pump (2) (3) (4), internal circulation pump (34) and the control interface of sludge reflux pump (35) are connected with control bus;
4.1.2, in the peak value and the cycle of intaking dynamic sinusoidal variations law curve computer operation interface setting day;
4.1.3, by medicine machine control pollutant levels;
4.1.4, when amount of inlet water changes gently, three sections intake pump rotating speed ratios remained on 40%: 30%: 30%; If when meeting water yield load rapid increasing of moment, can transfer the rotating speed of big intake pump simultaneously, and increase the rotating speed of sludge reflux pump, to reduce the number of dropouts of washing away to the device active sludge;
4.2, control constant dissolved oxygen DO
The dissolved oxygen concentration of the interior mixed liquor of dissolved oxygen sensor (19) first section aerobic reactor of online detection (14), measured value goes up at dissolved oxygen meter (9) and shows, the dissolved oxygen DO setting value comparative analysis of this measured value after communication transfers to control box (40) and in the control program, if measured value is in 1.5 ± 0.5mg/L scope, then control program maintains the original state, and does not carry out any program; If measured value exceeds setting range, then this data-signal transforms through simulation and exports motorized valve (28) to, adjusts valve opening degree, to increase or to reduce the blow rate required of fan blower (31); Be divided into following three kinds of control situations:
4.2.1, little when the rotation speed change of intake pump (2), promptly the influent load of first section reactor (12), (13), (14) changes not obviously, then control box is not done any executive routine, motorized valve (28) is kept certain open degree or fine setting;
4.2.2, continue to increase when the rotating speed of intake pump (2) or water inlet pollutant levels, cause the influent load of first section reactor (12), (13), (14) constantly to increase, the interior oxygen demand of aerobic reactor (14) increases, dissolved oxygen concentration reduces, when concentration determination value during less than 1.0mg/L, motorized valve (28) begins to regulate, and opens gradually with 4% stride, in dissolved oxygen concentration returns to 1.5 ± 0.5mg/L scope;
4.2.3, continue to reduce when the rotating speed of intake pump (2) or water inlet pollutant levels, cause the influent load of first section reactor (12), (13), (14) constantly to reduce, the interior oxygen demand of aerobic reactor (14) reduces, dissolved oxygen concentration increases, when concentration determination value during greater than 2.0mg/L, motorized valve (28) begins to regulate, and the stride with 4% is closed gradually, in dissolved oxygen concentration returns to .5 ± 0.5mg/L scope.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100073333A CN102053615B (en) | 2011-01-13 | 2011-01-13 | Control system and control method of unsteady-state sectional influent water depth nitrogen and phosphorus removal process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100073333A CN102053615B (en) | 2011-01-13 | 2011-01-13 | Control system and control method of unsteady-state sectional influent water depth nitrogen and phosphorus removal process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102053615A true CN102053615A (en) | 2011-05-11 |
| CN102053615B CN102053615B (en) | 2012-08-15 |
Family
ID=43958033
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011100073333A Expired - Fee Related CN102053615B (en) | 2011-01-13 | 2011-01-13 | Control system and control method of unsteady-state sectional influent water depth nitrogen and phosphorus removal process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102053615B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102690019A (en) * | 2012-05-08 | 2012-09-26 | 北京工业大学 | High-efficiency nitrogen and phosphorus synchronous removal method in treating low concentration wastewater |
| CN106219618A (en) * | 2016-04-08 | 2016-12-14 | 江苏天雨环保集团有限公司 | Integral intelligent pumping plants based on many water distribution points and water outlet distribution control method thereof |
| CN106865770A (en) * | 2017-03-30 | 2017-06-20 | 中国华电集团科学技术研究总院有限公司 | Underload A2The class SBR operation methods of O techniques |
| CN107500408A (en) * | 2017-09-04 | 2017-12-22 | 信开水环境投资有限公司 | A kind of multistage A/O techniques aeration control system fed back based on ammonia nitrogen and dissolved oxygen |
| CN107540169A (en) * | 2017-10-16 | 2018-01-05 | 合肥清原自控科技有限公司 | A kind of sewage treatment control system and its processing method |
| CN109399805A (en) * | 2018-10-29 | 2019-03-01 | 安徽京望环保科技有限公司 | A kind of circulating biological filter tank sewage treatment process and device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040040907A1 (en) * | 2000-09-27 | 2004-03-04 | Katia Wouters-Wasiak | Method for effluent purification |
| WO2009119961A1 (en) * | 2008-03-26 | 2009-10-01 | Sam Chang Enterprise Co., Ltd | System for controlling advanced wastewater treatment apparatus with two-stage reactor |
| CN101570382A (en) * | 2009-06-10 | 2009-11-04 | 北京工业大学 | Device for improving advanced nitrogen and phosphorus removal by step feed and method |
| CN201343460Y (en) * | 2008-11-28 | 2009-11-11 | 北京工业大学 | Device for strengthening the process control in CAST step-feed synchronous nitrogen and phosphorus removal |
| CN201936179U (en) * | 2011-01-13 | 2011-08-17 | 北京工业大学 | Unstable improved sectional inlet water depth denitrification and dephosphorization progress control system |
-
2011
- 2011-01-13 CN CN2011100073333A patent/CN102053615B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040040907A1 (en) * | 2000-09-27 | 2004-03-04 | Katia Wouters-Wasiak | Method for effluent purification |
| WO2009119961A1 (en) * | 2008-03-26 | 2009-10-01 | Sam Chang Enterprise Co., Ltd | System for controlling advanced wastewater treatment apparatus with two-stage reactor |
| CN201343460Y (en) * | 2008-11-28 | 2009-11-11 | 北京工业大学 | Device for strengthening the process control in CAST step-feed synchronous nitrogen and phosphorus removal |
| CN101570382A (en) * | 2009-06-10 | 2009-11-04 | 北京工业大学 | Device for improving advanced nitrogen and phosphorus removal by step feed and method |
| CN201936179U (en) * | 2011-01-13 | 2011-08-17 | 北京工业大学 | Unstable improved sectional inlet water depth denitrification and dephosphorization progress control system |
Non-Patent Citations (1)
| Title |
|---|
| 《中国优秀硕士学位论文全文数据库》 20090215 刘岩 污水处理控制系统的设计 第16-33,38,51-56页 1-3 , 第02期 2 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102690019A (en) * | 2012-05-08 | 2012-09-26 | 北京工业大学 | High-efficiency nitrogen and phosphorus synchronous removal method in treating low concentration wastewater |
| CN106219618A (en) * | 2016-04-08 | 2016-12-14 | 江苏天雨环保集团有限公司 | Integral intelligent pumping plants based on many water distribution points and water outlet distribution control method thereof |
| CN106865770A (en) * | 2017-03-30 | 2017-06-20 | 中国华电集团科学技术研究总院有限公司 | Underload A2The class SBR operation methods of O techniques |
| CN107500408A (en) * | 2017-09-04 | 2017-12-22 | 信开水环境投资有限公司 | A kind of multistage A/O techniques aeration control system fed back based on ammonia nitrogen and dissolved oxygen |
| CN107500408B (en) * | 2017-09-04 | 2020-07-28 | 国投信开水环境投资有限公司 | Multistage A/O process aeration control system based on ammonia nitrogen and dissolved oxygen feedback |
| CN107540169A (en) * | 2017-10-16 | 2018-01-05 | 合肥清原自控科技有限公司 | A kind of sewage treatment control system and its processing method |
| CN109399805A (en) * | 2018-10-29 | 2019-03-01 | 安徽京望环保科技有限公司 | A kind of circulating biological filter tank sewage treatment process and device |
| CN109399805B (en) * | 2018-10-29 | 2021-07-13 | 安徽京望环保科技有限公司 | Circulating biological filter sewage treatment process and device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102053615B (en) | 2012-08-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102053615B (en) | Control system and control method of unsteady-state sectional influent water depth nitrogen and phosphorus removal process | |
| CN102156432B (en) | Method for controlling aeration in biochemical reaction tank in real time | |
| CN101759290B (en) | Method for rapidly realizing and stably maintaining shortcut nitrification in continuous flow process | |
| CN102328996B (en) | Device and method for optimized control over carbon source feeding in denitrification biofilter process | |
| CN201662710U (en) | Double-parameter aeration control system for sewage treatment system | |
| CN106495321B (en) | Biological tank process optimization and operation control system and its control method | |
| CN114230110B (en) | Short-range intelligent phosphorus removal and medicine addition control method, equipment and system for sewage treatment | |
| CN109704463B (en) | Carbon optimization feeding system of AAO process sewage treatment plant | |
| CN104238527A (en) | Precise control method of sewage treatment plant aeration total quantity | |
| CN101121564B (en) | Fuzzy control device and method for A/O technique subsection water-feeding deep denitrogenation | |
| CN105731734B (en) | A kind of energy saving MBR sewage disposal systems | |
| CN108569756A (en) | A kind of Intellectualized sewage water treatment process control new method（EBIS） | |
| CN109205808A (en) | A kind of accurate aeration control method based on water outlet ammonia nitrogen and dissolved oxygen | |
| CN111547948A (en) | Optimized operation method of integrated sewage treatment equipment | |
| CN201191473Y (en) | A/O process segmental influent deep nitric removing fuzzy control teaching apparatus | |
| CN201936179U (en) | Unstable improved sectional inlet water depth denitrification and dephosphorization progress control system | |
| CN209740814U (en) | Carbon source optimizing and adding system for AAO process sewage treatment plant | |
| CN204661510U (en) | Sewage disposal plant aeration tank program control system | |
| CN207845269U (en) | constant DO control system based on real-time OUR | |
| CN214004188U (en) | Biological continuous reaction intelligent system | |
| CN205676222U (en) | Accurate aeration control system for Orbal oxidation ditch | |
| CN213231944U (en) | VFL sewage treatment equipment | |
| CN104111666A (en) | Optimized CAST domestic sewage sludge reduction control system and working method | |
| CN105549394B (en) | A kind of optimal control method and control system of oxidation ditch aeration and plug-flow process | |
| CN108928920B (en) | Comprehensive pool with pollutant emission reduction, regulation and tempering and denitrification functions |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent for invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Peng Yongzhen Inventor after: Ge Shijian Inventor after: Huo Mingcuan Inventor after: Cao Xu Inventor after: Wang Shuying Inventor after: Bao Fengyang Inventor before: Peng Yongzhen Inventor before: Ge Shijian Inventor before: Cao Xu Inventor before: Wang Shuying Inventor before: Bao Fengyang |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: PENG YONGZHEN GE SHIJIAN CAO XU WANG SHUYING BO FENGYANG TO: PENG YONGZHEN GE SHIJIAN HUO MINGXIN CAO XU WANG SHUYING BO FENGYANG |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180330 Address after: 150090 room 1003, Huahong International Center, No. 75, Minjiang Road, Nangang District, Harbin, Heilongjiang Patentee after: Heilongjiang bishuiyuan Environmental Engineering Co., Ltd. Address before: 100124 Chaoyang District, Beijing Ping Park, No. 100 Patentee before: Beijing University of Technology |
|
| TR01 | Transfer of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120815 Termination date: 20200113 |