CN110968028A - Oxygen supply energy-saving optimization control method for SBR process - Google Patents
Oxygen supply energy-saving optimization control method for SBR process Download PDFInfo
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- CN110968028A CN110968028A CN201911238202.9A CN201911238202A CN110968028A CN 110968028 A CN110968028 A CN 110968028A CN 201911238202 A CN201911238202 A CN 201911238202A CN 110968028 A CN110968028 A CN 110968028A
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- 238000000034 method Methods 0.000 title claims abstract description 48
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 19
- 239000001301 oxygen Substances 0.000 title claims abstract description 19
- 238000005457 optimization Methods 0.000 title claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 238000005273 aeration Methods 0.000 claims abstract description 32
- 238000012544 monitoring process Methods 0.000 claims abstract description 16
- 238000003756 stirring Methods 0.000 claims abstract description 15
- 238000001556 precipitation Methods 0.000 claims description 9
- 238000006731 degradation reaction Methods 0.000 claims description 5
- 238000006396 nitration reaction Methods 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000007547 defect Effects 0.000 abstract description 2
- 238000011369 optimal treatment Methods 0.000 abstract description 2
- 230000001376 precipitating effect Effects 0.000 abstract 1
- 238000011282 treatment Methods 0.000 description 11
- 230000000052 comparative effect Effects 0.000 description 8
- 238000004062 sedimentation Methods 0.000 description 5
- 239000010865 sewage Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000010802 sludge Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000007836 KH2PO4 Substances 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000011081 inoculation Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Classifications
-
- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B19/00—Programme-control systems
- G05B19/02—Programme-control systems electric
- G05B19/04—Programme control other than numerical control, i.e. in sequence controllers or logic controllers
- G05B19/05—Programmable logic controllers, e.g. simulating logic interconnections of signals according to ladder diagrams or function charts
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1263—Sequencing batch reactors [SBR]
-
- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
- G05D21/00—Control of chemical or physico-chemical variables, e.g. pH value
- G05D21/02—Control of chemical or physico-chemical variables, e.g. pH value characterised by the use of electric means
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention relates to the field of SBR process energy-saving methods, in particular to an SBR process oxygen supply energy-saving optimization control method, which solves the defect of poor energy-saving effect in the prior art and comprises the following steps: s1, feeding water for the first time for 5 min; S2-S3, primary aeration; s4, feeding water for the second time and stirring for 80 min; s5, secondary aeration; s6, precipitating for 80 min; s7, draining water for 5 min; s8, standing for 45 min; and S9, next circulation. The change in the reaction process is recorded in real time by the DO, ORP and pH value on-line monitoring instrument, the water quality index of the change point is analyzed at the same time, the characteristic point indicating the reaction process is obtained, the running mode is adjusted according to the characteristic point to carry out real-time monitoring control, and the optimal treatment effect and the minimum energy consumption can be achieved.
Description
Technical Field
The invention relates to the technical field of SBR process energy-saving methods, in particular to an SBR process oxygen supply energy-saving optimization control method.
Background
As most of municipal sewage treatment plants in China adopt secondary treatment plants by an activated sludge method, wherein the energy consumption of aeration and oxygen supply for biological treatment accounts for more than 60 percent of the total energy consumption of the sewage treatment plants, the advantages and disadvantages of an aeration control system directly influence the removal of organic matters and nitrogen in sewage treatment and the operation cost. At present, energy-saving measures of a general sewage treatment plant mainly aim at an aeration stage, and the adopted main method is basically realized by controlling an aeration system through monitored DO value feedback. However, for the energy saving and consumption reduction of the SBR process, due to the combination of anoxic/aerobic working conditions, the DO value is only adopted for feedback, so that the progress of the anoxic working conditions is difficult to reflect, the parameter control method is not perfect, and the energy saving effect is not good. In addition, biological treatment is not only used to remove organic pollutants, but denitrification is also accomplished primarily in biological treatment units. The SBR process can form different aerobic/anoxic/anaerobic environments due to the characteristics of the SBR process, so that the SBR process has a good denitrification effect. How to effectively control the reaction process in the SBR reactor and provide sufficient and excessive oxygen so as to achieve the purposes of carbon removal and denitrification and reduce the energy consumption to the maximum extent is a problem which needs to be solved urgently.
Disclosure of Invention
The invention aims to solve the defect of poor energy-saving effect in the prior art, and provides an oxygen supply energy-saving optimization control method for an SBR process.
In order to achieve the purpose, the invention adopts the following technical scheme:
an oxygen supply energy-saving optimization control method for an SBR process comprises the following steps:
s1, feeding water into the SBR reactor for the first time, monitoring the time of the primary water feeding by the PLC, and stopping the primary water feeding when the time of the primary water feeding reaches a set value;
s2, aerating the SBR reactor for the first time, monitoring DO, ORP and pH value in the reactor by PLC, and when dpH/dt is less than or equal to 0, dDO/dt (n +1) < dDO/dt (n), dORP/dt (n +1) < dORP/dt (n) state lasts for 5min, indicating that DO and ORP curves are greatly increased and a platform is formed subsequently when the DO and ORP curves appear under aerobic condition, and taking the curves as control signals for ending the degradation reaction of organic matters to carry out the next step;
s3, when the dpH/dt is more than or equal to 0 and lasts for 5min, indicating the end point of the continuous descending of the pH curve under the aerobic condition, and taking the end point as a control signal for finishing the nitration reaction, and stopping primary aeration;
s4, feeding water into the SBR reactor for the second time, starting stirring, monitoring the time of the secondary water feeding by the PLC, and stopping the secondary water feeding when the time of the secondary water feeding reaches a set value;
s5, when the state that dpH/dt is less than or equal to 0 lasts for 5min, the point that the pH value is changed from rising to falling under the anaerobic/anoxic condition is indicated as a control signal for ending denitrification, stirring is stopped, and secondary aeration is started;
s6, dpH/dt is less than or equal to 0, dDO/dt (n +1) < dDO/dt (n), dORP/dt (n +1) < dORP/dt (n) continue for 5min, secondary aeration is finished, and precipitation begins;
s7, monitoring the settling time by the PLC, finishing the settling and starting the water drainage when the settling time reaches a set value;
s8, the PLC monitors the drainage time, when the drainage time reaches a set value, the drainage is finished, and the standing is started;
and S9, the PLC monitors the standing time, and when the standing time reaches a set value, the standing is finished and the next cycle is started.
Preferably, the MLSS in the SBR reactor is 3450 mg/L to 3550 mg/L.
Preferably, the primary water inlet time is 5 min.
Preferably, the secondary water feeding and stirring time is 80 min.
Preferably, the precipitation time is 80 min.
Preferably, the drainage time is 5 min.
Preferably, the standing time is 45 min.
The invention has the beneficial effects that:
the change in the reaction process is recorded in real time by the DO, ORP and pH value on-line monitoring instrument, the water quality index of the change point is analyzed at the same time, the characteristic point indicating the reaction process is obtained, the running mode is adjusted according to the characteristic point to carry out real-time monitoring control, and the optimal treatment effect and the minimum energy consumption can be achieved.
Drawings
FIG. 1 is a diagram of an SBR period setting real-time control scheme of the SBR process oxygen supply energy-saving optimization control method provided by the invention;
FIG. 2 is a schematic diagram of the process flow of the SBR apparatus in the oxygen supply energy-saving optimization control method of the SBR process provided by the invention;
FIG. 3 is a real-time control single-cycle DO, ORP, pH change curve of the SBR process oxygen supply energy-saving optimization control method provided by the invention.
In fig. 3: finishing the degradation of the organic matters at the point A, finishing the nitration reaction at the point B, finishing the denitrification reaction at the point C and finishing the degradation of the organic matters of the secondary water inflow at the point D.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
Example (b): an oxygen supply energy-saving optimization control method for an SBR process comprises the following steps:
s1, feeding water into the SBR reactor for the first time, monitoring the time of the primary water feeding by the PLC, and stopping the primary water feeding when the time of the primary water feeding reaches a set value;
s2, aerating the SBR reactor for the first time, monitoring DO, ORP and pH value in the reactor by PLC, and when dpH/dt is less than or equal to 0, dDO/dt (n +1) < dDO/dt (n), dORP/dt (n +1) < dORP/dt (n) state lasts for 5min, indicating that DO and ORP curves are greatly increased and a platform is formed subsequently when the DO and ORP curves appear under aerobic condition, and taking the curves as control signals for ending the degradation reaction of organic matters to carry out the next step;
s3, when the dpH/dt is more than or equal to 0 and lasts for 5min, indicating the end point of the continuous descending of the pH curve under the aerobic condition, and taking the end point as a control signal for finishing the nitration reaction, and stopping primary aeration;
s4, feeding water into the SBR reactor for the second time, starting stirring, monitoring the time of the secondary water feeding by the PLC, and stopping the secondary water feeding when the time of the secondary water feeding reaches a set value;
s5, when the state that dpH/dt is less than or equal to 0 lasts for 5min, the point that the pH value is changed from rising to falling under the anaerobic/anoxic condition is indicated as a control signal for ending denitrification, stirring is stopped, and secondary aeration is started;
s6, dpH/dt is less than or equal to 0, dDO/dt (n +1) < dDO/dt (n), dORP/dt (n +1) < dORP/dt (n) continue for 5min, secondary aeration is finished, and precipitation begins;
s7, monitoring the settling time by the PLC, finishing the settling and starting the water drainage when the settling time reaches a set value;
s8, the PLC monitors the drainage time, when the drainage time reaches a set value, the drainage is finished, and the standing is started;
and S9, the PLC monitors the standing time, and when the standing time reaches a set value, the standing is finished and the next cycle is started.
In the embodiment, MLSS in the SBR reactor is 3450 mg/L-3550 mg/L, the primary water feeding time is 5min, the secondary water feeding and stirring time is 80min, the precipitation time is 20min, the water drainage time is 5min, and the standing time is 45 min.
In the embodiment, the SBR reactor is made of cylindrical organic glass, and the SBR reactor comprises two groups, wherein the inner diameter of a single group is 100mm, the effective height is 1100mm, the effective volume is 8.64L, and the water change amount per cycle is 4.7L. The reactor is generally operated at room temperature, and when the room temperature is lower than 20 ℃ in winter, the temperature of the reactor is controlled to be (23 +/-1) DEG C by a constant-temperature water bath. The water is fed by a submersible pump, the water is drained by gravity, and the aeration adopts a microporous aeration mode at the bottom of the reactor, namely, an air blower introduces air to the bottom of the reactor, and the air is released by a microporous aeration head to oxygenate the reactor so as to fully mix the microorganisms in the reactor with the substrate. The aeration rate is controlled by a rotameter. The time periods and the conversion of the stages of water inlet, aeration, sedimentation, drainage, idling and the like in the reaction process are set according to different experimental requirements, and are connected with a PLC cabinet through an online DO measuring instrument, an ORP measuring instrument and a pH measuring instrument, so that the automatic control is realized.
The water inlet adopts artificial synthetic simulated wastewater, sodium acetate is used as a carbon source, and NH is adopted4Cl as nitrogen source, KH2PO4Is a phosphorus source and, at the same time, is a guaranteeAdding proper trace elements as supplement when the cultured microorganisms need to grow and propagate. The quality of the inlet water is basically stabilized at COD 350mg/L and NH3about-N35 mg/L, adopting common flocculent sludge as inoculation sludge, and MLSS of 3000mg/L, and after the culture, domestication and stabilization, the MLSS in the system is about 3500 mg/L. The whole process of sewage treatment is automatically controlled by a self-made PLC device.
The control flow and the control nodes can be reasonably adjusted according to the treatment requirements and the actual treatment conditions, so that the flow is transformed into water inlet, stirring, aeration, sedimentation, water drainage and standing; or water inlet + primary aeration, stirring, secondary aeration, precipitation, water drainage and standing; or primary water feeding, stirring, secondary water feeding and aeration, sedimentation, water drainage and standing. Including but not limited to the above.
Comparative example one: in the comparative example, the operation mode of water inlet, aeration, precipitation, drainage and standing is adopted, the period is 8 h/period, water is fed for 5min, aeration is carried out for 390min, precipitation is carried out for 5min, drainage is carried out for 6min, and standing is carried out for 74 min. The cycle setting is adjusted at any time according to the running condition and the processing effect.
Comparative example two: in the comparative example, the period of the comparative example I is adjusted to be two times of aeration, 8 h/period, water is fed for 5min, aeration is carried out for 150min, standing is carried out for 90min, secondary aeration is carried out for 150min, sedimentation is carried out for 20min, water is drained for 5min, and standing is carried out for 60 min. The cycle setting is adjusted at any time according to the running condition and the processing effect.
Comparative example three: in the comparative example, the aeration time of the comparative example is reduced, the denitrification process of anoxic anaerobic stirring is added, the period is adjusted to 6 h/period, water is fed for 5min, aeration is carried out for 150min, water is fed for the second time and stirring is carried out for 90min, aeration is carried out for the second time for 30min, sedimentation is carried out for 20min, water is drained for 5min, and standing is carried out for 60 min. The cycle setting is adjusted at any time according to the running condition and the processing effect.
And (3) test results:
the above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (7)
1. An oxygen supply energy-saving optimization control method for an SBR process is characterized by comprising the following steps:
s1, feeding water into the SBR reactor for the first time, monitoring the time of the primary water feeding by the PLC, and stopping the primary water feeding when the time of the primary water feeding reaches a set value;
s2, aerating the SBR reactor for the first time, monitoring DO, ORP and pH value in the reactor by PLC, and when dpH/dt is less than or equal to 0, dDO/dt (n +1) < dDO/dt (n), dORP/dt (n +1) < dORP/dt (n) state lasts for 5min, indicating that DO and ORP curves are greatly increased and a platform is formed subsequently when the DO and ORP curves appear under aerobic condition, and taking the curves as control signals for ending the degradation reaction of organic matters to carry out the next step;
s3, when the dpH/dt is more than or equal to 0 and lasts for 5min, indicating the end point of the continuous descending of the pH curve under the aerobic condition, and taking the end point as a control signal for finishing the nitration reaction, and stopping primary aeration;
s4, feeding water into the SBR reactor for the second time, starting stirring, monitoring the time of the secondary water feeding by the PLC, and stopping the secondary water feeding when the time of the secondary water feeding reaches a set value;
s5, when the state that dpH/dt is less than or equal to 0 lasts for 5min, the point that the pH value is changed from rising to falling under the anaerobic/anoxic condition is indicated as a control signal for ending denitrification, stirring is stopped, and secondary aeration is started;
s6, dpH/dt is less than or equal to 0, dDO/dt (n +1) < dDO/dt (n), dORP/dt (n +1) < dORP/dt (n) continue for 5min, secondary aeration is finished, and precipitation begins;
s7, monitoring the settling time by the PLC, finishing the settling and starting the water drainage when the settling time reaches a set value;
s8, the PLC monitors the drainage time, when the drainage time reaches a set value, the drainage is finished, and the standing is started;
and S9, the PLC monitors the standing time, and when the standing time reaches a set value, the standing is finished and the next cycle is started.
2. The oxygen supply energy-saving optimization control method for the SBR process as claimed in claim 1, wherein the MLSS in the SBR reactor is 3450 mg/L-3550 mg/L.
3. The SBR process oxygen supply energy-saving optimization control method of claim 1, wherein the primary water feeding time is 5 min.
4. The SBR process oxygen supply energy-saving optimization control method of claim 1, wherein the secondary water feeding and stirring time is 80 min.
5. The SBR process oxygen supply energy-saving optimization control method as claimed in claim 1, wherein the precipitation time is 20 min.
6. The SBR process oxygen supply energy-saving optimization control method as claimed in claim 1, wherein the water drainage time is 5 min.
7. The SBR process oxygen supply energy-saving optimization control method of claim 1, wherein the standing time is 45 min.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1569690A (en) * | 2004-03-26 | 2005-01-26 | 彭永臻 | SBR alternant aerobic/anaerobic technology for biological denitrification and real time control device and method thereof |
| CN101182074A (en) * | 2007-11-16 | 2008-05-21 | 北京工业大学 | Real-time controlling method for denitrification by reinforced circulating type active sludge process |
| CN101306878A (en) * | 2008-06-06 | 2008-11-19 | 北京工业大学 | Process control device of CAST step-feed and further denitrification and method |
| CN103936151A (en) * | 2014-04-10 | 2014-07-23 | 北京工业大学 | Efficient nitrogen and phosphorus removal device and method for low carbon source municipal sewage |
| CN104743669A (en) * | 2015-04-03 | 2015-07-01 | 兰州交通大学 | Step-feed CAST nitrite denitrifying phosphorus removal method and process control device thereof |
-
2019
- 2019-12-06 CN CN201911238202.9A patent/CN110968028A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1569690A (en) * | 2004-03-26 | 2005-01-26 | 彭永臻 | SBR alternant aerobic/anaerobic technology for biological denitrification and real time control device and method thereof |
| CN101182074A (en) * | 2007-11-16 | 2008-05-21 | 北京工业大学 | Real-time controlling method for denitrification by reinforced circulating type active sludge process |
| CN101306878A (en) * | 2008-06-06 | 2008-11-19 | 北京工业大学 | Process control device of CAST step-feed and further denitrification and method |
| CN103936151A (en) * | 2014-04-10 | 2014-07-23 | 北京工业大学 | Efficient nitrogen and phosphorus removal device and method for low carbon source municipal sewage |
| CN104743669A (en) * | 2015-04-03 | 2015-07-01 | 兰州交通大学 | Step-feed CAST nitrite denitrifying phosphorus removal method and process control device thereof |
Non-Patent Citations (1)
| Title |
|---|
| 曾华等: "《脉冲式SBR 法处理生活污水的DO、pH、ORP 变化规律研究》", 《工业安全与环保》 * |
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