CN107117710B - Enhanced biological phosphorus removal method - Google Patents
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- CN107117710B CN107117710B CN201710363315.6A CN201710363315A CN107117710B CN 107117710 B CN107117710 B CN 107117710B CN 201710363315 A CN201710363315 A CN 201710363315A CN 107117710 B CN107117710 B CN 107117710B
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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
- C02F3/32—Biological treatment of water, waste water, or sewage characterised by the animals or plants used, e.g. algae
- C02F3/322—Biological treatment of water, waste water, or sewage characterised by the animals or plants used, e.g. algae use of algae
- C02F3/325—Biological treatment of water, waste water, or sewage characterised by the animals or plants used, e.g. algae use of algae as symbiotic combination of algae and bacteria
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
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- C—CHEMISTRY; METALLURGY
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- C02F2101/105—Phosphorus compounds
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Abstract
The invention discloses a method for strengthening biological phosphorus removal, and belongs to the field of sewage treatment. The biological phosphorus removal effect is enhanced by the microalgae, and the problem that the effect and the operation cost of the conventional phosphorus removal process cannot be considered at the same time is solved. The technical scheme of the invention comprises the stages of photosynthetic domestication, photosynthetic reinforcement, sewage treatment and the like, wherein the activated sludge in a biochemical pool of a sewage plant with a biological phosphorus removal function is used as inoculated sludge, the activated sludge is successfully started after 60 days, the removal load of a system TP can reach 0.04kgP/kgMLSS.d at most, and the sludge VSS/TSS in the system is more than 0.80. The process disclosed by the invention has the advantages of high total phosphorus removal rate, high residual sludge fertilizer efficiency, low energy consumption and drug consumption, high reaction rate and land occupation saving, is suitable for treating various phosphorus-containing wastewater, and is particularly suitable for removing phosphorus from sewage with carbon source deficiency and removing phosphorus from polluted natural water.
Description
Technical Field
The invention belongs to the field of sewage treatment, and particularly relates to a reinforced biological phosphorus removal method.
Background
Phosphorus removal is one of the important problems of sewage treatment, and besides two major methods of biological phosphorus removal and chemical phosphorus removal, the method also comprises emerging microalgae phosphorus removal. Phosphorus removal faces two problems, on one hand, TP needs to be removed from a water body to prevent eutrophication; on the other hand, phosphorus belongs to non-renewable resources, the storage amount of natural phosphorite reaches the warning line, and the phosphorus which needs to be removed from sewage is recycled when the phosphorus is exhausted, so that the healthy circulation of the phosphorus is realized.
The biological phosphorus removal mainly utilizes phosphorus-accumulating bacteria PAOs to release phosphorus under the anaerobic condition, excessively absorbs phosphorus under the aerobic condition, and realizes the removal of phosphorus from a water body through the discharge of excess sludge. In the biological phosphorus removal process, on one hand, carbon sources need to be consumed, and C/P is generally required to be more than 20; on one hand, aeration is needed under aerobic conditions, and a large amount of energy consumption is additionally consumed; meanwhile, the biological phosphorus removal efficiency is generally 60-70%, and the effluent TP is generally more than 0.5-1.0, so that the effect is difficult to further improve; the phosphorus content of the sludge is 3-4%, and the phosphorus content is low and is difficult to be used as fertilizer efficiency. But compared with chemical phosphorus removal, biological phosphorus removal is more economical, and the method is still the mainstream phosphorus removal method.
The chemical phosphorus removal mainly utilizes the reaction of a coagulant and phosphate to generate sediment which is removed from a water body. The method has the advantages of small occupied area, low energy consumption, realization of TP <0.1mg/L of discharged water and thorough removal of phosphorus; the disadvantages are high medicine consumption, difficult reutilization of the generated sludge, good phosphate effect and poor organic phosphorus effect.
Sewage plants often adopt a mode of combining biological phosphorus removal and chemical phosphorus removal to hopefully utilize the biological phosphorus removal function, reduce the treatment cost, combine chemical phosphorus removal and guarantee the treatment effect, but the satisfactory balance cannot be achieved on the effect and the economic cost.
In recent years, research related to the phosphorus removal of microalgae has appeared, and microalgae mainly comprises biological assimilation and absorbs phosphorus to remove the phosphorus from a water body, and the absorbed phosphorus is used for self growth, but the microalgae is difficult to separate mud from water and is difficult to apply in an engineering way.
In view of the problems faced by the present phosphorus removal, a novel phosphorus removal process with good treatment effect, low operation cost and recyclable phosphorus source is urgently needed to solve the phosphorus removal dilemma faced by sewage treatment. Research shows that microalgae phosphorus removal can be used for strengthening biological phosphorus removal and realizing effect addition. On one hand, the problem that the microalgae is difficult to separate sludge and water is solved; on the other hand, the microalgae can produce gas through photosynthesis, can be used as an oxygen source for biological phosphorus removal and aerobic, reduces or does not need aeration, and utilizes light energy to realize electron supply; meanwhile, the carbon source required by phosphorus removal can be provided by microalgae photosynthesis, so that the organic carbon source is saved, and the deep removal of TP can be finally realized.
Aiming at removing phosphorus in sewage, the invention adopts microalgae to strengthen biological phosphorus removal, and aims to solve the problem that the prior phosphorus removal process cannot give consideration to both effect and operation cost.
Disclosure of Invention
In view of the problems in the background art, the invention provides a method for enhanced biological phosphorus removal, which aims to solve the problem that the effect and the operating cost of a sewage phosphorus removal process in the prior art cannot be considered at the same time, and has the advantages of good treatment effect, low energy consumption, strong residual sludge fertilizer efficiency and the like.
In order to achieve the above object, the present invention provides an enhanced biological phosphorus removal method, which is characterized by comprising the following steps:
1) the reactor is built, and an SBR reactor is adopted, and the operation is carried out according to the sequence of water inlet, light-tight stirring, illumination aeration, sedimentation, water drainage and idling; the idle time is 0-0.5 h; stirring in dark place, and stirring in dark place; depositing in dark place during deposition;
2) inoculating sludge, namely inoculating activated sludge in a biochemical pool of a sewage plant with a biological phosphorus removal function, wherein after the sludge is inoculated, the sludge concentration in the system is 4-5g/L when the SBR reactor is at the highest water level;
3) in the photosynthetic domestication stage, the inlet water TP is 30-50mg/L, and the inlet water volatile fatty acid/TP>10; sequentially operating according to the step 1), wherein each period is 8 hours, and comprises the steps of stirring for 3 hours in a dark place, stirring for 2 hours in an illumination place, aerating for 2 hours in an illumination place, precipitating for 45min, and feeding water, draining water and leaving unused for the rest of time; when the illumination stirring and the illumination aeration are carried out, the illumination intensity is 500-2(ii) a When illumination aeration is carried out, the dissolved oxygen of the system is controlled to be 2-6 mg/L; controlling the sludge age of the system to be 15-20 days; after the drainage and the idling are finished, entering the next period, and repeating the mode for operation; TP removal rate in the light stirring stage>When 2mg-P/mg MLSS.h, entering the next step;
4) in the photosynthetic strengthening stage, the inlet water TP is 30-50mg/L, and the inlet water volatile fatty acid/TP>6 alkalinity of feed Water/TP>2; sequentially operating according to the step 1), wherein each period is 8 hours, and comprises the steps of stirring for 3 hours in a dark place, stirring for 3 hours in an illumination place, aerating for 1 hour in an illumination place, precipitating for 30min, and feeding water, draining water and leaving unused for the rest of time; when the illumination stirring and the illumination aeration are carried out, the illumination intensity is 1000-2(ii) a When illumination aeration is carried out, the dissolved oxygen of the system is controlled to be 2-6 mg/L; controlling the sludge age of the system to be 10-15 d; after the drainage and the idling are finished, entering the next period, and repeating the mode for operation; TP removal rate in the light stirring stage>When 6mg-P/mgMLSS.h, entering the next step;
5) in the sewage treatment stage, the COD/TP of the inlet water is in>6 alkalinity of feed Water/TP>2; an SBR reactor is adopted, and the operation is carried out according to the sequence of water inlet, photophobic stirring, illumination stirring, sedimentation, water drainage and idling without aeration; stirring in dark for 1.5-3h, and stirring in dark; when the mixture is stirred under illumination, the illumination intensity is 1000-2(ii) a Controlling the sludge age of the system to be 10-15 d; stirring by illumination until TP in the system<0.1mg/L, stopping stirring, precipitating for 30min, draining, keeping out of the sun during precipitation, entering the next cycle after leaving unused, and repeating the operation in the mode.
Preferably, in the sewage treatment stage, the removal load of the system TP is 0.01-0.04kgP/kgMLSS.d, and the VSS/TSS of the sludge in the system is more than 0.80.
Preferably, the maximum TP concentration in the system/initial TP concentration after water entry of the system during the stirring phase in the dark is > 2.
The SBR reactor in the step 1) is a sequencing batch reactor well known to those skilled in the art, and is treated in batches, each period comprises the steps of water feeding, reaction, precipitation, water drainage, idling and the like, and the reaction is further divided into light-resistant stirring, illumination stirring and illumination aeration; the idle time is mainly matched with the condition that the time of each period is the same, the period time is rounded and is generally 0-1h, and a person skilled in the art can select the appropriate idle time according to the teaching of the invention; meanwhile, as well known to those skilled in the art, the SBR has two water levels, i.e., a highest water level, which is an operation water level at the time of reaction, and a lowest water level, which is a water level after water discharge.
The activated sludge in the biochemical pool of the sewage plant with the biological phosphorus removal function in the step 2) refers to activated sludge with PAOs flora, and the biochemical pools with anaerobic function sections generally contain PAOs, such as A2O, A/O dephosphorization process, etc., one skilled in the art can select a suitable sludge source based on the teachings of the present invention; the sludge concentration refers to the sludge concentration in the system when the highest water level is reached after water enters the SBR reactor, and is used for indicating the microorganism content or designing and calculating;
the requirement of the water inlet volatile fatty acid/TP in the steps 3) and 4) can be domestic sewage or industrial wastewater, and can be configured by adding acetate and propionate into water to ensure the content of the volatile fatty acid/TP, and a person skilled in the art can select a proper organic carbon source to supplement the volatile fatty acid according to the teaching of the invention. For domestic sewage, the content of volatile fatty acids is generally 10-20% of COD, and those skilled in the art can select a suitable organic carbon source to supplement the volatile fatty acids according to the teaching of the present invention.
And 3), 4) controlling the sludge age, wherein sludge discharge is mainly realized through sludge discharge, the sludge discharge amount is calculated according to the sludge age requirement, and the sludge discharge can be executed in a drainage stage or an idle stage after drainage.
And 3) when the TP removal rate in the illumination stirring stage is more than 2mg-P/mgMLSS.h, the traditional biological phosphorus removal is not carried out, the TP removal phenomenon cannot occur, and when the TP removal phenomenon begins in the illumination stirring stage, the microalgae is represented to begin to grow in the system and is coupled with the existing PAOs flora.
And 4) when the TP removal rate in the illumination stirring stage is more than 6mg-P/mgMLSS.h, the microalgae and PAOs are dominant.
Step 4) and step 5), the inlet water alkalinity/TP requirement is met, wherein the alkalinity is measured by mgCaCO3/L, and sodium carbonate or sodium bicarbonate can be added for adjustment when the alkalinity is insufficient. One skilled in the art can select suitable inorganic carbon sources based on the teachings of the present invention.
In the SBR reactor in the step 5), the operation period can adopt a non-fixed period and is determined according to the TP content in the water body; fixed cycle operation may also be employed.
The illumination in the steps 3), 4) and 5) can adopt a tungsten lamp or sunlight, and the illumination intensity is lux/m2The area is determined according to the surface area of the liquid level of the reactor; one skilled in the art can select an appropriate light source based on the teachings of the present invention.
Step 5) not limiting the concentration of TP in the inlet water, only limiting the proportion of organic carbon source, inorganic carbon source and TP, and being suitable for treating various phosphorus-containing sewage; meanwhile, the composition of the organic carbon source is not required, and the proportion of the volatile fatty acid is not limited.
Preferably, the load and the rate are used for characterizing the removal condition of P, the unit of the rate is mgP/mgMLSS.h, the unit of the load is kgP/kgMLSS.d, and the unit conversion can be carried out on the load and the rate; the general rate is used for representing the process, analyzing the system running state and the load is used for designing values.
Preferably, the maximum concentration of TP in the system/initial concentration of TP after water is fed into the system at the light-shielding stirring stage is greater than 2, the characterization system is still in the biological phosphorus removal process, the defect of the biological phosphorus removal is compensated, the effect is enhanced, the anaerobic phosphorus release is good, and the important precondition of the biological phosphorus removal is provided.
Preferably, the light-resistant stirring stage is light-resistant, so that the oxygen generated by photosynthesis of the microalgae is mainly prevented from influencing an anaerobic environment.
Preferably, the precipitation stage is protected from light, and the microalgae is mainly prevented from photosynthesis to generate oxygen, so that the precipitation effect is influenced.
Preferably, in the sewage treatment stage, the TP removal load reaches 0.01-0.04kgP/kg MLSS.d, the TP removal load is influenced by the concentration of inlet water TP, the upper limit is reached when the concentration of inlet water TP is greater than 40mg/L, and the lower limit is reached when the concentration of inlet water TP is less than 10 mg/L.
The invention has the beneficial technical effects that:
1) the dephosphorization comprises two processes of biological dephosphorization and microalgae dephosphorization;
2) in the biological phosphorus removal aerobic stage, oxygen is generated through photosynthesis of microalgae, phosphorus absorption is met, and 100% of aeration energy consumption can be saved after the start is successful;
3) the microalgae has the function of absorbing phosphorus for self synthesis, the fertilizer efficiency of the excess sludge is high, the sludge sedimentation performance is good, and SV30>90%；
4) The phosphorus removal rate of the system is more than 98%, and the TP of the effluent can be less than 0.1 mg/L;
5) the needed carbon source is low, the photosynthesis of the microalgae can provide organic matters for the phosphorus removal process, the carbon source is saved, the COD/TP is generally required to be more than 20 in the traditional biological phosphorus removal process, and the COD/TP only needs 6.
Drawings
The invention will be further described in detail and fully with reference to the accompanying drawings, in which:
FIG. 1 is a schematic diagram of the TP change in the system at the end of each phase of the phosphorus removal method of the present invention, which is illustrated as the TP change in the SBR period at the end of the photosynthetic acclimation phase, photosynthetic enhancement phase and sewage treatment phase;
FIG. 2 is a schematic diagram of DO changes in the system at the end of each period of the phosphorus removal method, which is illustrated as TP changes in the SBR period at the end of the photosynthetic acclimation period, photosynthetic enhancement period and sewage treatment period.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer and clearer, the present invention will be further described in detail with reference to specific embodiments.
The enhanced biological phosphorus removal effect of the invention is that on the basis of the traditional anaerobic-aerobic phosphorus removal theory, the advanced treatment of phosphorus is realized by introducing microalgae; on one hand, dissolved oxygen required for phosphorus removal can be provided by photosynthesis of microalgae, and a carbon source required for phosphorus removal can be provided by photosynthesis of the microalgae; on the other hand, the existence of the phosphorus removal activated sludge strengthens the flocculation of the microalgae, so that the microalgae can realize good sludge-water separation; meanwhile, the microalgae and biological phosphorus removal coupling system can realize deep phosphorus removal, the phenomena of anaerobic phosphorus release and aerobic (illumination) excessive phosphorus absorption occur in both microalgae and phosphorus accumulating bacteria, the total phosphorus removal is more thorough, and the total phosphorus in effluent can be stably less than 0.1 mg/L. The invention aims to quickly enrich and strengthen the phosphorus accumulating bacteria by starting with high TP; and gradually enriching and domesticating the flora by adjusting the two stages of illumination and illumination aeration and the time proportion thereof, so that the microalgae and the phosphorus accumulating bacteria are balanced, and finally the microalgae can provide all DO and part of organic carbon sources for a system containing the phosphorus accumulating bacteria. Aiming at removing phosphorus in sewage, the invention adopts microalgae to strengthen biological phosphorus removal, and aims to solve the problem that the prior phosphorus removal process cannot give consideration to both effect and operation cost. The invention is suitable for the treatment of various phosphorus-containing wastewater, in particular for the phosphorus removal of sewage with carbon source deficiency and the phosphorus removal and purification of polluted natural water.
Referring to fig. 1 and 2, as shown in fig. 1, after the system is successfully started, the output water TP is stable at less than 0.1mg/L, as shown in fig. 2, while the system does is stirred by light (without aeration), the system does gradually rises, and oxygen supply by photosynthesis of microalgae is shown. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.
Example 1:
1) the method comprises the following steps of (1) building a reactor, wherein the SBR reactor is adopted, the reactor is cylindrical, the diameter of the bottom surface of the reactor is 400cm, the height of the reactor is 1200cm, the effective volume of the reactor is 125L, and the reactor is operated according to the sequence of water inlet, light-resistant stirring, illumination aeration, sedimentation, water drainage and idling; the idle time is 0-0.5h and is set according to the requirement;
2) inoculating sludge, inoculating activated sludge in an A2/O process aeration tank, and when the SBR reactor is at the highest water level after the sludge is inoculated, the sludge concentration in the system is 4.95 g/L;
3) in the photosynthetic domestication stage, tap water is added with sodium phosphate and sodium acetate for water distribution, so that the TP of inlet water is 40mg/L, the volatile fatty acid of inlet water is 420mg/L, and the volatile fatty acid/TP =10.05>10; sequentially operating according to the step 1), wherein each period is 8 hours, and comprises the steps of stirring for 3 hours in a dark place, stirring for 2 hours in an illumination place, aerating for 2 hours in an illumination place, precipitating for 45min, and feeding water, draining water and leaving unused for the rest of time; when the stirring is performed by illumination and the aeration is performed by illumination, the illumination intensity is 1000lux/m2(ii) a When illumination aeration is carried out, the dissolved oxygen of the system is controlled to be 2-6 mg/L; controlling the sludge age of the system to be 20 days; after the drainage and the idling are finished, entering the next period, and repeating the mode for operation; after 30 days, the TP removal rate reaches 2mg-P/mgMLSS.h in the illumination stirring stage, and the next step is carried out;
4) in the photosynthetic reinforcement stage, tap water is added with sodium phosphate and sodium acetate for water distribution, so that the inlet water TP is 40mg/L, the inlet water volatile fatty acid is 260mg/L, and the inlet water volatile fatty acid/TP =6.5>6, the alkalinity of inlet water is 100mg/L, and the alkalinity of inlet water/TP =2.5>2; sequentially operating according to the step 1), wherein each period is 8 hours, and comprises the steps of stirring for 3 hours in a dark place, stirring for 3 hours in an illumination place, aerating for 1 hour in an illumination place, precipitating for 30min, and feeding water, draining water and leaving unused for the rest of time; when the stirring is performed by illumination and the aeration is performed by illumination, the illumination intensity is 3000lux/m2(ii) a When illumination aeration is carried out, the dissolved oxygen of the system is controlled to be 2-6 mg/L; controlling the sludge age of the system to be 15 days; after the drainage and the idling are finished, entering the next period, and repeating the mode for operation; after 20 days, the TP removal rate reaches 6mg-P/mgMLSS.h in the illumination stirring stage, and the next step is carried out;
5) in the sewage treatment stage, industrial wastewater is adopted, the inlet water TP is 40mg/L, the inlet water COD is 300mg/L, and the inlet water COD/TP =7.5>6, the alkalinity of inlet water is 100mg/L, and the alkalinity of inlet water/TP =2.5>2; an SBR reactor is adopted, and the operation is carried out according to the sequence of water inlet, photophobic stirring, illumination stirring, sedimentation, water drainage and idling without aeration; stirring for 2h in a dark place; when the mixture is stirred under illumination, the illumination intensity is 3000lux/m2(ii) a Controlling the sludge age of the system to be 10 days; stirring by illumination until TP in the system<0.1mg/L, stopping stirring, precipitating for 30min, draining, idling, entering the next period, and repeating the operation in the mode; after 10 days, the light stirring time is reduced from the initial 6h to 4h, and then the light is fixedThe stirring time was 4h (cycle time 6 h). The maximum value of the concentration of TP in the system in the lightproof stirring stage is 90mg/L, which is 2.25 times of the initial concentration of TP in the system, and the anaerobic phosphorus release effect is good. After the cycle time is operated according to 6h, the removal load of the system TP reaches 0.040kgP/kg MLSS.d, and effluent TP is obtained<0.1mg/L, and VSS/TSS =0.81 of sludge in the system.
Example 2:
steps 1) -4) are the same as in example 1;
5) in the sewage treatment stage, domestic sewage is adopted, the inlet water TP is 10mg/L, the inlet water COD is 200mg/L, and the inlet water COD/TP =20>6, the alkalinity of inlet water is 100mg/L, and the alkalinity of inlet water/TP =2.5>2; an SBR reactor is adopted, and the operation is carried out according to the sequence of water inlet, photophobic stirring, illumination stirring, sedimentation, water drainage and idling without aeration; stirring for 1h in a dark place; when the mixture is stirred under illumination, the illumination intensity is 3000lux/m2(ii) a Controlling the sludge age of the system to be 10 days; stirring by illumination until TP in the system<0.1mg/L, stopping stirring, precipitating for 30min, draining, idling, entering the next period, and repeating the operation in the mode; after 5 days, the light stirring time is reduced from 4h to 2h, and then the light stirring time is fixed to be 2h (the period time is 3 h). The maximum value of the concentration of TP in the system in the lightproof stirring stage is 24mg/L, which is 2.4 times of the initial concentration of TP in the system, and the anaerobic phosphorus release effect is good. After the system runs for 3 hours in the cycle time, the removal load of the system TP reaches 0.020kgP/kg MLSS.d, and effluent TP is discharged<0.1mg/L, and VSS/TSS =0.82 of sludge in the system.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the technical principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (3)
1. The enhanced biological phosphorus removal method is characterized by comprising the following steps:
1) the reactor is built, and an SBR reactor is adopted, and the operation is carried out according to the sequence of water inlet, light-tight stirring, illumination aeration, sedimentation, water drainage and idling; the idle time is 0-0.5 h; stirring in dark place, and stirring in dark place; depositing in dark place during deposition;
2) inoculating sludge, namely inoculating activated sludge in a biochemical pool of a sewage plant with a biological phosphorus removal function, wherein after the sludge is inoculated, the sludge concentration in the system is 4-5g/L when the SBR reactor is at the highest water level;
3) in the photosynthetic domestication stage, the inlet water TP is 30-50mg/L, and the inlet water volatile fatty acid/TP is more than 10; sequentially operating according to the step 1), wherein each period is 8 hours, and comprises the steps of stirring for 3 hours in a dark place, stirring for 2 hours in an illumination place, aerating for 2 hours in an illumination place, precipitating for 45min, and feeding water, draining water and leaving unused for the rest of time; when the stirring and aeration are performed by illumination, the illumination intensity is 500 and 1000 lux; when illumination aeration is carried out, the dissolved oxygen of the system is controlled to be 2-6 mg/L; controlling the sludge age of the system to be 15-20 days; after the drainage and the idling are finished, entering the next period, and repeating the mode for operation; when the TP removal rate is more than 2mg-P/mgMLSS.h in the illumination stirring stage, entering the next step;
4) in the photosynthetic reinforcement stage, the inlet water TP is 30-50mg/L, the inlet water volatile fatty acid/TP is more than 6, and the inlet water alkalinity/TP is more than 2; sequentially operating according to the step 1), wherein each period is 8 hours, and comprises the steps of stirring for 3 hours in a dark place, stirring for 3 hours in an illumination place, aerating for 1 hour in an illumination place, precipitating for 30min, and feeding water, draining water and leaving unused for the rest of time; when the stirring and aeration are performed by illumination, the illumination intensity is 1000-; when illumination aeration is carried out, the dissolved oxygen of the system is controlled to be 2-6 mg/L; controlling the sludge age of the system to be 10-15 d; after the drainage and the idling are finished, entering the next period, and repeating the mode for operation; when the TP removal rate is more than 6mg-P/mgMLSS.h in the illumination stirring stage, the next step is carried out;
5) in the sewage treatment stage, the COD/TP of inlet water is more than 6, and the alkalinity/TP of the inlet water is more than 2; an SBR reactor is adopted, and the operation is carried out according to the sequence of water inlet, photophobic stirring, illumination stirring, sedimentation, water drainage and idling without aeration; stirring in dark for 1.5-3h, and stirring in dark; when the mixture is stirred under illumination, the illumination intensity is 1000-; controlling the sludge age of the system to be 10-15 d; and (3) stirring by illumination until TP in the system is less than 0.1mg/L, stopping stirring, draining water after precipitating for 30min, keeping the system away from light during precipitation, entering the next period after idling, and repeating the operation in the mode.
2. The enhanced biological phosphorus removal method of claim 1, wherein in the sewage treatment stage, the removal load of the system TP is 0.01-0.04kgP/kg MLSS.d, and the VSS/TSS of the sludge in the system is more than 0.80.
3. The enhanced biological phosphorus removal method of claim 1, wherein the maximum concentration of TP in the system/initial concentration of TP after water feeding in the system is >2 during the light-shielding stirring stage.
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| CN102515347A (en) * | 2011-12-12 | 2012-06-27 | 浙江工商大学 | Domestication method of granular sludge for reinforcing biological phosphate removing system |
| CN102701438A (en) * | 2012-05-04 | 2012-10-03 | 北京工业大学 | Normal temperature low-ammonia-nitrogen nitrosation starting method |
| CN103011520A (en) * | 2012-12-23 | 2013-04-03 | 北京工业大学 | Method for starting A2N two-stage SBR denitrifying phosphorus removal |
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