CN113149218B - Method for adding excess sludge anaerobic fermentation liquor for enhancing municipal sewage SBR treatment effect - Google Patents
Method for adding excess sludge anaerobic fermentation liquor for enhancing municipal sewage SBR treatment effect Download PDFInfo
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- 238000000855 fermentation Methods 0.000 title claims abstract description 145
- 239000010802 sludge Substances 0.000 title claims abstract description 145
- 238000000034 method Methods 0.000 title claims abstract description 44
- 239000010865 sewage Substances 0.000 title claims abstract description 37
- 230000000694 effects Effects 0.000 title claims description 19
- 230000002708 enhancing effect Effects 0.000 title claims description 5
- 238000003756 stirring Methods 0.000 claims abstract description 46
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 14
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 14
- 239000011574 phosphorus Substances 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims description 58
- 239000000203 mixture Substances 0.000 claims description 17
- 230000008569 process Effects 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 230000008859 change Effects 0.000 claims description 13
- 230000035484 reaction time Effects 0.000 claims description 9
- 206010021143 Hypoxia Diseases 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 230000007954 hypoxia Effects 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 230000004151 fermentation Effects 0.000 abstract description 36
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 22
- 238000005273 aeration Methods 0.000 abstract description 22
- 229910052799 carbon Inorganic materials 0.000 abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 12
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 8
- 238000012544 monitoring process Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 229910002651 NO3 Inorganic materials 0.000 description 7
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 7
- 238000002474 experimental method Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 238000012851 eutrophication Methods 0.000 description 2
- 238000011066 ex-situ storage Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/006—Regulation methods for biological treatment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/04—Oxidation reduction potential [ORP]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/40—Liquid flow rate
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
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- Water Supply & Treatment (AREA)
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Abstract
The invention discloses a method for adding excess sludge anaerobic fermentation liquor of an enhanced municipal sewage SBR reactorIn the method, each operation period of the SBR reactor comprises anaerobic water feeding stirring, aeration stirring (aerobic I section), anoxic sludge feeding fermentation liquor stirring (anoxic I section), aeration stirring (aerobic II section), anoxic sludge feeding fermentation liquor stirring (anoxic II section), aeration stirring (aerobic III section) and standing and water drainage operations. By adjusting pH, ORP, ammonia nitrogen, COD and NO in the municipal sewage SBR3 ‑The on-line monitoring can calculate the COD and ammonia nitrogen components in the fermentation liquor reversely, optimize the adding amount of the fermentation liquor and ensure that the total nitrogen of the effluent reaches the standard. The method can reduce the carbon source adding cost of nitrogen and phosphorus removal of the municipal sewage, ensure the effluent quality and improve the recycling potential of the sludge fermentation liquor.
Description
Technical Field
The invention relates to an excess sludge anaerobic fermentation liquor adding method for strengthening municipal sewage SBR treatment effect, mainly solving the problems of poor total nitrogen removal effect or secondary pollution caused by excessive adding due to unstable components of the excess sludge anaerobic fermentation liquor, and belongs to the technical field of sewage treatment and sludge recycling application.
Background
In recent years, water body pollution and eutrophication events occur frequently, so that the social economy of China suffers great loss, and one of the main causes of the water body pollution and the eutrophication events is the overproof discharge of nitrogen. Because municipal sewage is low in carbon and nitrogen, the denitrification efficiency is affected due to insufficient organic matters, and the municipal sewage is difficult to discharge after reaching the standard. In practical application, sodium acetate, methanol and the like are often required to be added as external carbon sources to achieve the denitrification effect, but the addition cost is high, the wide application is difficult in practical operation, the sludge fermentation liquor contains more soluble organic matters, including volatile fatty acids with the potential of being the external carbon sources, and the sludge fermentation liquor can be used as a supplementary carbon source of a sewage biological denitrification process, so that a new way is developed for the reduction and resource utilization of the sludge.
The component concentration of the anaerobic fermentation liquor of the excess sludge fluctuates, and if the addition is insufficient, the denitrification and dephosphorization effects of the SBR reactor are poor, and the effluent quality is influenced; if the addition amount is excessive, the aeration amount is increased, the energy consumption and the operation cost of the system are improved, more ammonia nitrogen, phosphorus and the like are introduced, the sewage treatment load is increased, and the risk that the nitrogen and phosphorus of the effluent and even organic matters exceed the standard is increased. Therefore, a more accurate automatic adding method of the excess sludge anaerobic fermentation liquid is needed to effectively avoid the problems, and the method has important significance for the economic, efficient and stable operation of municipal sewage plants.
Disclosure of Invention
The invention aims to solve the problems of insufficient or waste carbon source and the like caused by the fact that the adding of the excess sludge anaerobic fermentation liquor in the prior art cannot be dynamically adjusted according to the quality of inlet water and the components of the excess sludge anaerobic fermentation liquor, and provides an excess sludge anaerobic fermentation liquor adding method for enhancing the treatment effect of municipal sewage SBR.
The invention adopts the following specific technical scheme:
the invention provides a method for adding excess sludge anaerobic fermentation liquor for strengthening the treatment effect of municipal sewage SBR, which comprises the following steps:
s1: under the anaerobic condition, adding municipal sewage to be treated into the SBR reactor after the sludge domestication, and fully stirring;
s2: fully stirring municipal sewage in the SBR under an aerobic condition, and marking the process as an aerobic I section;
s3: under the anoxic condition, adding excess sludge anaerobic fermentation liquor into the SBR reactor after aerobic I-section treatment, and fully stirring the mixture, wherein the process is marked as an anoxic I-section; in the mixture, the concentration ratio of C/N is 5; at the initial stage of adding the excess sludge anaerobic fermentation liquid, obtaining NH of the added excess sludge anaerobic fermentation liquid through the change of pH and ORP of the mixture in the SBR reactor4 +-N predicted concentration, C/N predicted range and COD predicted concentration;
s4: under aerobic condition, fully stirring the mixture treated in the anoxic I section in the SBR reactor, and marking the process as an aerobic II section;
s5: continuously adding excess sludge anaerobic fermentation liquor into the SBR reactor treated by the aerobic II section under the anoxic condition, and fully stirring, wherein the process is marked as an anoxic II section; the volume of the excess sludge anaerobic fermentation liquid added in the anoxic II stage passes through the COD concentration and NH in the SBR reactor after the aerobic II stage4 +-N concentration and NO3 -N concentration, and NH of the excess sludge anaerobic fermentation broth obtained by the step S34 +-N predicted concentration and COD predicted concentration;
s6: under aerobic condition, fully stirring the mixture treated in the anoxic II section in the SBR reactor, and marking the process as an aerobic III section;
s7: and (3) standing the SBR reactor treated by the aerobic III section, and then discharging the municipal sewage treated by the SBR reactor.
Preferably, the COD concentration of the municipal sewage is 158-160 mg/L, the TKN concentration is 50-52 mg/L, and the total phosphorus concentration is 6.5-7 mg/L.
Preferably, in each of the steps S1 to S5, the stirring time is 1 h; in step S6, stirring for 30 min; the time taken for step S7 is 30 min.
Preferably, the COD concentration of the added excess sludge anaerobic fermentation liquid is 4000-6000 mg/L, the ammonia nitrogen concentration is 300-540 mg/L, the total phosphorus concentration is 200-300 mg/L, and the pH value is 9-9.5.
Preferably, in the anoxic I section, the adding volume of the residual sludge anaerobic fermentation liquid is calculated by formulas (1) to (3),
N’＝2.23R’+705.75 (2)
in the formula, M1The adding volume of the residual sludge anaerobic fermentation liquid in the anoxic I section is L; v is the total effective volume of the SBR reactor and the unit L; c1The COD concentration in the SBR reactor at the end of the aerobic I section is in mg COD/L; n is a radical of1For NH in the SBR reactor at the end of the aerobic section I4 +-N concentration in mg N/L; n is1For NO in the SBR reactor at the end of the aerobic section I3 --N concentration in mg N/L; c' is the predicted COD concentration of the anaerobic fermentation liquor of the residual sludge at the end of the anoxic I section in the period of the previous SBR reactor, and the unit mg COD/L; r' is the minimum value of ORP in the initial stage of adding the residual sludge anaerobic fermentation liquid in the anoxic I stage in the period of the last SBR reactor, and the unit is mv; k' is the slope value of the pH-t linear fitting curve of the anoxic I section in the previous SBR reactor period; b' is a parameter in the ORP-t fitted curve of the anoxic I segment in the previous SBR reactor cycle, which is in the form of y ═ a × ln (-B × ln (x)); n' is NH of the anaerobic fermentation liquor of the excess sludge at the end of the anoxic I section in the previous SBR reactor period4 +-predicted concentration of N in mg N/L; if the SBR reactor is the first period, the C value is any value within the range of 4000-7200 mg COD/L, and the N' value is any value within the range of 300-540 mg N/L.
Preferably, in step S3, NH of the excess sludge anaerobic fermentation broth4 +The predicted N concentration, the predicted C/N range and the predicted COD concentration are calculated by the formulas (4) to (6) respectively,
N＝2.23R+705.75 (4)
C/N＝(-62.42B-4.21,9134.68k-73.73) (5)
in the formula, N is NH of the anaerobic fermentation liquor of the excess sludge4 +-predicted concentration of N in mg N/L; C/N is the C/N prediction range of the excess sludge anaerobic fermentation liquor; c is the COD predicted concentration of the anaerobic fermentation liquor of the excess sludge, and the unit mg COD/L; r is anoxic I-stage addition residueThe minimum value of ORP in the initial stage of the residual sludge anaerobic fermentation liquid is mv; k is the slope value of the pH-t linear fitting curve in the anoxic I section; b is a parameter in the ORP-t fitted curve in hypoxia I segment, which is of the form y ═ a × ln (-B × ln (x)).
Further, in the step S5, the volume of the excess sludge anaerobic fermentation liquid added in the anoxic II stage is calculated by the formulas (7) and (8),
in the formula, M is the adding mass of the residual sludge anaerobic fermentation liquid in the anoxic section II, and the unit mg of COD is; v is the adding volume of the residual sludge anaerobic fermentation liquid in the anoxic II section, and the unit L is; v is the total effective volume of the SBR reactor and the unit L; c2The COD concentration in the SBR reactor at the end of the aerobic section II is mgCOD/L; n is a radical of2For NH in the SBR reactor at the end of the aerobic II section4 +-N concentration in mg N/L; n is2Is NO in SBR reactor at the end of aerobic II section3 --N concentration in mg N/L; t is the set time of the anoxic II section; t is denitrification reaction time in the anoxic section II; t is t0Compensating time for adding the excess sludge anaerobic fermentation liquor; wherein, t + t0≤T。
Further, the denitrification reaction time t in the anoxic II section is determined by the following method:
starting from the addition of the residual sludge anaerobic fermentation liquid in the anoxic II section, respectively obtaining the change rate K of the pH along with the time according to the formula (8) and the formula (9) through the change curves of the pH and the ORP along with the time in the SBR reactorpHAnd the rate of change K of ORP with timeORP(ii) a When K ispHIs changed from positive to negative and KORPWhen the value is equal to 0, the denitrification reaction is ended, and the time is the denitrification reaction time t in the anoxic II section; the equations (9) and (10) are specifically as follows:
KpH＝(pHi-pHi-1)/(ti-ti-1) (9)
KORP＝(ORPi-ORPi-1)/(ti-ti-1) (10)。
furthermore, the adding compensation time t of the excess sludge anaerobic fermentation liquor0Is determined by the following method:
when the effluent NO of the SBR reactor of the previous period3 -The concentration of N is less than or equal to the first control value TNdWhen it is, let t03 min; when TN>TNdAnd NH in the SBR reactor at the end of the last period of the anoxic II section4 +Concentration of-N-NH4 +-TN>Second control value NH4 +-NdLet t 02 min; when TN>TNdAnd NH4 +-N≤NH4 +-NdLet t0＝4min。
Preferably, the initial stage is the first 10min after adding the excess sludge anaerobic fermentation broth in the anoxic stage I.
Compared with the prior art, the invention has the following beneficial effects:
according to the invention, the concentration of components such as COD (chemical oxygen demand), ammonia nitrogen and the like in the added sludge fermentation liquor can be calculated on line according to the change of pH and ORP (oxidation-reduction potential) signals after the fermentation liquor is added into the anoxic I section of the SBR reactor every day, the adding amount of a carbon source (sludge fermentation liquor) in the subsequent anoxic II section is adjusted in real time, the excessive or insufficient adding of the carbon source caused by the larger fluctuation of the components of the fermentation liquor is avoided, the stable effluent quality is ensured, and the aeration energy consumption and the fermentation liquor consumption are reduced. That is to say, the invention can correct the component conditions of the anoxic section I and the anoxic section II in time, thereby dynamically adjusting the fed fermentation liquor amount, avoiding the conditions of insufficient or wasted carbon source and the like, and influencing the operation effect of the SBR reactor.
Drawings
FIG. 1 is a schematic flow diagram of the dosing method of the present invention;
FIG. 2 is a fitting curve graph of pH and t after adding excess sludge anaerobic fermentation broth in anoxic section I;
FIG. 3 is a fitting curve graph of ORP and t after adding excess sludge anaerobic fermentation broth in an anoxic I section;
FIG. 4 shows NH in anaerobic fermentation broth of excess sludge in anoxic stage I4 +-a fitted plot of N concentration versus ORPmin;
FIG. 5 is a fitting curve graph of C/N and B in the anaerobic fermentation broth of excess sludge in the anoxic I stage;
FIG. 6 is a fitting curve diagram of C/N and k in the anaerobic fermentation liquor of the excess sludge in the anoxic I section.
Detailed Description
The invention will be further elucidated and described with reference to the drawings and the detailed description. The technical features of the embodiments of the present invention can be combined correspondingly without mutual conflict.
The invention provides a method for adding excess sludge anaerobic fermentation liquor for enhancing the treatment effect of municipal sewage SBR, wherein each operation period of an SBR reactor comprises anaerobic water inlet stirring, aeration stirring (aerobic I section), anoxic sludge inlet fermentation liquor stirring (anoxic I section), aeration stirring (aerobic II section), anoxic sludge inlet fermentation liquor stirring (anoxic II section), aeration stirring (aerobic III section), standing and drainage operations. The method can be operated by matching with a commercially-used SBR reactor, and the structure of the SBR reactor (reaction system) is briefly described as follows:
the main structure of the reaction system comprises a water inlet tank, an SBR reactor main body, a water outlet tank, a sludge fermentation liquid tank and an online controller, wherein the water inlet tank is connected with a water inlet of the SBR reactor main body through a water inlet pump, the water outlet tank is connected with a water outlet of the SBR reactor main body through a water discharge pump, and the sludge fermentation liquid tank is connected with a carbon source inlet of the SBR reactor main body through a carbon source pump. The SBR reactor main body comprises an aeration device, a stirring device and the like, and is provided with a pH/ORP sensor, COD and NH4 +-N、NO3 --N on-line monitors, etc. Wherein, for better on-line control of the reaction system, a water inlet pump, a carbon source pump, a water pump, a carbon source pump, a reactor and a reactor can be arranged in the reactor,The drainage pump, the aeration device, the stirring device and other equipment are all connected with the online controller. In this example, the total effective volume of the SBR reactor body was 11L.
In the reaction system with the structure, firstly, sludge domestication is needed to be carried out on the SBR reactor, and the sludge domestication can be carried out by adopting a common method in the prior art, namely activated sludge in a secondary sedimentation tank of a sewage treatment plant is inoculated into the SBR reactor, so that the sludge concentration in the reactor reaches 3000-5000 mg/L; artificially preparing sewage with low carbon-nitrogen ratio, feeding water in an anaerobic section for one time, and carrying out anaerobic treatment for 40min at a stirring speed of 100 r/min; aerobic aeration is carried out for 150min, the aeration rate is 2L/min, and the dissolved oxygen is more than 4 mg/L; and (3) carrying out anoxic stirring for 120min, precipitating and draining for 50min, stabilizing the process after 15 hours of operation, keeping the hydraulic retention time for 8 hours, adjusting the retention time of sludge to be kept for 15 days, and finally keeping the concentration of the sludge to be 2500-3000 mg/L after stable operation. The sludge fermentation liquor adding method is adopted in the SBR reactor after the sludge acclimation, and the operation steps and the processes are as follows:
s1: anaerobic water feeding and stirring: under anaerobic conditions, the municipal sewage to be treated is added to the SBR reactor and stirred well. That is to say, start the intake pump and pump the municipal sewage pump that treats into SBR reactor main part to start agitating unit, this stage is mainly that phosphorus accumulating bacteria utilizes the carbon source in the municipal sewage to carry out abundant phosphorus release reaction.
In practical application, in order to achieve a better treatment effect, the COD concentration of the municipal sewage is preferably controlled to be 158-160 mg/L, the TKN concentration is preferably controlled to be 50-52 mg/L, and the total phosphorus concentration is preferably controlled to be 6.5-7 mg/L.
In this example, the municipal sewage was supplied at a C/N concentration ratio of 3, and the operation time at this stage was 1 hour.
S2: aeration stirring (aerobic I section): under aerobic conditions, municipal sewage in the SBR reactor is fully stirred. That is to say, after the anaerobic water inlet stirring stage is finished, the air pump is started to carry out aeration treatment on the reactor, nitrification reaction and aerobic phosphorus absorption reaction mainly occur in the stage, ammonia nitrogen in municipal sewage is converted into nitrate, residual organic matters in the municipal sewage are removed, and at the moment, phosphorus accumulating bacteria absorb a large amount of phosphorus.
In the present embodiment, in order to achieve a better processing effect, the operation time of this stage may be set to 1 h.
S3: stirring anoxic sludge fermentation liquor (anoxic section I): under the anoxic condition, adding the excess sludge anaerobic fermentation liquor into the SBR reactor after the aerobic I-section treatment, and fully stirring the mixture. That is, after the aerobic stage I is finished, the air pump is closed to stop aeration, the sludge fermentation broth carbon source pump is started to pump the residual sludge anaerobic fermentation broth with a quantitative volume into the SBR reactor, and the stirring device is started at the same time, so that the SBR reactor utilizes municipal sewage and the residual sludge anaerobic fermentation broth as carbon sources to perform denitrification reaction.
In practical application, in order to realize better treatment effect, the COD concentration of the added excess sludge anaerobic fermentation liquid is 4000-6000 mg/L, the ammonia nitrogen concentration is 300-540 mg/L, the total phosphorus concentration is 200-300 mg/L, and the pH value is 9-9.5. The operation time of this stage may be set to 1 h. Meanwhile, the concentration ratio of C/N (namely the ratio of COD concentration to the total concentration of ammonia nitrogen and nitrate nitrogen) in the mixture is 5 by adjusting the adding volume of the excess sludge anaerobic fermentation liquor. Specifically, the adding volume of the excess sludge anaerobic fermentation liquid can be calculated by formulas (1) to (3), and the formulas (1) to (3) are as follows:
N’＝2.23R’+705.75 (2)
in the formula, M1The adding volume of the residual sludge anaerobic fermentation liquid in the anoxic I section is L. V is the total effective volume of the SBR reactor in L. C1The COD concentration in the SBR reactor at the end of the aerobic I section is in mg COD/L. N is a radical of1For NH in the SBR reactor at the end of the aerobic section I4 +-N concentration in mg N/L。n1Is NO in SBR reactor at the end of aerobic section I3 -N concentration in mg N/L. C' is the calculated COD predicted concentration of the anaerobic fermentation liquid of the excess sludge, the unit mg COD/L and the application range is 4000-7200 mg COD/L. N' is calculated NH of the residual sludge anaerobic fermentation liquid4 +The predicted concentration of N is unit mg N/L, and the application range is 300-540 mg N/L. If the SBR reactor is in the first period (namely the initial operation period), the C value is any value within the range of 4000-7200 mg COD/L, and the N' value is any value within the range of 300-540 mg N/L. R' is the minimum value of ORP in the initial stage of adding the residual sludge anaerobic fermentation liquid in the anoxic I stage in the period of the SBR reactor, the unit is mv, and the application range is-64 mv to-172 mv. And k' is the slope value of the pH-t linear fitting curve of the anoxic I section in the previous SBR reactor period, and the application range is 0.009-0.0106. B' is a parameter in an ORP-t fitting curve of the anoxic I section in the previous SBR reactor period, the fitting curve is in the form of y-A x ln (-B x ln (x)), and the applicable range is-0.20898 to-0.45065. Wherein, the initial stage generally refers to the first 10min after adding the excess sludge anaerobic fermentation liquor in the anoxic I stage.
Meanwhile, in the initial stage after the excess sludge anaerobic fermentation liquid is added into the SBR reactor, NH of the added excess sludge anaerobic fermentation liquid is obtained through the signal change of the pH and ORP of the mixture in the SBR reactor4 +-predicted concentration of N, predicted range of C/N and predicted concentration of COD. It should be noted that, because of the particularity of the excess sludge anaerobic fermentation liquid, the concentrations and the proportions of the components of the excess sludge anaerobic fermentation liquid are constantly fluctuated, so that the theoretical fixed values of the components of the added excess sludge anaerobic fermentation liquid need to be obtained through calculation, so as to facilitate the subsequent calculation of the volume of the excess sludge anaerobic fermentation liquid to be added in the anoxic II stage. The method for calculating the theoretical fixed value of each component of the added excess sludge anaerobic fermentation liquid comprises the following steps: NH of anaerobic fermentation liquid of excess sludge4 +The predicted N concentration, the predicted C/N range and the predicted COD concentration are calculated by the formulas (4) to (6) respectively,
N＝2.23R+705.75 (4)
C/N＝(-62.42B-4.21,9134.68k-73.73) (5)
in the formula, N is NH of excess sludge anaerobic fermentation liquor4 +The predicted concentration of N is in unit of mg N/L, and the application range is 300-540 mg N/L. And C/N is the C/N prediction range of the excess sludge anaerobic fermentation liquid. C is the COD predicted concentration of the residual sludge anaerobic fermentation liquid, the unit mg COD/L is, and the application range is 4000-7200 mg COD/L. R is the minimum value of ORP in the initial stage of adding the anaerobic fermentation liquor of the excess sludge into the anoxic I section, and the application range is-64 mv to-172 mv. k is a slope value of a pH-t linear fitting curve, and the application range is 0.009-0.0106. B is a parameter in the ORP-t fitted curve, which is in the form of y ═ a × ln (-B × ln (x)), with a range of applicability from-0.20898 to-0.45065.
In the embodiment, the volume of the added excess sludge anaerobic fermentation liquid is 0.1L calculated by a formula, so that the concentration ratio of C/N in the added mixture is 5, and the running time of the stage is 1 h. In this embodiment, by performing the non-in-situ denitrification experiment of the SBR sludge, the following three fitting curves are obtained to calculate the ammonia nitrogen and COD concentrations of the sludge fermentation liquid:
1) NH of sludge fermentation broth4 +-N concentration-ORPmin fitted curve:
taking 125mLSBR sludge, adding sludge fermentation liquor containing ammonia nitrogen and COD with different concentrations as a carbon source to enable the C/N to be 5, starting a denitrification experiment under an anoxic condition, monitoring an ORP value on line, and making an ORP-t diagram as shown in figure 3. As the reaction proceeds, the ORP decreases, with a minimum value ORPmin. According to ORPmin and fermentation liquor NH under the condition of different fermentation liquor components4 +-N concentration, making ORPmin-NH4 +The fitted curve of-N is shown in FIG. 4, and the formula is "N is 2.23R +705.75, wherein R is the minimum ORP, and N is the ammonia nitrogen concentration of the fermentation broth".
2) C/N ratio of sludge fermentation liquor and parameter k are fitted with a curve:
ex situ denitrification experiments were performed as above withoutThe same pH-t curve at C/N, where y is pH and x is time t, is fitted with the function y ═ kx + b. The resulting curve is shown in fig. 2. The linear relation between C/N and the parameter k is shown in FIG. 5, and the formula is C/N-9134.68B-73.73, wherein C/N is sludge fermentation broth COD and NH4 +The ratio of N concentrations, k being a parameter of the pH-t fitted curve.
3) C/N ratio of the sludge fermentation liquor and the parameter B are fitted with a curve:
ex situ denitrification experiments were performed as above and ORP-t curves were made at different C/N and the fit was in the form of y ═ a × ln (-B × ln (x)), where y is ORP, x is time t and B is the parameters of the ORP-t fitted curve. Further, the linear relationship between the parameter B and the fermentation broth C/N is shown in fig. 6, and the formula is-62.42B-4.21, where C/N is the ratio of sludge fermentation broth COD to NH4+ -N concentration.
S4: aeration stirring (aerobic II section): and fully stirring the mixture treated in the anoxic I section in the SBR reactor under the aerobic condition. That is, after the anoxic I stage, the air pump is started to perform aeration treatment on the SBR reactor, nitrification reaction mainly occurs in the stage, ammonia nitrogen in inlet water is converted into nitrate, and meanwhile, residual organic matters are removed.
In the present embodiment, in order to achieve a better processing effect, the operation time of this stage may be set to 1 h.
S5: stirring anoxic sludge fermentation liquor (anoxic section II): and under the anoxic condition, continuously adding the excess sludge anaerobic fermentation liquor into the SBR reactor after the aerobic II-stage treatment, and fully stirring. That is, after the aerobic section II is finished, the air pump is closed to stop aeration, the excess sludge anaerobic fermentation broth carbon source pump is started to continuously pump the excess sludge anaerobic fermentation broth into the SBR reactor, and the stirring device is started at the same time, so that the reactor utilizes the excess sludge anaerobic fermentation broth as a carbon source to generate denitrification reaction.
The volume of the excess sludge anaerobic fermentation liquid added in the stage passes through the COD concentration and NH in the SBR reactor after the aerobic II stage4 +-N concentration and NO3 -N concentration, and the residual sludge anaerobic fermentation broth NH obtained by step S34 +-predicted concentration of N and predicted concentration of COD. The method comprises the following specific steps:
the volume of the excess sludge anaerobic fermentation liquid added in the anoxic II section is calculated by the formulas (7) and (8),
in the formula, M is the adding mass of the residual sludge anaerobic fermentation liquid in the anoxic II section, and the unit mg COD is. v is the adding volume of the residual sludge anaerobic fermentation liquid in the anoxic II section, and the unit L is the adding volume of the residual sludge anaerobic fermentation liquid. V is the total effective volume of the SBR reactor in L. C2The COD concentration in the SBR reactor at the end of the aerobic section II is in mg COD/L. N is a radical of2NH in the SBR reactor at the end of the aerobic II section4 +N concentration in mg N/L. n is2Is NO in SBR reactor at the end of aerobic II section3 -N concentration in mg N/L. C is the COD predicted concentration of the excess sludge anaerobic fermentation liquid calculated by the formula (5), the unit mg COD/L is, and the application range is 4000-7200 mg COD/L. N is NH of the excess sludge anaerobic fermentation liquid calculated by the formula (3)4 +The predicted concentration of N is unit mg N/L, and the application range is 300-540 mg N/L. T is the set time of the anoxic II section, and the set time can be selected and set according to actual conditions.
t is the denitrification reaction time in the anoxic II section. The denitrification reaction time t in the anoxic II stage is determined by the following method: from the beginning of adding the excess sludge anaerobic fermentation liquid in the anoxic II section, monitoring the pH and the ORP on line every 30s, and respectively obtaining the change rate K of the pH along with the time according to the formula (8) and the formula (9) through the change curves of the pH and the ORP along with the time in the SBR reactorpHAnd the rate of change K of ORP with timeORPWherein t isi-ti-130 s. When K ispHIs changed from positive to negative and KORPWhen the value is equal to 0, the denitrification reaction is ended, and the time is hypoxia IIDenitrification reaction time t in the section. The formulas (9) and (10) are specifically as follows:
KpH＝(pHi-pHi-1)/(ti-ti-1) (9)
KORP＝(ORPi-ORPi-1)/(ti-ti-1) (10)。
t0the compensation time for adding the excess sludge anaerobic fermentation liquid. Wherein, t + t0T is less than or equal to T. Compensating time t for adding excess sludge anaerobic fermentation liquor0Is determined by the following method: when the effluent NO of the SBR reactor of the previous period3 -The concentration of N is less than or equal to the first control value TNdWhen it is, let t03 min. When TN>TNdAnd NH in the SBR reactor at the end of the last period of the anoxic II section4 +Concentration of-N-NH4 +-TN>Second control value NH4 +-NdLet t02 min. When TN>TNdAnd NH4 +-N≤NH4 +-NdLet t04 min. In practical application, the specific value of the time can be adjusted according to practical situations.
In the present embodiment, in order to achieve a better processing effect, the operation time of this stage may be set to 1 h.
S6: aeration stirring (aerobic section III): and (3) fully stirring the mixture treated in the anoxic II stage in the SBR reactor under the aerobic condition, and marking the process as an aerobic III stage. That is, after the anoxic section II is finished, the air pump is started to perform aeration treatment on the SBR reactor, nitrification reaction mainly occurs in the stage, ammonia nitrogen in inlet water is converted into nitrate, and meanwhile, residual organic matters are removed.
In the present embodiment, in order to achieve a better processing effect, the operation time of this stage may be set to 0.5 h.
S7: standing and draining: standing the SBR reactor treated by the aerobic III section, and then discharging the municipal sewage treated by the denitrification and dephosphorization of the SBR reactor. That is, when the aerobic stage III is finished, the stirring device and the aeration device are closed, the mixture is placed still and settled, then the drainage pump is started, and the supernatant is drained through the drainage valve, wherein the drainage ratio can be 70%.
In this embodiment, in order to achieve a better treatment effect, the operation time for the standing precipitation may be set to 20min, and the drainage time may be set to 10 min.
In the process, the pH, ORP, COD and NH of the SBR reactor can be collected4 +-N、NO3 -And the instrument parameters such as-N and the like are provided for an online controller, the online controller sends a control signal to a sludge fermentation liquid carbon source pump according to the parameters, and the carbon source adding time of the fermentation liquid is controlled online, so that full-automatic unmanned operation is realized.
The effluent treated by the SBR reactor can reach the national discharge standard, and compared with the conventional SBR reactor operation process, the method not only obviously improves the effluent effect, but also can effectively avoid excessive or insufficient carbon source addition caused by large fluctuation of fermentation liquor components, and reduces the aeration energy consumption and the fermentation liquor consumption while ensuring the effluent quality to be stable and up to the standard.
The above-described embodiments are merely preferred embodiments of the present invention, which should not be construed as limiting the invention. Various changes and modifications may be made by one of ordinary skill in the pertinent art without departing from the spirit and scope of the present invention. Therefore, the technical scheme obtained by adopting the mode of equivalent replacement or equivalent transformation is within the protection scope of the invention.
Claims (4)
1. A method for adding excess sludge anaerobic fermentation liquor for enhancing the treatment effect of municipal sewage SBR is characterized by comprising the following steps:
s1: under the anaerobic condition, adding municipal sewage to be treated into the SBR reactor after the sludge domestication, and fully stirring;
s2: fully stirring municipal sewage in the SBR under an aerobic condition, and marking the process as an aerobic I section;
s3: under the condition of oxygen deficiency, the sewage flows through an aerobic I sectionAdding excess sludge anaerobic fermentation liquor into the treated SBR reactor, and fully stirring the mixture, wherein the process is marked as an anoxic section I; in the mixture, the concentration ratio of C/N is 5; at the initial stage of adding the excess sludge anaerobic fermentation liquid, obtaining NH of the added excess sludge anaerobic fermentation liquid through the change of pH and ORP of the mixture in the SBR reactor4 +-N predicted concentration, C/N predicted range and COD predicted concentration;
s4: under aerobic condition, fully stirring the mixture treated in the anoxic I section in the SBR reactor, and marking the process as an aerobic II section;
s5: continuously adding excess sludge anaerobic fermentation liquor into the SBR reactor after the aerobic II section treatment under the anoxic condition, and fully stirring, wherein the process is marked as an anoxic II section; the volume of the excess sludge anaerobic fermentation liquid added in the anoxic II stage passes through the COD concentration and NH in the SBR reactor after the aerobic II stage4 +-N concentration and NO3 -N concentration, and the residual sludge anaerobic fermentation broth NH obtained by step S34 +-the predicted concentration of N and the predicted concentration of COD are obtained;
s6: under aerobic condition, fully stirring the mixture treated in the anoxic II section in the SBR reactor, and marking the process as an aerobic III section;
s7: standing the SBR reactor treated by the aerobic III section, and then discharging the municipal sewage treated by the SBR reactor;
in the anoxic I section, the adding volume of the anaerobic fermentation liquor of the excess sludge is calculated by formulas (1) to (3),
N’＝2.23R’+705.75 (2)
in the formula, M1Is short ofAdding volume of the residual sludge anaerobic fermentation liquid in the oxygen I section, wherein the unit is L; v is the total effective volume of the SBR reactor and is unit L; c1The COD concentration in the SBR reactor at the end of the aerobic I section is in mg COD/L; n is a radical of1For NH in the SBR reactor at the end of the aerobic section I4 +-N concentration in mg N/L; n is1Is NO in SBR reactor at the end of aerobic section I3 --N concentration in mg N/L; c' is the predicted COD concentration of the anaerobic fermentation liquor of the residual sludge at the end of the anoxic I section in the period of the previous SBR reactor, and the unit mg COD/L; r' is the minimum value of ORP in the initial stage of adding the residual sludge anaerobic fermentation liquid in the anoxic I stage in the period of the last SBR reactor, and the unit is mv; k' is the slope value of the pH-t linear fitting curve of the anoxic I section in the previous SBR reactor period; b' is a parameter in the ORP-t fitted curve of the anoxic I segment in the previous SBR reactor cycle, which is in the form of y ═ a × ln (-B × ln (x)); n' is NH of the anaerobic fermentation liquor of the excess sludge at the end of the anoxic I section in the previous SBR reactor period4 +-predicted concentration of N in mg N/L; if the SBR is in the first period, the C value is any value within the range of 4000-7200 mg COD/L, and the N' value is any value within the range of 300-540 mg N/L;
in the step S3, NH of the excess sludge anaerobic fermentation liquid4 +The predicted N concentration, the predicted C/N range and the predicted COD concentration are calculated by the formulas (4) to (6) respectively,
N＝2.23R+705.75 (4)
C/N＝(-62.42B-4.21,9134.68k-73.73) (5)
in the formula, N is NH of excess sludge anaerobic fermentation liquor4 +-predicted concentration of N in mg N/L; C/N is the C/N prediction range of the excess sludge anaerobic fermentation liquor; c is the COD predicted concentration of the anaerobic fermentation liquor of the excess sludge, and the unit mg COD/L; r is the minimum value of ORP in the initial stage of adding the anaerobic fermentation liquor of the excess sludge in the anoxic I stage and the unit is mv(ii) a k is the slope value of the pH-t linear fitting curve in the anoxic I section; b is a parameter in the ORP-t fitted curve in hypoxia I segment, of the form y ═ a × ln (-B × ln (x));
in step S5, the volume of the excess sludge anaerobic fermentation liquid added in the anoxic II section is calculated by the formulas (7) and (8),
in the formula, M is the adding mass of the residual sludge anaerobic fermentation liquid in the anoxic II section, and the unit mg COD is the adding mass of the residual sludge anaerobic fermentation liquid; v is the adding volume of the residual sludge anaerobic fermentation liquid in the anoxic II section, and the unit L is; v is the total effective volume of the SBR reactor and is unit L; c2The COD concentration in the SBR reactor at the end of the aerobic II section is in mg COD/L; n is a radical of2For NH in the SBR reactor at the end of the aerobic II section4 +-N concentration in mg N/L; n is2For NO in the SBR reactor at the end of the aerobic II section3 --N concentration in mg N/L; t is the set time of the anoxic II section; t is denitrification reaction time in the anoxic II section; t is t0Compensating time for adding the excess sludge anaerobic fermentation liquor; wherein, t + t0≤T；
The denitrification reaction time t in the anoxic II section is determined by the following method:
starting from the addition of the residual sludge anaerobic fermentation liquid in the anoxic II section, respectively obtaining the change rate K of the pH along with the time according to the formula (8) and the formula (9) through the change curves of the pH and the ORP along with the time in the SBR reactorpHAnd the rate of change K of ORP with timeORP(ii) a When K ispHIs changed from positive to negative and KORPWhen the value is equal to 0, the denitrification reaction is ended, and the time is the denitrification reaction time t in the anoxic II section; the equations (9) and (10) are specifically as follows:
KpH＝(pHi-pHi-1)/(ti-ti-1) (9)
KORP＝(ORPi-ORPi-1)/(ti-ti-1) (10)；
the compensation time t for adding the excess sludge anaerobic fermentation liquor0Is determined by the following method:
when the effluent NO of the SBR reactor of the previous period3 -The concentration of N is less than or equal to the first control value TNdWhen it is, let t03 min; when TN>TNdAnd NH in the SBR reactor at the end of the last period of the anoxic II section4 +Concentration of-N-NH4 +-TN>Second control value NH4 +-NdLet t02 min; when TN>TNdAnd NH4 +-N≤NH4 +-NdLet t0＝4min；
The initial stage is the first 10min after adding the excess sludge anaerobic fermentation broth in the anoxic I stage.
2. The adding method of the excess sludge anaerobic fermentation liquid as claimed in claim 1, wherein the municipal sewage has a COD concentration of 158-160 mg/L, a TKN concentration of 50-52 mg/L, and a total phosphorus concentration of 6.5-7 mg/L.
3. The method for adding the excess sludge anaerobic fermentation broth according to claim 1, wherein in the steps S1-S5, the stirring time is 1 h; in step S6, stirring for 30 min; the time taken for step S7 is 30 min.
4. The method for adding the excess sludge anaerobic fermentation liquid according to claim 1, wherein the COD concentration of the added excess sludge anaerobic fermentation liquid is 4000-6000 mg/L, the ammonia nitrogen concentration is 300-540 mg/L, the total phosphorus concentration is 200-300 mg/L, and the pH value is 9-9.5.
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