CN114349290A - Enhanced phosphorus removal method based on MBBR sewage treatment process - Google Patents
Enhanced phosphorus removal method based on MBBR sewage treatment process Download PDFInfo
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Abstract
The invention relates to a method for strengthening phosphorus removal based on an MBBR sewage treatment process, which comprises the steps of treating sewage in an anaerobic tank, an anoxic tank, an MBBR tank and a sedimentation tank in sequence, discharging the obtained effluent, directly returning part of the obtained precipitated sludge to the anaerobic tank, sending part of the obtained precipitated sludge to a hydrolysis fermentation unit for treatment, obtaining hydrolysis fermentation mixed liquid, and returning the obtained hydrolysis fermentation mixed liquid to the anaerobic tank to finish the process. Compared with the prior art, the method has the advantages that activated sludge generated in the domestic sewage process is subjected to hydrolytic fermentation to generate easily degradable organic matters (rbCOD) and Volatile Fatty Acids (VFAs), the defects of intake water VFAs are supplemented, the phosphorus removal effect of a sewage plant is improved, the demand on an external carbon source is reduced, the aeration energy consumption is reduced, and the use of phosphorus removal agents is reduced.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and relates to an enhanced phosphorus removal method based on an MBBR sewage treatment process.
Background
The main factor of water eutrophication is closely related to the phosphorus in the water. With the development of society, agricultural chemical fertilizers are continuously used in large quantities, and urban domestic sewage and industrial sewage are discharged to enter water bodies such as rivers, lakes, oceans and the like, so that the phosphorus content in the water environment is continuously increased, the eutrophication condition of the water environment is serious, and great harm is brought to the ecological environment.
With the increasing pressure of water environment protection, energy conservation, emission reduction and the like in China, the requirement on the quality of the effluent water of the sewage treatment plant is more and more strict, and the established sewage treatment plant faces urgent needs for upgrading and reconstruction. However, the problem of insufficient carbon source generally exists in the influent water of sewage plants in many areas of China, and the problem of poor denitrification and dephosphorization effects is a common problem in the industry.
In order to solve the problem of N, P difficulty in treatment due to insufficient carbon source, the currently adopted method is to add organic carbon sources (such as methanol, sodium acetate, acetic acid and the like) to supplement soluble biodegradable organic matters (rbCOD) to realize enhanced biological nitrogen and phosphorus removal. In addition, chemical phosphorus removal is also commonly adopted at home and abroad. For example, the metal salt dephosphorization method needs to input a large amount of chemical agents, generates a large amount of chemical bottom sludge, causes secondary pollution, and additionally increases the sludge disposal cost. In addition, a physical adsorption dephosphorization method is adopted, but the problems of high use cost, saturation or blockage of the adsorbent and difficulty in regeneration of the adsorbent exist; the membrane treatment dephosphorization method, the treatment problems of membrane pollution and enrichment are still to be solved; the natural treatment method has the problems of low organic load per unit area, namely large occupied area, and relatively low natural treatment rate, namely long sewage retention time.
Obviously, the operating cost and the sludge disposal cost of the sewage plant are increased by adding carbon sources or medicaments, adsorbents and the like, so that the method is difficult to continuously popularize and apply and is also against the concept of sustainable development.
Some researches on supplementing carbon sources by using sludge hydrolysis fermentation are carried out at home and abroad, and some process application examples are developed, but anaerobic fermentation is mostly carried out on primary sludge. The primary sludge fermentation can produce high-concentration rbCOD and VFAs, but the primary sludge is small in total quantity, unstable and lack of sufficient quantity of mixed floras with hydrolysis fermentation function, so that the hydrolysis speed is low and the utilization rate is not high by using the process.
Disclosure of Invention
The invention aims to provide an enhanced phosphorus removal method based on an MBBR sewage treatment process, which overcomes the defect of difficult phosphorus removal of the current domestic sewage treatment process, and adopts the defects of backflow supplement of inlet water VFAs after hydrolysis and fermentation of activated sludge so as to improve the phosphorus removal effect of a sewage plant.
The purpose of the invention can be realized by the following technical scheme:
an enhanced dephosphorization method based on an MBBR sewage treatment process comprises the steps of treating sewage in an anaerobic tank, an anoxic tank, an MBBR tank and a sedimentation tank in sequence, discharging obtained effluent, directly returning part of obtained precipitated sludge to the anaerobic tank, sending part of the obtained precipitated sludge to a hydrolysis fermentation unit for treatment, obtaining hydrolysis fermentation mixed liquid, and returning the obtained hydrolysis fermentation mixed liquid to the anaerobic tank, thus completing the process.
Further, the total reflux ratio of the precipitated sludge is 30-80% Q, wherein Q is the water inflow of the sewage.
Furthermore, the amount of the precipitated sludge directly returned to the anaerobic tank is 20-79% Q, and the amount of the precipitated sludge fed into the hydrolysis fermentation unit is 1-20% Q.
More preferably, the amount of the precipitated sludge fed into the hydrolysis fermentation unit is 4-7% Q.
Further, the hydrolysis fermentation unit comprises a hydrolysis fermentation tank and a concentration tank which are connected in sequence, part of precipitated sludge is sent into the hydrolysis fermentation tank, then, mud-water separation is carried out in the concentration tank, the obtained hydrolysis fermentation mixed liquid returns to the anaerobic tank, part of the obtained sludge flows back into the hydrolysis fermentation tank, and the rest sludge is discharged.
Furthermore, the SRT of the sludge age in the hydrolysis fermentation tank is 3-7 d, the pH is controlled to be 4-6, the sludge level in the hydrolysis fermentation tank during static precipitation is 0.5-1.0 m (because the hydrolysis fermentation tank adopts an intermittent aeration and stirring mode, a static precipitation period also exists), and the running sludge solid load rate of the concentration tank is 30-100 kg/(m2.d)。
More preferably, in the operation process of the hydrolysis fermentation tank, the mixed liquid in the tank is controlled to be in an 'anoxic-anaerobic' alternative environment by adopting an intermittent aeration and stirring mode, and the stirring is carried outThe power density is 10-20 kw/m3The tank capacity is controlled, and meanwhile, the running range of the oxidation-reduction potential ORP is controlled to be-300 to +100 mv.
Furthermore, the hydrolysis yield of the sludge in the hydrolysis fermentation tank is 0.03-0.18 g of VFAs/gVSS, and the product is expressed by volatile fatty acid, VFAs; or the hydrolysis yield of the sludge in the hydrolysis fermentation tank is 0.08-0.35 gSCOD/gVSS, and the product is expressed by soluble COD (chemical oxygen demand), SCOD.
Furthermore, the concentration of the precipitated sludge fed into the hydrolysis fermentation tank is 5-12 g/L, the average sludge concentration during operation in the hydrolysis fermentation tank is 6-9 g/L, and the sludge concentration returned from the concentration tank to the hydrolysis fermentation tank is 10-15 g/L.
Further, part of the nitrified liquid from the MBBR tank is sent to the sedimentation tank, and the rest part of the nitrified liquid returns to the anoxic tank.
Compared with the prior art, the method can perform anaerobic hydrolysis on the activated sludge generated in the treatment process of the sewage plant to generate the rapidly degradable organic compounds rbCOD and VFAs, and effectively supplement the defects of incoming water VFAs; the fast absorption of the phosphorus accumulating bacteria is facilitated, and the P removing capability is improved; the extra addition of carbon sources and chemical phosphorus removal agents is reduced, and the cost is reduced; the sludge yield of the sewage plant is reduced, and the cost of sludge treatment and disposal is reduced.
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FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments. The present embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.
In the following embodiments or examples, unless otherwise specified, all of the conventional commercially available raw materials or conventional processing techniques in the art are indicated.
In order to improve the phosphorus removal effect of a sewage plant and the like, the invention provides an enhanced phosphorus removal method based on an MBBR sewage treatment process, as shown in figure 1, sewage is treated by an anaerobic tank, an anoxic tank, an MBBR tank and a sedimentation tank in sequence, the obtained effluent is discharged, part of the obtained precipitated sludge directly returns to the anaerobic tank, and the other part of the obtained precipitated sludge is sent to a hydrolysis fermentation unit for treatment to obtain hydrolysis fermentation mixed liquid and then returns to the anaerobic tank, thus completing the process.
In some embodiments, the total reflux ratio of the settled sludge is 30% to 80% Q, wherein Q is the wastewater influent. Specifically, if the total reflux ratio of the sludge is (30% and 80%) Q (Q is raw water inflow), the corresponding proportion of Q directly flowing back to the front end of the anaerobic tank is (20-29%, 60-79%), and the proportion of Q flowing back to the hydrolysis fermentation tank is (1-10%, 1-20%)
In a more specific embodiment, the amount of the precipitated sludge directly returned to the anaerobic tank is 20-79% Q, and the amount of the precipitated sludge fed into the hydrolysis fermentation unit is 1-20% Q. More preferably, the amount of the precipitated sludge fed into the hydrolysis fermentation unit is 4-7% Q.
In some specific embodiments, the hydrolysis fermentation unit comprises a hydrolysis fermentation tank and a concentration tank which are connected in sequence, part of the precipitated sludge is sent into the hydrolysis fermentation tank, then, mud and water separation is carried out in the concentration tank, the obtained hydrolysis fermentation mixed liquid is returned to an anaerobic tank, part of the obtained sludge flows back into the hydrolysis fermentation tank, and the rest sludge is discharged.
In a more specific embodiment, the sludge age SRT in the hydrolysis fermentation tank is 3-7 d, the pH is controlled to be 4-6, the sludge level in the hydrolysis tank during static precipitation is 0.5-1.0 m (because the hydrolysis tank adopts an intermittent aeration and stirring mode, a static precipitation period also exists), and the solid load rate of the running sludge of the concentration tank is 30-100 kg/(m & lt/m & gt)2.d)。
More preferably, in the running process of the hydrolysis fermentation tank, the mixed liquid in the tank is controlled to be in an anaerobic-anoxic-anaerobic alternate environment (aeration is stopped every 5 hours generally, the retention time is 0.5-1.0 hour) by adopting an intermittent aeration and stirring mode, and the stirring power density is 10-20 kw/m3The tank capacity is monitored, and the running range of the oxidation-reduction potential ORP is monitored to be-300 to +100mv (controlled by regulating and controlling the sludge retention time and stirring and aerating means). In addition, in order to prevent the odor pollution, the hydrolysis fermentation tank is covered and sealed,and is sent to a deodorization device for treatment by arranging an exhaust pipe.
In a more specific embodiment, the hydrolysis yield of the sludge in the hydrolysis fermentation tank is 0.03-0.18 g VFAs/gVSS, and the product is expressed by volatile fatty acid, VFAs; or the hydrolysis yield of the sludge in the hydrolysis fermentation tank is 0.08-0.35 gSCOD/gVSS, and the product is expressed by soluble COD (chemical oxygen demand), SCOD. Here, the hydrolysis product of the sludge is mainly a mixed acid such as acetic acid and propionic acid.
In a more specific embodiment, the concentration of the precipitated sludge fed into the hydrolysis fermentation tank is 5-12 g/L, the average sludge concentration in the hydrolysis fermentation tank during operation is 6-9 g/L, and the sludge concentration returned from the concentration tank to the hydrolysis fermentation tank is 10-15 g/L. In some embodiments, the portion of the nitrified liquid from the MBBR tank is sent to the sedimentation tank, and the remainder is returned to the anoxic tank.
The above embodiments may be implemented individually, or in any combination of two or more.
The above embodiments will be described in more detail with reference to specific examples.
Example 1:
as shown in fig. 1, a method for enhanced phosphorus removal based on an MBBR sewage treatment process comprises the following steps: most of the sludge precipitated in the sedimentation tank flows back to the initial end of the biological tank, namely the inlet end of the anaerobic tank, the rest of the sludge enters the hydrolysis fermentation tank and the concentration tank in turn for hydrolysis fermentation, wherein the hydrolysis fermentation tank is provided with an anchor stirrer (the stirring power density is about 15 kw/m)3A tank capacity) to realize anaerobic hydrolytic fermentation of sludge by adopting a complete mixed flow, wherein a concentration tank adopts static gravity sedimentation to mainly finish mud-water separation of mixed liquor from a hydrolytic fermentation tank, and the mixed liquor rich in VFAs enters the anaerobic tank from the concentration tank; the sludge concentrated at the bottom of the concentration tank flows back to the hydrolysis fermentation tank, the sludge can be circularly repeated in the hydrolysis fermentation tank and the concentration tank, the sludge retention time is prolonged, and the redundant sludge is discharged through a discharge system.
The main design parameters are as follows: the total sludge reflux ratio is designed to be 30 percent, the concentration of the active sludge in the biological pond is 3000mg/L, and the sludge flows back to the hydrolysis fermentation pondThe sludge flow is 10%, the sludge inlet concentration of the hydrolysis fermentation tank is 12g/L, the sludge concentration returned from the concentration tank to the hydrolysis fermentation tank is about 15g/L, the SRT (continuous sequencing batch) of the hydrolysis fermentation tank is 5d, the pH is controlled to be 4-6, the sludge level is about 0.6-0.8 m during static precipitation in the hydrolysis fermentation tank, and the solid load rate of the running sludge is about 60kg/(m & lt/m & gt)2D). The hydrolysis yield of the sludge is 0.15g VFAs/gVSS and 0.30g SCOD/gVSS; meanwhile, the operation range of the oxidation-reduction potential ORP is controlled to be-300 to +100 mv.
The pretreated sewage and the other part of activated sludge which flows back from the sedimentation tank enter an anaerobic zone or an anoxic zone of the biological tank (namely respectively corresponding to the anaerobic tank and the anoxic tank) together to strengthen anaerobic phosphorus release;
the sewage is degraded in the biological tank through anoxic, anaerobic and aerobic processes to realize the removal of pollutants and the reduction of concentration, the treated sludge-water mixed liquid flows into a sedimentation tank, sludge-water separation is carried out in the sedimentation tank, and the separated supernatant reaches the standard and is discharged;
the concentrated activated sludge is respectively conveyed to the water inlet end of the biological tank and the water inlet end of the hydrolysis fermentation tank through a sludge reflux pump, and redundant excess sludge generated by the system is treated through a sludge treatment and discharge process unit.
Example 2:
as shown in fig. 1, a method for enhanced phosphorus removal based on an MBBR sewage treatment process comprises the following steps: most of sludge precipitated in the sedimentation tank flows back to the initial end of the biological tank, the rest of sludge enters the hydrolysis fermentation tank and the concentration tank in sequence for hydrolysis fermentation, wherein the hydrolysis fermentation tank is provided with an anchor stirrer, anaerobic hydrolysis fermentation of the sludge is realized by adopting complete mixing flow, the concentration tank adopts static gravity sedimentation, mainly completes mud-water separation of mixed liquor from the hydrolysis fermentation tank, and mixed liquor rich in VFAs enters the initial end of the biological tank from the concentration tank; the sludge concentrated at the bottom of the concentration tank flows back to the hydrolysis fermentation tank, the sludge can be circularly repeated in the hydrolysis fermentation tank and the concentration tank, the sludge retention time is prolonged, and the redundant sludge is discharged through a discharge system.
The main design parameters are as follows: designing a total sludge reflux ratio of 80 percent and an active sludge concentration of 2500mg/L in a biological tank, wherein the sludge inlet flow rate of the sludge refluxed to a hydrolysis fermentation tank is 20 percent, the sludge inlet concentration of the hydrolysis fermentation tank is 5g/L, and the SRT (anaerobic stress tolerance) of the hydrolysis fermentation tank is 4 d; the hydrolysis yield of the sludge is 0.12g of VFAs/gVSS and 0.27g of SCOD/gVSS;
the sewage after pretreatment and the other part of activated sludge which flows back from the sedimentation tank enter an anaerobic zone or an anoxic zone of the biological tank together to strengthen anaerobic phosphorus release;
the sewage is degraded in the biological tank through anoxic, anaerobic and aerobic processes to realize the removal of pollutants and the reduction of concentration, the treated sludge-water mixed liquid flows into a sedimentation tank, sludge-water separation is carried out in the sedimentation tank, and the separated supernatant reaches the standard and is discharged;
the concentrated activated sludge is respectively conveyed to the water inlet end of the biological tank and the water inlet end of the hydrolysis fermentation tank through a sludge reflux pump, and redundant excess sludge generated by the system is treated through a sludge treatment and discharge process unit.
Example 3:
in a certain sewage plant, the sewage inflow index is as follows: COD 300mg/L, BOD 150mg/L, SS 150mg/L, TN 50mg/L, NH3-N 30mg/L，TP 3mg/L。
Because the carbon source of the inlet water is insufficient, the method of the embodiment 1 is adopted to reconstruct the original MBBR process, and the main parameters are as follows: the mud flow rate returned to the hydrolysis fermentation tank is 10 percent, the SRT is 5 days, the supernatant of the hydrolysis fermentation tank enters an anaerobic tank of the biological tank, the VFA concentration of the supernatant is 2170-3410mg/L, TN is 93-117mg/L, and TP is 19-24 mg/L. The operation after the transformation shows that the dephosphorization effect of the sewage plant is obviously improved under the condition of not adding external commercial carbon sources and dephosphorization agents, and the TP of the effluent is stably lower than 0.5mg/L, thereby meeting the requirement of first-level A discharge.
Although the original MBBR technology (namely omitting a side-stream activated sludge hydrolysis fermentation tank) can also reach the effluent standard of grade 1B, the effluent quality is unstable.
The embodiments described above are described to facilitate an understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention based on the disclosure of the present invention.
Claims (10)
1. An enhanced phosphorus removal method based on an MBBR sewage treatment process is characterized in that sewage is treated by an anaerobic tank, an anoxic tank, an MBBR tank and a sedimentation tank in sequence, the obtained effluent is discharged, part of the obtained precipitated sludge directly returns to the anaerobic tank, and the other part of the obtained precipitated sludge is sent to a hydrolysis fermentation unit for treatment to obtain hydrolysis fermentation mixed liquid and then returns to the anaerobic tank, and the treatment is completed.
2. The method of claim 1, wherein the total reflux ratio of the precipitated sludge is 30-80% Q, wherein Q is the wastewater influent.
3. The method for enhanced phosphorus removal based on the MBBR sewage treatment process of claim 2, wherein the amount of the precipitated sludge directly returned to the anaerobic tank is 20-79% Q, and the amount of the precipitated sludge fed into the hydrolysis fermentation unit is 1-20% Q.
4. The method for enhanced phosphorus removal based on the MBBR sewage treatment process of claim 3, wherein the amount of the precipitated sludge fed into the hydrolysis fermentation unit is 4-7% Q.
5. The method of claim 1, wherein the hydrolysis fermentation unit comprises a hydrolysis fermentation tank and a concentration tank which are connected in sequence, part of the precipitated sludge is fed into the hydrolysis fermentation tank, then sludge-water separation is carried out in the concentration tank, the obtained hydrolysis fermentation mixed liquid is returned to an anaerobic tank, part of the obtained sludge flows back into the hydrolysis fermentation tank, and the rest of the obtained sludge is discharged.
6. According to claim 5The enhanced phosphorus removal method based on the MBBR sewage treatment process is characterized in that the SRT of the sludge age in the hydrolysis fermentation tank is 3-7 d, the pH is controlled to be 4-6, the sludge level in the hydrolysis fermentation tank is 0.5-1.0 m during static precipitation, and the solid load rate of the sludge running in the concentration tank is 30-100 kg/(m & lt m & gt)2.d)。
7. The MBBR sewage treatment process-based enhanced phosphorus removal method of claim 6, wherein in the operation process of the hydrolysis fermentation tank, the mixed liquid in the tank is controlled to be in an anaerobic-anoxic-anaerobic alternative environment by adopting an intermittent aeration and stirring mode, and the stirring power density is 10-20 kw/m3The tank capacity is controlled, and meanwhile, the running range of the oxidation-reduction potential ORP is controlled to be-300 to +100 mv.
8. The method for enhanced phosphorus removal based on MBBR sewage treatment process of claim 5, wherein the hydrolysis yield of the sludge in the hydrolysis fermentation tank is 0.03-0.18 gVFAs/gVSS, and the product is expressed by Volatile Fatty Acids (VFAs); or the hydrolysis yield of the sludge in the hydrolysis fermentation tank is 0.08-0.35 g SCOD/gVSS, and the product is expressed by soluble COD (chemical oxygen demand).
9. The MBBR sewage treatment process-based enhanced phosphorus removal method of claim 5, wherein the concentration of the precipitated sludge fed into the hydrolysis fermentation tank is 5-12 g/L, the average sludge concentration during operation in the hydrolysis fermentation tank is 6-9 g/L, and the sludge concentration returned from the concentration tank to the hydrolysis fermentation tank is 10-15 g/L.
10. The method for enhanced phosphorus removal based on the MBBR sewage treatment process of claim 1, wherein part of the nitrified liquid from the MBBR tank is sent to the sedimentation tank, and the rest part is returned to the anoxic tank.
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