CN210559910U - Sewage nature-imitated purification system - Google Patents
Sewage nature-imitated purification system Download PDFInfo
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- CN210559910U CN210559910U CN201920979423.0U CN201920979423U CN210559910U CN 210559910 U CN210559910 U CN 210559910U CN 201920979423 U CN201920979423 U CN 201920979423U CN 210559910 U CN210559910 U CN 210559910U
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Abstract
The utility model relates to an imitative natural purification system of sewage through extension biochemical section HRT to 23h-34h, leading filler compound pre-acidification district increases the micromolecule and volatilizees sour, sets up the oxygen deficiency behind the aeration section, good oxygen intensive denitrification, reduces measures such as settling zone surface load to 0.3-0.8m/h and provides the structural optimization of pond for degree of depth nitrogen and phosphorus removal. In the operation mode, the dissolved oxygen in the aerobic zone is controlled to be 0.1-0.5mg/L, the ORP potential is controlled to be-10-20 mV, the aeration quantity is controlled by keeping 2-4mg/L of ammonia nitrogen in the effluent of the biochemical tank, and the nitrogen and phosphorus removal effect is improved. The sludge concentration is increased to 6-15g/L, and the effective pool depth is 7-9m to reduce the occupied land. The device have and go out water quality good, the running cost is low, advantages such as management convenience, application prospect is extensive.
Description
Technical Field
The utility model belongs to the sewage treatment field especially relates to an imitative natural purification system of sewage.
Background
By natural law, a domestic sewage treatment system can be understood as an artificially enhanced microbial ecosystem with the aim of removing organic matters and specific nutrient elements. In the process that domestic sewage enters a natural ecological system (taking a river as an example), self-purification (mainly removal of organic matters and nitrogen and phosphorus) can be realized under the conditions of low temperature and high temperature without distinguishing low-carbon-nitrogen-ratio sewage and high-carbon-nitrogen-ratio sewage by the self-purification function of a natural circulation system, and in the process of supplying river water to underground water, removal of SS (suspended matters) phosphorus can be realized without adding chemical agents. The method has good reference significance for reconsidering the design of the sewage treatment plant. From the angle, the operation rule and the operation process of a microbial ecosystem are considered more when the reactor is designed, so that the addition of chemical agents is expected to be reduced, the response to the low-temperature and low-carbon-nitrogen-ratio sewage quality is enhanced, the operation energy consumption is reduced, and the more excellent treatment efficiency is realized.
The reason why the river is polluted can be understood as that the amount of pollutants discharged into the river exceeds the self-cleaning capacity of a river ecosystem, the biochemical reaction in a sewage treatment system is mostly understood as a first-order kinetic process, and in the design of the existing sewage treatment system, in order to reduce the occupied land and reduce the investment cost, a higher load is often adopted.
Unlike industrial wastewater, most of the components of domestic sewage (except humic acid and humus) defined as organic pollutants or inorganic pollutants can be well utilized or converted by microorganisms and removed from water. From this perspective, the microorganism metabolism process is strengthened in the domestic sewage treatment process, and it is feasible to exert the efficiency of the microorganism ecosystem to realize deep purification of sewage, and the operation cost is economical.
At present, along with the development of economic society of China, the amount of pollutants discharged artificially is rapidly increased, meanwhile, the self-cleaning capacity of a natural ecological system is objectively reduced due to the large utilization of ecological water, wetlands, lands and the like, and in order to maintain the ecological system at a level relatively suitable for human living, the state has come out of more and more strict sewage treatment standards. However, the existing sewage treatment reactor pursuing high efficiency and low investment cost often cannot meet the discharge standards in the actual operation process, so that the existing sewage treatment process has to adopt a denitrification filter tank, a carbon source adding mode and the like for further denitrification; further removing phosphorus by adopting processes such as coagulating sedimentation and filtering; and the COD is further removed by adopting the technologies of coagulating sedimentation, membrane filtration and the like. The measures can achieve the effect of advanced treatment, but also bring the problems of high medicament cost, high carbon emission in the treatment process and the like, and whether the cost (resource consumption, carbon emission in chemical production) and benefit (water quality purification and reduction of influence on a natural ecosystem) of the physicochemical treatment measures are positive needs to be further deeply accounted and evaluated from the protection of the whole ecosystem.
From the development history of sewage treatment systems, no matter the sewage treatment processes such as an activated sludge process and an SBR (sequencing batch reactor) process are COD at the beginning of creation, ammonia nitrogen is the main, nitrogen and phosphorus removal is not the main, and the subsequent addition of an anoxic zone or an anoxic stirring and anaerobic zone enables the sewage treatment processes to have the functions of nitrogen and phosphorus removal, but a reactor is not designed according to the requirements of deep nitrogen and phosphorus removal, so that the efficient nitrogen and phosphorus removal effect is ensured.
Due to the arrangement of the septic tank, domestic sewage is mostly in a state of low carbon-nitrogen ratio, and the condition of low carbon ratio is considered as an important factor for limiting the denitrification effect of the sewage. On the premise, the setting of the denitrification filter tank becomes an inevitable choice. However, in terms of the microbial metabolic process related to denitrification, nitrification and denitrification, short-cut nitrification and denitrification, coupling of short-cut denitrification with anaerobic ammonia oxidation, anaerobic ammonia oxidation and other processes all exist in natural ecosystems, and occupy an important position in the circulation of natural nitrogen elements. In the process from the nitrification and denitrification, the short-cut nitrification and denitrification to the anaerobic ammonia oxidation, the amount of organic matters required in the microbial metabolism process is reduced from high to low, and theoretically, a carbon source is not required in the anaerobic ammonia oxidation process. The natural ecosystem is beneficial to the utilization of processes such as short-cut nitrification and short-cut denitrification, coupling of the short-cut denitrification with anaerobic ammonia oxidation, anaerobic ammonia oxidation and the like, and the problem that the denitrification process is influenced by a low carbon ratio does not exist in the self-purification process of the natural ecosystem. From the perspective of microbial metabolism, in the processes of nitrification and denitrification, short-cut nitrification and denitrification, coupling of short-cut denitrification and anaerobic ammonia oxidation, and decreasing of carbon sources of anaerobic ammonia oxidation, the rate efficiency of the microorganisms is further reduced. In the existing sewage treatment system, the nitrification and denitrification processes are ubiquitous and widely utilized, but the short-cut nitrification and short-cut denitrification and anaerobic ammonia oxidation processes do not play an important role in the sewage denitrification and phosphorus removal system. The reason for this is that the existing sewage treatment reactor does not provide sufficient favorable conditions for the shortcut nitrification and shortcut denitrification and the anaerobic ammonia oxidation process, and cannot enrich enough shortcut nitrifying bacteria and anaerobic ammonia oxidation bacteria to generate enough nitrite. From the metabolic demand and ecological niche of anammox, compared with denitrifying bacteria, the growth conditions (ecological niche) are favorable for low carbon-nitrogen ratio, low dissolved oxygen, long sludge age, long hydraulic retention time, low load or high ammonia nitrogen, and the like, but the existing sewage treatment system does not have the conditions.
From the response angle of low temperature, the low temperature can not kill the microorganisms, only influences the enzyme activity and the metabolic process of the microorganisms and reduces the metabolic capacity of the microorganisms, and under the condition, the retention time is prolonged, so that the response to the low temperature period can be realized.
Even from the perspective of nitrification and denitrification, as much carbon source as possible should be ensured in the biochemical reaction processIs utilized by the denitrification process to reduce the utilization of the denitrification process by the aerobic treatment process, however, in the existing treatment process, although the denitrification zone absorbs most of the carbon source, part of the carbon source of the inlet water is converted into CO through the aeration process due to the high dissolved oxygen in the aerobic zone and the dissolved oxygen brought by the reflux of the nitrifying liquid2And water is consumed and is not utilized as a denitrification carbon source, so that the imbalance of the carbon-nitrogen ratio is aggravated, and one way for solving the problem is to reduce the concentration of dissolved oxygen, so that the nitrification and denitrification processes are synchronous in the same reactor as much as possible, and the direct oxidation process of organic matters by taking oxygen as an electron acceptor is reduced.
SUMMERY OF THE UTILITY MODEL
In view of the above, one of the main objectives of the present invention is to provide a natural purification system for sewage, so as to at least partially solve at least one of the above technical problems.
In order to achieve the above object, the utility model provides an imitative natural purification system of sewage, include:
the primary anaerobic zone is provided with a primary anaerobic zone water inlet and a primary anaerobic zone water outlet;
the anoxic zone is provided with an anoxic zone water inlet and an anoxic zone water outlet, and the anoxic zone water inlet is communicated with the primary anaerobic zone water outlet;
the main reaction zone is provided with a main reaction zone water inlet and a main reaction zone water outlet, and the main reaction zone water inlet is communicated with the anoxic zone water outlet; and
the settling zone is communicated with a water inlet of the settling zone and a biochemical water outlet, and the water inlet of the settling zone is communicated with the water outlet of the main reaction zone.
Based on the technical scheme, the utility model discloses an imitative natural purification system of sewage has one of following advantage at least for prior art:
1. the nitrogen and phosphorus removal efficiency is high, the removal rates of TN (total nitrogen), TP (total phosphorus) and COD are respectively more than 90%, 99.5% and 93%, and the concentrations of TN, TP and COD in effluent can be 5mg/L, 0.05mg/L and less than 15 mg/L;
2. no medicament is added, the aeration energy consumption is lower than 0.09kW/t, the operation cost can be below 0.3 yuan/t, and no extra carbon footprint is generated due to the addition of the medicament in the water treatment process;
3. the method is suitable for sewage with low carbon-nitrogen ratio, the COD/TN ratio of the sewage is about 3-4, and the ideal denitrification and dephosphorization effect can be still kept;
4. the effect of the method is excellent in the process of denitrification and dephosphorization at a low temperature, and the ideal denitrification and dephosphorization effect can be still maintained at the temperature of 5-15 ℃;
5. the system has the advantages of excellent water outlet quality, low operation cost, convenient operation management, no need of matching dosing pumps and the like, full automation of the operation process and wide application prospect.
Drawings
FIG. 1 is a flow chart of a method for deep purification of wastewater according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of an embodiment of the present invention when the deep wastewater purification technology is implemented by a reactor structure design;
FIG. 3 is a schematic view of a reaction structure of a deep sewage purification technique implemented by sequential control of a reactor according to an embodiment of the present invention;
FIG. 4 shows the COD change of the inlet and outlet water in the embodiment 1 of the present invention;
FIG. 5 shows the change of the inlet and outlet TN in embodiment 1 of the present invention;
fig. 6 shows the change of the water inlet and outlet TP in embodiment 1 of the present invention.
In the above figures, the reference numerals have the following meanings:
1-a water inlet; 2-a desilting area; 3-a pre-acidification zone; 4-first stage anaerobic zone; 5-anoxic zone; 6-first-stage aerobic zone; 7-a secondary anaerobic zone; 8-a secondary aerobic zone; 9-third-stage anaerobic zones; 10-third-level aerobic zone; 11-a fourth-stage anaerobic zone; 12-nitrified liquid reflux flowmeter; 13-sludge reflux flow meter; 14-nitrifying liquid reflux pump; 15-nitrifying liquid return line; 16-sludge return line; 17-sludge reflux pump; 18-a gas supply line; 19-a precipitation zone; 20-excess sludge pump; 21-biochemical water outlet; 22-a main reaction tank; 23-decanter.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the accompanying drawings.
In the classical nitrification and denitrification process, denitrification is mainly removed through the reflux of nitrified liquid, but the problem existing in the process is the ceiling problem of denitrification rate, one part of nitrogen elements in a denitrification area is nitrate from which nitrified liquid flows back, and the other part of nitrogen elements in a denitrification area is ammonia nitrogen brought by inlet water, in the traditional high-load denitrification process, the ammonia nitrogen can not be removed in an anoxic area, so that the nitrogen can not enter an aerobic area and still can not be removed after being converted into the nitrate, and one part of nitrogen elements still can not enter the anoxic area through the reflux of nitrified liquid and still can be removed, so that the denitrification efficiency of a common sewage treatment reactor is between 70 and 80 percent, and higher removal rate is difficult to be realized, in order to solve the problem, the microorganisms can accumulate polysaccharides in the anoxic area while keeping low dissolved oxygen, and organic matters such as PHA (polyhydroxyalkanoate) and the like can not be consumed in the aerobic area, and then the anaerobic zone connected in series behind the aerobic zone is used as an internal carbon source to carry out denitrification process, so that the biological denitrification breaks through the limitation of the traditional nitrification and denitrification process. The AOA (anoxic-aerobic-anoxic) reactor meets the problem of sludge bulking caused by filamentous bacteria in the experimental process, and the problem can be controlled by arranging an anaerobic zone, pre-hydrolyzing and acidifying and reducing the load of a settling zone.
In the fresh water ecosystem, the river bank side slope is considered as a hot zone of anaerobic ammonia oxidation, and one possible reason is that the river bank side slope has alternation of anaerobic and aerobic, and the supply of dissolved oxygen is in an insufficient level, so that anaerobic ammonia oxidation bacteria can be enriched.
A large amount of discharged sludge is considered to be an operation mode which must be kept in order to maintain an efficient biological phosphorus removal process, which causes a short sludge age of biological phosphorus removal, and a long sludge age is often required to be maintained in order to enrich autotrophic bacteria in a nitrogen removal process, which is considered to be mismatching in the sludge age in the nitrogen and phosphorus removal process. However, in view of the metabolic process of phosphorus, if the concentration of phosphorus in the sludge is increased to a higher level, the sludge age can be increased to a higher state, as calculated from the conservation of materials. In the ecological niche, classical polyphosphate bacteria release energy through hydrolysis of polyphosphate to absorb external micromolecular volatile acid. In order to strengthen the process, a pre-acidification area is arranged by water inflow, and a part of carbohydrate organic matters are converted into volatile acid, so that the method has important significance for enriching the phosphorus-accumulating bacteria and improving the concentration of sludge phosphorus. From the limit of phosphorus removal, the traditional nitrogen and phosphorus removal system is generally considered to only remove phosphorus to about 1mg/L, but the value is obtained under the condition that the enrichment of phosphorus-accumulating bacteria is not ideal, and if the proportion of the phosphorus-accumulating bacteria is increased to a certain value, the phosphorus removal is also increased to a higher level.
The sludge concentration is an important parameter in a sewage treatment system, and in order to prevent sludge in a sedimentation tank from floating upwards and release phosphorus and ensure supply of dissolved oxygen in the actual operation process, the sludge concentration is always kept at 3-6g/L, which invisibly increases the occupied area. In order to reduce the occupied area, the sludge concentration can be further improved, the problem of oxygen supply cannot become a limiting factor due to low dissolved oxygen, and the sludge in the sedimentation tank can be floated up due to denitrification, so that the content of an internal carbon source can be reduced by reducing the load, the content of nitrate entering the sedimentation tank can be reduced, and the sludge floating up caused by denitrification can be prevented from being controlled by the denitrification excess of the sedimentation tank. Regarding the release problem of phosphorus, it should be noted that, from the metabolic process of phosphorus-accumulating bacteria, phosphorus-accumulating bacteria only crack polyphosphate when volatile acid exists outside, and release energy, and absorb the volatile acid, which is macroscopically the phosphorus rise of the sedimentation tank. If the sedimentation tank does not contain the volatile acid of the small molecules, the problem of releasing phosphorus in the sedimentation tank should not exist. The reason for the accumulation of the micromolecule volatile acid possibly existing in the sedimentation tank during operation can be derived from uneven sludge discharge, and the micromolecule volatile acid released by anaerobic digestion of the sludge is caused by the local long-term anaerobic process caused by the accumulated sludge. This problem is avoided to a great extent now through the massive adoption of mechanical mud scraping and sucking machine, and simultaneously, if adopt centripetal radial flow sedimentation tank, the volume of dying in the sedimentation tank will further dwindle to avoid the problem of sedimentation tank phosphorus release. The increase of the concentration of the sludge can effectively reduce the hydraulic retention time, and further reduce the capital construction cost and the occupied area.
Regarding the problem of the pond depth, from the perspective of aeration and oxygen supply, oxygen supply and efficiency are already mature in water depth of less than 10m, and the occupied area can be further reduced by increasing the pond depth.
At present, the capital investment of urban sewage treatment plants is 3000 yuan/t water (treatment capacity per day), in the process, the operation cost is 0.6 yuan/t (including aeration energy consumption and medicament cost), the depreciation period is 30 years, the depreciation cost is 0.27 yuan/t, and the total operation cost is 0.87 yuan/t. After the long-residence-time low-load sewage treatment system is adopted, the investment cost can be increased to 4000 yuan/t of water (treatment capacity per day), the operation cost can be reduced to 0.3 yuan/t due to the reduction of medicament and aeration energy consumption, the depreciation period is still 30 years, the depreciation cost is 0.36 yuan/ton, the total operation cost is 0.66 yuan/t, and the system has cost advantage compared with the existing sewage treatment plant. For the problem of occupied area, the treatment system can be solved by increasing the depth of the tank, improving the concentration of sludge and other measures, and compared with the existing sewage treatment system, the treatment system has the advantage of operation. From the analysis of the carbon footprint (containing the medicament production) of the whole chain of sewage treatment, the whole treatment system is more environment-friendly because no medicament is added in the system.
The utility model discloses an imitative natural purification system of sewage, include:
the primary anaerobic zone is provided with a primary anaerobic zone water inlet and a primary anaerobic zone water outlet;
the anoxic zone is provided with an anoxic zone water inlet and an anoxic zone water outlet, and the anoxic zone water inlet is communicated with the primary anaerobic zone water outlet;
the main reaction zone is provided with a main reaction zone water inlet and a main reaction zone water outlet, and the main reaction zone water inlet is communicated with the anoxic zone water outlet; and
the settling zone is communicated with a water inlet of the settling zone and a biochemical water outlet, and the water inlet of the settling zone is communicated with the water outlet of the main reaction zone.
The purification system comprises a sand-water separation area for precipitating inorganic particles, wherein the sand-water separation area is provided with a separation area water inlet and a separation area water outlet, and the separation area water outlet is connected with the primary anaerobic area water inlet.
Wherein a pre-acidification area for regulating influent water is arranged between the anaerobic area and the sand-water separation area.
Wherein, the main reaction zone comprises a plurality of stages of main reaction zone aerobic sections and main reaction zone anaerobic sections which are connected in series, or the main reaction zone comprises a main reaction tank;
wherein the aerobic section of the main reaction zone is provided with an oxygen supply pipeline for providing oxygen;
a nitrifying liquid return pipeline for returning nitrifying liquid to the anoxic zone is arranged between the anoxic zone and the anaerobic section of the main reaction zone;
wherein, nitrify liquid reflux pump and nitrify liquid reflux flowmeter on nitrify liquid return line.
Wherein a sludge return pipeline is arranged between the sedimentation zone and the primary anaerobic zone;
wherein a sludge return pump is arranged on the sludge return pipeline;
and the settling zone is provided with a residual sludge discharge pipeline, and the residual sludge discharge pipeline is provided with a residual sludge pump.
Wherein, the purification system comprises a filter tank, and a water inlet of the filter tank is connected with a water outlet of the sedimentation zone.
Wherein the depth of each zone of the purification system is 7-9 m.
The purification system of the utility model can adopt the following method to carry out sewage treatment:
(1) the water to be treated enters a sand-water separation zone and is precipitated to obtain water I;
(2) the water quality I enters a pre-acidification area, and water inlet tempering is carried out to obtain water quality II;
(3) the water quality II enters a primary anaerobic zone, and phosphorus is released and activated sludge floc is rapidly proliferated to obtain water quality III;
(4) the water quality III enters an anoxic zone and reacts to obtain water quality IV;
(5) the water quality IV enters a main reaction zone for reaction to obtain water quality V;
(6) and (5) enabling the water quality five to enter a precipitation area, and performing mud-water separation in the precipitation area to obtain water quality six, namely the purified reclaimed water.
Wherein, after the step (6) is finished, the step (7) is also carried out:
(7) and the water enters a coagulating sedimentation area and a multi-medium filter tank to further remove suspended matters and total phosphorus.
Wherein the filtration rate of the water quality six in the multi-medium filtration tank in the step (7) is 2-5 m/h;
in the step (7), coagulation and coagulation aids are not added in the coagulation sedimentation area and the multi-medium filter tank, and suspended matters and total phosphorus are removed by interception in the filtering process; meanwhile, a biological membrane is formed on the surface of the filter material, so that the synchronous nitrification and denitrification process is realized.
Wherein, the retention time of the water quality to be treated in the step (1) in the sand-water separation zone is 1-2 h;
wherein, the bottom of the sand-water separation zone in the step (1) is in an inverted quadrangular pyramid shape;
wherein, the pre-acidification zone in the step (2) is internally provided with a composite filler for constructing a biological membrane hydrolysis acidification zone;
wherein the composite filler comprises polyvinylidene chloride;
wherein the filling volume ratio of the composite filler is 70-90%;
wherein, in the step (3), the retention time of the second water quality in the first-stage anaerobic zone is 2-4 h;
wherein, the stirring is carried out in the processes of releasing phosphorus and quickly proliferating activated sludge flocs in the step (3);
wherein the reaction in the step (4) comprises a denitrification phosphorus absorption reaction and an anaerobic ammonia oxidation reaction;
wherein, in the step (4), the retention time of the water quality III in the anoxic zone is 2-4 h;
wherein, the step (4) is stirred in the reaction process;
wherein, the nitrified liquid generated in the step (5) flows back to enter an anoxic zone, and the reflux ratio is 100-400%;
wherein, the reaction in the step (5) comprises one or more of a combination of step nitration reaction, denitrification reaction and multi-stage phosphorus absorption reaction;
wherein, the main reaction zone in the step (5) comprises a main reaction zone aerobic section and a main reaction zone anaerobic section or the main reaction zone comprises a main reaction tank;
wherein, in the step (5), the retention time of the water quality IV in the aerobic section of the main reaction zone is 3-4h, and the retention time of the anoxic section is 3-4 h;
wherein, in the step (5), a submersible water impeller is arranged in the aerobic section of the main reaction zone;
wherein, the concentration of dissolved oxygen in the aerobic section of the main reaction zone in the step (5) is 0.1-0.5 mg/L;
wherein, the oxidation-reduction potential in the aerobic section of the last stage main reaction zone in the step (5) is controlled to be-10-20 mV;
wherein, the concentration of ammonia nitrogen generated in the reaction step in the step (5) is 2-4 mg/L;
wherein, the sludge part obtained in the mud-water separation step in the step (6) flows back to the first-stage anaerobic zone;
wherein, the sludge generated in the step (6) flows back to enter a first-stage anaerobic zone, and the reflux ratio is 30-100%;
wherein the surface load of the precipitation zone in the step (6) is 0.3-0.8 m/h;
wherein, the sedimentation zone in the step (6) adopts a centripetal radial flow type sedimentation zone with water inlet at the periphery and water outlet at the periphery;
wherein when the surface load of the settling zone in the step (6) is kept between 0.3 and 0.8m/h, the sludge concentration in the steps (3) to (7) is kept between 6 and 15 g/L;
wherein the total retention time of the water in the steps (1) to (5) is 23 to 34 hours;
wherein, the steps (4) to (6) can be realized by arranging an anoxic zone, an anaerobic zone, an aerobic zone and the like on the configuration of the reactor, and can also be realized by the operation control on the time sequence in one tank body.
When the steps (4) to (6) are realized through time sequence control, the return of the nitrifying liquid is cancelled, the sedimentation tank is cancelled, and the sludge return starting point is moved from the sedimentation tank to the rear end of the main reaction zone. The relationship between the running time of each section in the time sequence and the hydraulic retention time when the structure is realized is that the running time of the time sequences of the steps (4) to (6) is 20 to 30 percent of the hydraulic retention time.
In one embodiment, the present invention adopts, for example, the following technical solutions:
the utility model relates to a town sewage deep purification system and method, in particular to deep denitrification and dephosphorization under the condition of C/N ratio or low temperature. By prolonging HRT of a biochemical section to 23-34h, a small molecular volatile acid is added in a front filler composite pre-acidification area, anoxic and aerobic enhanced denitrification is arranged behind an aeration section, and the structural optimization of the tank is provided for deep denitrification and dephosphorization by measures of reducing the surface load of a settling area to 0.3-0.8m/h and the like. In the operation mode, the dissolved oxygen in the aerobic zone is controlled to be 0.1-0.5mg/L, the ORP potential is controlled to be-10-20 mV, the aeration quantity is controlled by keeping 2-4mg/L of ammonia nitrogen in the effluent of the biochemical tank, and the nitrogen and phosphorus removal effect is improved. The sludge concentration is increased to 6-15g/L, and the effective pool depth is 7-9m to reduce the occupied land. The technology and the method can be matched with non-reagent coagulating sedimentation filtration when the water inlet COD/TN is at 3.0-4.0 and the temperature is 5-12 ℃, ensure that the removal rates of TN, TP and COD are respectively more than 90%, 99.5% and 93%, simultaneously keep the aeration energy consumption lower than 0.09kW/t, and have the advantages of excellent water outlet quality, low operation cost, convenient management and the like, and wide application prospect.
In a preferred embodiment, the present invention adopts, for example, the following technical solutions: a town sewage natural-imitating deep purification method is characterized in that in the aspect of reactor configuration or reactor operation mode:
(1) the inlet water firstly enters a separation area 2 (sand-water separation area) through a water inlet 1, and inorganic particles which are not removed by the grit chamber are precipitated to prevent the subsequent process from being influenced;
(2) a pre-acidification zone 3 is arranged in front of the primary anaerobic zone 4 for water inlet tempering, and a part of organic matters are converted into volatile acid;
(3) the hydrolyzed and acidified effluent enters a primary anaerobic zone 4, phosphorus is released in the primary anaerobic zone 4, meanwhile, the activated sludge floc is quickly proliferated, the growth of filamentous bacteria is reduced, and the retention time in the primary anaerobic zone 4 is 2-4 h;
(4) the effluent of the primary anaerobic zone 4 enters an anoxic zone 5, and nitrate is used as an electron acceptor in the anoxic zone 5 to carry out reactions such as denitrification phosphorus absorption, anaerobic ammonia oxidation and the like;
(5) the effluent of the anoxic zone enters two-stage or three-stage series aerobic zone/anaerobic zone (main reaction zone aerobic section and main reaction zone anaerobic section), which are connected in series in the embodiment, namely a first-stage aerobic zone 6, a second-stage anaerobic zone 7, a second-stage aerobic zone 8, a third-stage anaerobic zone 9, a third-stage aerobic zone 10 and a fourth-stage anaerobic zone 11, and the gradient nitrification and denitrification reaction and the multi-stage phosphorus absorption reaction are carried out in the zones to ensure that the phosphorus concentration of the effluent reaches.
(6) The effluent of the four-stage anaerobic zone 11 enters a settling zone 19, mud and water are separated in the settling zone 19, a part of sludge flows back to the first-stage anaerobic zone 4, and a part of sludge is discharged as residual sludge.
(7) The effluent of the settling zone 19 enters a coagulating sedimentation tank, and a multi-medium filter tank is used for further removing SS and suspended phosphorus and is discharged from a biochemical water outlet 21, and finally, effluent regeneration is realized.
Wherein, in the steps (1) to (7), the depth of the pool body is 7 to 9m, so that the occupied area is reduced, and the total hydraulic retention time of the steps (1) to (5) is 23 to 34 h;
in the sand-water separation zone in the step (1), the hydraulic retention time is 1-2h, and the bottom of the sand-water separation zone is of an inverted rectangular pyramid structure and is connected with a mud pump to discharge mud and sand;
wherein, polyvinylidene chloride (PVDC) composite filler is arranged in the pre-acidification zone in the step (2), the filling ratio is 70-90%, and a biological membrane hydrolysis acidification zone is constructed;
wherein, the hydraulic retention time in the step (3) is 2-4h, stirring is carried out, and meanwhile, the sludge flows back to enter an anaerobic zone with the reflux ratio of 30-100%;
wherein, the anoxic zone 5 in the step (4) has hydraulic retention time of 2-4h, and is stirred, and nitrified liquid flows back to enter the anoxic zone with reflux ratio of 100-400%;
wherein, the anoxic zone in the step (5) enters into two-stage or three-stage aerobic/anaerobic reaction after the reaction is finished; in the reaction process, each stage of aerobic residence time is 3-4h, the anoxic zone residence time is 3-4h, and simultaneously, the submersible water impeller is arranged in the aerobic zone, in the embodiment, the submersible water impeller is arranged, and a decanter 23 is adopted, and the plug flow stirring is carried out during the aerobic aeration so as to ensure the uniformity of the reaction.
Wherein the concentration of dissolved oxygen in the aerobic zone in the step (5) is 0.1-0.5mg/L, the ORP potential of the last stage of the aerobic section is controlled at-10-20 mV, and the concentration of residual ammonia nitrogen is 2-4 mg/L.
Wherein, the surface load of the sedimentation zone in the step (6) is 0.3-0.8m/h, the pool type adopts a peripheral water inlet and peripheral water outlet centripetal radial flow sedimentation zone, and each pool is provided with a separate sludge reflux pump.
Wherein, when the surface load of the settling zone is kept between 0.3 and 0.8m/h, the sludge concentration in the steps (3) to (7) is kept between 6 and 15g/L, thereby further improving the load and reducing the occupied area.
Wherein, the steps (1) to (2) are realized by the design of a reactor configuration; the steps (3) - (5) can be realized by space arrangement on the reactor configuration, or can be realized by time sequence operation control in a pool, when the time sequence control is realized, the reflux of the nitrified liquid is cancelled, and the relation between the operation time of each section on the time sequence and the hydraulic retention time is that the operation time of the steps (3) - (5) is 20% -30% of the hydraulic retention time on the space configuration when the time sequence is realized.
Wherein the filtering speed of the multi-medium filtering tank in the step (7) is 2-5 m/h.
And (4) in the step (7), coagulation and coagulation-aid agents are not added in the coagulation sedimentation zone and the multi-medium filter tank, SS and suspended phosphorus are removed by interception in the filtering process, meanwhile, a biological membrane is formed on the surface of a filter material, the synchronous nitrification and denitrification process is realized under low dissolved oxygen, and the nitrogen is further removed, so that the deep purification of the sewage is finally realized.
Wherein the aerobic section of the main reaction zone is provided with an oxygen supply pipeline 18 for providing oxygen;
a nitrifying liquid return pipeline 15 for returning nitrifying liquid to the anoxic zone is arranged between the anoxic zone and the anaerobic section of the main reaction zone;
wherein, the nitrifying liquid return pipeline 15 is provided with a nitrifying liquid return pump 14 and a nitrifying liquid return flow meter 12.
Wherein a sludge return pipeline 16 is arranged between the settling zone 19 and the primary anaerobic zone 4;
wherein, a sludge return pump 17 is arranged on the sludge return pipeline 16;
wherein, the settling zone 19 is provided with a residual sludge discharge pipeline, and the residual sludge discharge pipeline is provided with a residual sludge pump 20.
Wherein, the steps (1) to (2) are realized by the design of a reactor configuration (a sewage natural purifying system) (figure 2); the steps (3) - (5) can be realized by space arrangement on the reactor configuration, or can be realized by time sequence operation control in a pool, when the time sequence control is realized (figure 3), the reflux of the nitrified liquid is cancelled, and the relation between the operation time of each section on the time sequence and the hydraulic retention time is that the operation time of the steps (3) - (5) is 20% -30% of the hydraulic retention time on the space configuration when the time sequence is realized.
The technical solution of the present invention is further explained by the following specific embodiments with reference to the attached drawings. It should be noted that the following specific examples are only illustrative, and the scope of the present invention is not limited thereto.
The chemicals and raw materials used in the following examples were either commercially available or self-prepared by a known preparation method.
Example 1
Certain sewage treatment plant in Shandong adopts the INSR imitative nature sewage treatment process (the imitative nature deep purification method of sewage), the amount of treated water is 3 ten thousand tons/d, INSR pond total hydraulic retention time 36h realizes through the structural optimal design of reactor (as shown in figure 2), sets up two-stage good oxygen behind the first order oxygen deficiency, and denitrogenation is reinforceed to the anaerobism section. The COD of inlet water is about 180mg/L, the total nitrogen of inlet water is about 53mg/L, the total phosphorus of inlet water is about 6mg/L, the dissolved oxygen of an aerobic zone is 0.1-0.8mg/L, the sludge concentration is 6g/L, the surface load of a precipitation zone is 0.8m/h, the outlet water of the precipitation zone is directly filtered out after coagulation precipitation, no PAC, PAM and other agents are added, the operation effect in the low-temperature period in winter is good, the problem that ammonia nitrogen does not reach the standard is avoided, the energy consumption per ton of water in the current operation is 0.18-0.30kW/t, and the operation cost is lower. In the operation process, the denitrification effect is improved by controlling the ORP in the aerobic zone and the ammonia nitrogen in the effluent of the precipitation zone to be about 4 mg/L. COD of the conventional effluent is about 15mg/L (shown in figure 4), total nitrogen of the effluent is about 6mg/L (shown in figure 5), total phosphorus of the effluent is about 0.05mg/L (shown in figure 6), and SS of the effluent is about 6 mg/L.
Example 2
A certain sewage treatment plant in Jiangsu adopts the imitative natural sewage treatment process of INSR, the handling capacity is 6 ten thousand tons/d, realize through the chronogenesis control of reactor operation, the reactor configuration is like (fig. 3) realization, carry out the oxygen deficiency stirring after the good oxygen aeration and strengthen the denitrogenation effect, its operation chronogenesis is for intaking stirring 1h, stirring denitrogenation 1h, aeration 2h, denitrogenation 0.5h after the stirring, deposit 1h, drainage 0.5 h. The total hydraulic retention time of the biochemical pool is 26 hours, the dissolved oxygen is controlled to be 0.3-1.5mg/L in the aeration process, the COD of the inlet water is about 300mg/L, the total nitrogen of the inlet water is about 45mg/L, the total phosphorus of the inlet water is about 5mg/L, the sludge concentration is 5g/L, the problem of low denitrification efficiency is not found in the low-temperature period in winter, the energy consumption per ton of water in the prior art is 0.30-0.50kW/t, and the operation cost is lower. In the operation process, the denitrification effect is improved by controlling the ORP and the effluent ammonia nitrogen in the aerobic zone to be about 2 mg/L. COD of the conventional total effluent is about 30mg/L, total nitrogen of the total effluent is about 5mg/L, total phosphorus of the total effluent is about 0.01mg/L, and SS of the effluent is about 7 mg/L. At present, the energy consumption of the operation per ton of water is 0.15-0.20 kW/t.
Example 3
A rural sewage treatment station in a certain Beijing area adopts the INSR natural sewage treatment imitating technology, the treated water amount is 50 tons/d, the optimization design on the reactor configuration is realized, the reactor configuration is shown in figure 2, the discharged water adopts a ceramic membrane to suck the discharged water, two-stage aerobic is arranged after the first-stage oxygen deficiency, and the denitrification is strengthened in an anaerobic section. The COD of the inlet water is about 160mg/L, the total nitrogen of the inlet water is about 40mg/L, the total phosphorus of the inlet water is about 3mg/L, and the designed water flux of the outlet water membrane is 25L/m2And h, the energy consumption of the current operation per ton of water is 0.60-0.83 kW/t. In the operation process, the denitrification effect is improved by controlling the dissolved oxygen in the aerobic zone to be about 0.5mg/L, and the sludge concentration is 12 g/L. COD of the effluent is about 35mg/L (figure 4), total nitrogen of the effluent is about 10mg/L (figure 5), total phosphorus of the effluent is about 0.2mg/L (figure 6), and SS of the effluent is about 2 mg/L.
The above-mentioned embodiments, further detailed description of the objects, technical solutions and advantages of the present invention, it should be understood that the above-mentioned embodiments are only specific embodiments of the present invention, and are not intended to limit the present invention, and any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (10)
1. The utility model provides an imitative natural purification system of sewage which characterized in that includes:
the primary anaerobic zone is provided with a primary anaerobic zone water inlet and a primary anaerobic zone water outlet;
the anoxic zone is provided with an anoxic zone water inlet and an anoxic zone water outlet, and the anoxic zone water inlet is communicated with the primary anaerobic zone water outlet;
the main reaction zone is provided with a main reaction zone water inlet and a main reaction zone water outlet, and the main reaction zone water inlet is communicated with the anoxic zone water outlet; and
the settling zone is communicated with a water inlet of the settling zone and a biochemical water outlet, and the water inlet of the settling zone is communicated with the water outlet of the main reaction zone.
2. The purification system of claim 1,
the purification system comprises a sand-water separation area for precipitating inorganic particles, wherein the sand-water separation area is provided with a separation area water inlet and a separation area water outlet, and the separation area water outlet is connected with the primary anaerobic area water inlet.
3. The purification system of claim 2,
and a pre-acidification area for regulating and tempering inlet water is arranged between the anaerobic area and the sand-water separation area.
4. The purification system of claim 1,
the main reaction zone comprises a plurality of stages of main reaction zone aerobic sections and main reaction zone anaerobic sections which are connected in series or the main reaction zone comprises a main reaction tank.
5. The purification system of claim 1,
the aerobic section of the main reaction zone is provided with an air supply pipeline for providing oxygen.
6. The purification system of claim 5,
a nitrifying liquid return pipeline for returning nitrifying liquid to the anoxic zone is arranged between the anoxic zone and the anaerobic section of the main reaction zone;
and a nitrifying liquid reflux pump and a nitrifying liquid reflux flowmeter are arranged on the nitrifying liquid reflux pipeline.
7. The purification system of claim 1,
a sludge return pipeline is arranged between the sedimentation zone and the primary anaerobic zone;
and a sludge return pump is arranged on the sludge return pipeline.
8. The purification system of claim 1,
and the settling zone is provided with a residual sludge discharge pipeline, and the residual sludge discharge pipeline is provided with a residual sludge pump.
9. The purification system of claim 1,
the purification system comprises a filter tank, and a water inlet of the filter tank is connected with a water outlet of the sedimentation zone.
10. The purification system of claim 1,
the depth of each zone of the purification system is 7-9 m.
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