CN114249420B - Anaerobic ammonia oxidation starting, culturing and running method and system - Google Patents
Anaerobic ammonia oxidation starting, culturing and running method and system Download PDFInfo
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Abstract
The invention discloses a method and a system for starting, culturing and operating anaerobic ammoxidation, wherein the method comprises the steps of introducing drainage of an anaerobic ammoxidation test device into a denitrification tank in a starting stage, carrying out sequencing batch operation of introducing drainage, dosing and stirring reaction, stopping stirring and standing, discharging supernatant until anaerobic ammoxidation activity appears, entering a culturing stage, adding a reagent, controlling the pH value to a set value along with the rise of the pH value in the tank, balancing the pH value to be a reaction end point, entering an operation stage when the nitrogen load or the concentration of strains reaches the set value, carrying out sequencing batch operation in a nitrification tank according to water inlet denitrification, aeration and nitrosation, standing and drainage until short-range sludge acclimation is successful, connecting the denitrification tank with the nitrification tank in series, and adopting a mode of gradually increasing the nitrogen load of the nitrification tank to the denitrification tank and gradually reducing dosing to provide the nitrogen load until full wastewater operation is realized. The method and the system have the advantages of quick strain starting, quick culture speed, good effect, low energy consumption and the like.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a method and a system for starting, culturing and operating anaerobic ammonia oxidation.
Background
Along with the continuous expansion of the urban scale, the sewage treatment scale is also increasing. Sewage denitrification is an important link in the sewage treatment process, and research and development of economical and efficient denitrification technology and realization of carbon emission reduction are important research points in the field of sewage treatment in the future. The current sewage biochemical treatment technology with the most mature application and the widest application range takes the nitrification and denitrification technology as the core, but has two unavoidable problems of high operation energy consumption and high carbon emission.
The anaerobic ammonia oxidation technology is the biological denitrification technology with the lowest energy consumption discovered at present, has the advantages of low energy consumption for supply, no need of organic carbon source, high volume load, low sludge yield and the like, and is praised as the sewage denitrification technology with the most prospect. Anaerobic ammonia oxidizing bacteria are bacteria belonging to the phylum of the floating mould, the appearance of the bacteria is red, and the rhodobacter sphaeroides are common names of the anaerobic ammonia oxidizing bacteria in the industry. The cell wall of the anaerobic ammonia oxidation bacteria is provided with a volcanic mouth or funnel-shaped structure, and the bacteria are propagated in a bud mode. But the anaerobic ammonia oxidation strain is different from the traditional nitrifying/denitrifying bacteria group, and has very slow growth speed, high difficulty in culture enrichment and harsh growth conditions. Therefore, the anaerobic ammonia oxidation bacteria are generally commonly known in the sewage treatment industry to be difficult to culture and enrich, and the control condition is strict, so that the anaerobic ammonia oxidation bacteria are also an important reason that the process is difficult to apply to a large scale in the engineering field. The biochemical formula of anaerobic ammoxidation is as follows:
NH 4 + +1.32NO 2 - +0.066HCO 3 - +0.12H + →N 2 +0.26NO 3 - +0.066CH 2 O 0.5 N 0.15 +2.03H 2 O
the related patents of the prior anaerobic ammonia oxidation technology and application mainly relate to methods such as reactor optimization, anaerobic ammonia oxidation strain simulation wastewater cultivation, anaerobic ammonia oxidation strain screening optimization, and the like, and mainly relate to a strain optimization method which combines a specific anaerobic ammonia oxidation reactor with the prior sewage treatment technology to optimize, improves the activity of the prior anaerobic ammonia oxidation strain, and screens the anaerobic ammonia oxidation strain through an adjusting tank. However, the following problems exist in the current system and technical process for starting, culturing and running anaerobic ammonium oxidation bacteria:
(1) Anaerobic ammonia oxidation strain proliferation rate is very slow, source is narrow, selling price is high, whole reserves in industry are low, technology and strain source monopoly exist, and popularization and application of the technology are limited to a certain extent.
(2) Most of the existing anaerobic ammonia oxidation reactors are UASB, EGSB, IC in configuration, high in parameter requirement and high in construction cost, and the reactors are additionally constructed on the optimization and upgrading of the existing large-scale AO cell body process.
(3) Anaerobic ammonia oxidation strain culture conditions are harsh, the anaerobic ammonia oxidation strain culture conditions are sensitive to the environment, the operation stability is weak, and especially for high-concentration complex wastewater, the front-end pretreatment flow is complex, and the influence of water quality is great.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a method and a system for starting, culturing and operating anaerobic ammonia oxidation, which have the advantages of high strain starting speed, high culturing speed, good effect and low energy consumption.
In order to solve the technical problems, the invention adopts the following technical scheme.
A method for anaerobic ammoxidation start-up, cultivation and operation, comprising the steps of:
s1, starting: introducing the drainage of the anaerobic ammonia oxidation test device into a denitrification tank, controlling the water temperature in the tank to be 30-35 ℃, adding a medicament to maintain the ammonia nitrogen concentration in the tank to be 50-100mg/L, the nitrite nitrogen concentration to be 10-50mg/L, and regulating the pH value in the tank to be 7.0-8.0 according to the total alkalinity of 100-1000mg/L and calculated by calcium carbonate, keeping the tank in a stirring state, stopping stirring and standing when the high liquid level set in the denitrification tank is reached, discharging supernatant until the low liquid level set in the denitrification tank is reached, so as to introduce drainage-dosing stirring reaction, stopping stirring and standing, discharging supernatant to be a sequencing batch period, performing sequencing batch operation until anaerobic ammonia oxidation activity appears, and finishing the starting stage;
s2, culturing: after the start-up stage is completed, a reaction matrix is provided in the denitrification tank in a mode of adding medicine and water, a medicine is added, the concentration of nitrite nitrogen in the tank is ensured to be not higher than 200mg/L, the water temperature in the denitrification tank is controlled to be 30-35 ℃, along with the rising of the pH value in the tank, acid is added to control the pH value in the tank to be 7.0-8.0, when the pH value is no longer rising and is in a trend, the reaction end point is the sequencing batch period reaction end point, the concentration of ammonia nitrogen at the reaction end point in each sequencing batch period tank is ensured to be 50-100mg/L, the concentration of nitrite nitrogen is ensured to be 0-10mg/L, and after a period of operation, the total nitrogen removal load in the tank is not less than 0.3 kgN/(m) 3 D) or when the strain concentration is more than or equal to 1g/L, entering the next step;
s3, operation phase:
s3.1, starting a nitrifying pond: inoculating nitrified sludge and wastewater, introducing into a nitrifying pond, and performing denitrification, aeration nitrosation, standing and discharging according to the inlet waterThe four steps of water are performed in a sequencing batch mode, and the biochemical conditions of aeration nitrosation are as follows: dissolved oxygen DO is 0.5 mg/L-1.0 mg/L, water temperature is 30-35 ℃, pH is maintained at 7.0-8.0, and when c (NO) in the nitrifying pond 2 - )/c(NH 4 + ) > 1.0, and c (NO 2 - )/c(NO 3 - ) When the ratio of the nitrite nitrogen mass concentration to the ammonia nitrogen mass concentration in the effluent is more than 10, the characteristic of successful short-cut nitrification sludge domestication is adjusted to be 1.1-1.3;
s3.2, connecting a denitrification tank and a nitrification tank in series: the denitrification tank is connected with the nitrification tank in series, the denitrification tank is operated in a sequencing batch mode according to four steps of water inlet and medicine adding-stirring reaction-stopping stirring standing-supernatant discharging, the nitrification tank is operated in a sequencing batch mode according to four steps of water inlet denitrification-aeration nitrosation-standing-supernatant discharging, in a single sequencing batch period, when the supernatant liquid is discharged from the denitrification tank until reaching a set low liquid level, the supernatant liquid of the nitrification tank is introduced into the denitrification tank until reaching a set high liquid level of the denitrification tank, and then the nitrification tank starts to feed wastewater; the method comprises the steps of gradually increasing the nitrogen load from a nitrification tank to a denitrification tank and gradually reducing the external dosing to provide the nitrogen load, wherein the total nitrogen amount of nitrite nitrogen and ammonia nitrogen provided by the nitrification tank is gradually increased according to the proportion of 10% -20%, and the total nitrogen amount provided by the external dosing is gradually decreased according to the proportion of 10% -20%, until the whole wastewater operation is realized.
In the method for starting, culturing and operating anaerobic ammonia oxidation described above, preferably, in step S1, the determination flag for the occurrence of the anaerobic ammonia oxidation activity is: in a sequencing batch period, the ammonia nitrogen concentration and the nitrite nitrogen concentration synchronously drop, and the removal amount m (nitrite nitrogen) of the nitrite nitrogen and the removal amount m (ammonia nitrogen) of the ammonia nitrogen are 1.2-1.4.
In the method for starting, culturing and operating anaerobic ammonia oxidation, preferably, in step S1, the chemical includes a chemical containing nitrogen element, inorganic carbon and a chemical containing nutrient element; the nitrogen-containing agent comprises nitrite and ammonium salt, wherein the nitrite comprises sodium nitrite and/or potassium nitrite, and the ammonium salt comprises ammonium chloride and/or ammonium sulfate; the inorganic carbon is sodium bicarbonate, and the medicament containing nutrient elements comprises CaCl 2 ·2H 2 O、FeSO 4 、MgSO 4 ·7H 2 O、KH 2 PO 4 、EDTA、KHCO 3 、MnCl 2 ·4H 2 O、ZnSO 4 ·7H 2 O、NiCl 2 ·6H 2 O、CuSO 4 ·5H 2 O and NaMoO 4 ·2H 2 O, and the agent added in the steps S2 and S3 is the same as the agent added in the step S1.
In the method for starting, culturing and operating the anaerobic ammonia oxidation, preferably, in the step S1, the water temperature in the tank is controlled at 33-35 ℃, and the ammonia nitrogen concentration in the tank is maintained at 50-80mg/L, the nitrite nitrogen concentration is maintained at 30-50mg/L, the total alkalinity is 300-500mg/L, and the pH value is controlled at 7.5-8.0 by adding the medicament.
In the method for starting, culturing and operating the anaerobic ammonia oxidation, preferably, in the step S2, the pH value in the pond is controlled to be 7.5-8.0, and the total alkalinity in the pond is controlled to be 500-1000mg/L based on calcium carbonate.
In the anaerobic ammonia oxidation starting, culturing and running method, preferably, in the step S1 and the step S2, the water temperature in the denitrification tank is controlled by adding RO purified water, wastewater discharged from a sewage plant or tap water, the stirring stopping and standing time is 10-60 min, and the pH value is controlled by adding hydrochloric acid or sulfuric acid; and/or in the steps S1, S2 and S3, strain interception and strain recycling are carried out on the supernatant discharged from the denitrification tank.
In the method for starting, culturing and operating the anaerobic ammonia oxidation, preferably, in step S3.1, the water temperature of the nitrifying pond is regulated by a cooling device, and the pH value in the pond is maintained by adding alkali.
In the method for starting, culturing and operating the anaerobic ammonia oxidation, preferably, in the step S3.2, the increasing period is 7 days to 30 days, and the decreasing period is 7 days to 30 days.
The invention also provides a system for starting, culturing and operating the anaerobic ammonia oxidation, which comprises a denitrification tank, a nitrification tank and an anaerobic ammonia oxidation test device, wherein the anaerobic ammonia oxidation test device is communicated with the denitrification tank, and the nitrification tank is communicated with the denitrification tank.
The anaerobic ammonia oxidation starting, culturing and running system is characterized in that the anaerobic ammonia oxidation test device is communicated with the denitrification tank through a first water inlet pump, the nitrification tank is communicated with the denitrification tank through a second water inlet pump, the nitrification tank is connected with a third water inlet pump, and the denitrification tank is connected with a water outlet pump.
The anaerobic ammonia oxidation starting, culturing and running system is characterized in that the denitrification tank is provided with a stirrer, a first pH meter, a first temperature meter and a first liquid level meter, the denitrification tank is communicated with an acid adding device, and the denitrification tank is communicated with a interception barrel through a water outlet pump.
The anaerobic ammonia oxidation starting, culturing and running system is characterized in that an aeration device is preferably arranged in the nitrification tank, the nitrification tank is further provided with a second pH meter, a second temperature meter and a second liquid level meter, the nitrification tank is communicated with an alkali adding device, and a cooling tower is arranged between the nitrification tank and a third water inlet pump.
The anaerobic ammonia oxidation starting, culturing and running system preferably further comprises a PLC controller, wherein the first pH meter, the first thermometer, the first liquid level meter, the second pH meter, the second thermometer and the second liquid level meter are respectively connected with the input end of the PLC controller, and the output end of the PLC controller is respectively connected with the acid adding device, the nitrification tank, the second water inlet pump, the water outlet pump, the alkali adding device, the cooling tower and the third water inlet pump.
Compared with the prior art, the invention has the advantages that:
(1) The invention develops an integrated and self-controlled system which is formed by utilizing an anaerobic ammonia oxidation test device as a strain starting source and utilizing an improved nitrification and denitrification tank body as a strain starting and culturing place, and establishes a method for starting, culturing and operating the anaerobic ammonia oxidation, thereby achieving the effects of quick strain starting and culturing speed, good effect and low energy consumption. Compared with the traditional nitrification and denitrification process, the anaerobic ammonia oxidation process has the advantages of high operation energy consumption, high treatment efficiency, high treatment yield and the like.
(2) The method for culturing, enriching and operating the anaerobic ammonia oxidation system achieves higher strain quantity and treatment load in a relatively shorter time, shortens the conversion period from a test scale to a production scale, and saves the cost required by purchasing large-scale strains. According to the invention, the tiny bacteria particles contained in the anaerobic ammonia oxidation test drainage are continuously enriched and cultivated in the culture pond, and the different control parameters of the three stages of starting, cultivating and running are controlled, so that the higher bacterial number and treatment load are achieved in a relatively shorter time, and the conversion period from the test scale to the production scale is shortened.
(3) Compared with the newly-built UASB, EGSB, IC reactor and other reactors, the system with the cooperation of the anaerobic ammonia oxidation test device and the nitrification and denitrification Chi Tixiang can fully utilize the existing tank body in the process technology upgrading of the sewage plant, only needs to carry out partial transformation, does not need to newly build a reactor, and greatly reduces the transformation cost. The system of the invention uses fine bacteria particles and starting factors contained in the drainage of the anaerobic ammonia oxidation test device as inoculation starting sources, and uses the partially improved nitrification and denitrification tank body as the places of two reaction stages of anaerobic ammonia oxidation respectively, and simultaneously, each parameter of the system is adjusted to realize automatic control.
(4) According to the invention, a denitrification function is introduced in a nitrosation process section by adopting a sequencing batch operation mode, so that the COD content in the wastewater is reduced and the exhaust oxygen content is reduced by denitrification while the nitrogen conversion is realized, a high aeration tank required by other technologies is omitted, the energy consumption is lower, the operation stability of anaerobic ammoxidation under the impact of severe water quality is improved, and the purity of the strain is higher.
Drawings
FIG. 1 is a schematic diagram of the system for starting, culturing and operating anaerobic ammonium oxidation in example 1 of the present invention.
Legend description:
1. a denitrification tank; 2. a nitrifying pond; 3. an anaerobic ammonia oxidation test device; 4. a stirrer; 5. an aeration device; 6. a cooling tower; 7. a first water inlet pump; 8. a second water inlet pump; 9. a third water inlet pump; 10. a water outlet pump; 11. a retaining barrel; 12. a first pH meter; 13. a first thermometer; 14. a first level gauge; 15. a PLC system; 16. an acid adding device; 17. an alkali adding device; 18. a second pH meter; 19. a second thermometer; 20. and a second level gauge.
Detailed Description
The invention is further described below in connection with the drawings and the specific preferred embodiments, but the scope of protection of the invention is not limited thereby. The materials and instruments used in the examples below are all commercially available.
Example 1:
the method for starting, culturing and running the anaerobic ammonia oxidation comprises the following steps:
s1, starting: the anaerobic ammonia oxidation test device 3 is normally drained every day and introduced into a denitrification tank 1 (also called as a tank A), and water sources with low COD content such as drain water outside a sewage plant, tap water and the like can be added together according to the water temperature in the tank to control the water temperature in a culture tank, and meanwhile, a medicament is added to maintain a certain substrate concentration in the tank, wherein the dosing types comprise nitrogen element, inorganic carbon and nutrient element. And (3) keeping the interior of the tank in a stirring state, stopping stirring and standing for 10min when the set high liquid level of the denitrification tank 1 is reached, discharging supernatant, intercepting strains and recycling strains on the discharged supernatant, continuously introducing water when the set low liquid level is reached, externally adding drugs, starting stirring reaction, stopping stirring and standing, discharging supernatant, namely, taking the water drainage-drug adding stirring reaction-stirring stopping stirring and standing-discharging supernatant as a sequencing batch cycle, repeating the steps until the anaerobic ammonia oxidation activity appears, finishing the starting stage, and stopping the anaerobic ammonia oxidation test device 3. The invention sets the judgment mark of the anaerobic ammoxidation activity in the pool as follows: in one water inlet and outlet period, ammonia nitrogen and nitrite nitrogen concentrations synchronously decrease, and m (removal amount of nitrite nitrogen): m (ammonia nitrogen removal amount) is 1.2-1.4.
In this start-up phase:
the nitrogen element comprises one or two of sodium nitrite and potassium nitrite and one or two of ammonium chloride and ammonium sulfate, and NH in the pond is controlled 4 + Ammonia nitrogen concentration of 50-100mg/L, NO 2 - The concentration is 10-50mg/L;
the inorganic carbon is sodium bicarbonate, and the concentration of the total alkalinity (calculated by calcium carbonate) is controlled to be 100-1000mg/L;
the nutrient elements comprise CaCl 2 ·2H 2 O、FeSO 4 、MgSO 4 ·7H 2 O、KH 2 PO 4 、EDTA、KHCO 3 、MnCl 2 ·4H 2 O、ZnSO 4 ·7H 2 O、NiCl 2 ·6H 2 O、CuSO 4 ·5H 2 O and NaMoO 4 ·2H 2 One or more substances in O are configured.
Controlling the water temperature in the pool to be 30-35 ℃.
Adding hydrochloric acid or sulfuric acid according to the pH change in the tank to control the pH in the tank to 7.0-8.0, and preferably 7.5-8.0.
S2, culture and proliferation stage
When the starting stage is completed, a sufficient amount of reaction matrix is provided according to the nitrogen removal load in the denitrification tank 1, and the type of the added medicament is consistent with that of the starting stage. The dosing adopts a single batch or multiple batch dosing mode every day, the water temperature in the wastewater or tap water control tank outside the sewage plant is 30-35 ℃, and the concentration of the nitrite nitrogen in the denitrification tank 1 is ensured to be not higher than 200mg/L.
Along with the rising of the pH value, the pH value in the diluted hydrochloric acid or sulfuric acid adding pond is controlled to be 7.0-8.0, and the preferable range is 7.5-8.0. When the pH curve is no longer rising and is leveled, the moment is the batch reaction end point. By adjusting the adding proportion and the adding amount of sodium nitrite and ammonium chloride, the concentration of ammonia nitrogen at the reaction end point in the tank in each batch of detection data is ensured to be 50-100mg/L, and the concentration of nitrite nitrogen is ensured to be 0-10mg/L.
After a period of operation, when the load in the tank reaches 0.3 kgN/(m) 3 D) and above, or when the strain concentration reaches 1g/L and above, proceeding to the next step.
S3, operation stage
1. Nitrification tank 2 (O tank) start-up
Inoculating conventional nitrified sludge into a nitrifying pond 2, and separating inflow water for denitrification and aeration for nitrosation in a sequencing batch operation modeThe four steps of chemical treatment, standing and drainage are carried out, the aim of removing most BOD is achieved in the water inlet denitrification stage, and biochemical conditions are controlled in the aeration denitrification stage: DO is 0.5-1.0mg/L, water temperature is 30-35 ℃, and pH is maintained at 7.0-8.0. When c (NO) 2 - )/c(NH 4 + ) > 1.0, and c (NO 2 - )/c(NO 3 - ) And when the sludge is more than 10, the short-range sludge domestication is successfully characterized. The total nitrogen in the wastewater can be partially converted into nitrite nitrogen through aeration, the concentration ratio of nitrite nitrogen to ammonia nitrogen in the effluent can be regulated to be 1.1-1.3 by controlling the aeration time length and alkalinity supplement, and a reaction matrix is provided for the anaerobic ammonia oxidation culture pond.
2. The denitrification tank 1 (A tank) is connected in series with the nitrification tank 2 (O tank)
The denitrification tank (1) and the nitrification tank (2) are connected in series, the denitrification tank (1) performs sequencing batch operation according to four steps of water inlet and chemical adding-stirring reaction-stopping stirring standing-supernatant discharging, the nitrification tank (2) performs sequencing batch operation according to four steps of water inlet denitrification-aeration nitrosation-standing-supernatant discharging, and in a single sequencing batch period, when the supernatant is discharged from the denitrification tank (1) until reaching a set low liquid level, the supernatant of the nitrification tank (2) is introduced into the denitrification tank (1) until reaching a set high liquid level of the denitrification tank (1), and then the nitrification tank (2) starts to feed wastewater. In order to achieve the purposes of gradually adapting to actual wastewater by the anaerobic ammonia oxidation strain and reducing the impact of the water of the actual wastewater on the anaerobic ammonia oxidation strain, a method of gradually increasing the nitrogen load of a nitrifying pond 2 to a denitrifying pond 1 and gradually reducing the nitrogen load provided by external dosing is adopted, wherein the total nitrogen provided by the nitrifying pond 2 (nitrosamine plus ammonia nitrogen) is gradually increased according to the proportion of 10-20%, the total nitrogen provided by external dosing is gradually decreased according to the proportion of 10-20%, and the increasing period and the decreasing period are both 7-30 days.
The anaerobic ammonia oxidation start-up, culture and operation system of the present invention may be used for the anaerobic ammonia oxidation start-up, culture and operation method of the present embodiment, but is not limited thereto.
The system comprises a denitrification tank 1, a nitrification tank 2 and an anaerobic ammonia oxidation test device 3, wherein the anaerobic ammonia oxidation test device 3 is communicated with the denitrification tank 1, and the nitrification tank 2 is communicated with the denitrification tank 1.
In this embodiment, anaerobic ammonia oxidation test device 3 communicates with denitrification tank 1 through first intake pump 7, and nitrification tank 2 communicates with denitrification tank 1 through second intake pump 8, and nitrification tank 2 is connected with third intake pump 9, and denitrification tank 1 is connected with water pump 10.
In this embodiment, the denitrification tank 1 is provided with a stirrer 4, a first pH meter 12, a first temperature meter 13 and a first liquid level meter 14, the denitrification tank 1 is communicated with an acid adding device 16, and the denitrification tank 1 is communicated with a interception barrel 11 through a water outlet pump 10.
In the embodiment, an aeration device 5 is arranged in the nitrification tank 2, the nitrification tank 2 is also provided with a second pH meter 18, a second temperature meter 19 and a second liquid level meter 20, the nitrification tank 2 is communicated with an alkali adding device 17, and a cooling tower 6 is arranged between the nitrification tank 1 and the third water inlet pump 9.
In this embodiment, the system further includes a PLC controller 15, where the first pH meter 12, the first temperature meter 13, the first liquid level meter 14, the second pH meter 18, the second temperature meter 19, and the second liquid level meter 20 are respectively connected to an input end of the PLC controller 15, and an output end of the PLC controller 15 is respectively connected to the acid adding device 16, the nitrification tank 2, the second water inlet pump 8, the water outlet pump 10, the alkali adding device 17, the cooling tower 6, and the third water inlet pump 9. Wherein, the first pH meter 12 is connected with the acid adding device 16, the first temperature meter 13 is connected with the nitrifying pond 2, the second temperature meter 19 in the nitrifying pond 2 is connected with the cooling tower 6, the first liquid level meter 14 is connected with the second water inlet pump 8 and the water outlet pump 10, the second pH meter 18 is connected with the alkali adding device 17, and the second liquid level meter 20 is connected with the second water inlet pump 8 and the third water inlet pump 9, thereby realizing self-control pH, water temperature and liquid level adjustment.
In this embodiment, the denitrification tank 1 and the nitrification tank 2 are isolated to form two independent tank structures, and the denitrification tank 1 and the nitrification tank 2 can share one side wall. The denitrification tank 1 is used as an anaerobic ammoxidation culture tank in the system and adopts a sequencing batch operation mode. The stirrer 4 in the denitrification tank 1 adopts a hyperboloid disc or stirring paddle structure, and the rotating speed is 20-60rpm. The interception barrel 11 adopts a filter screen with 80 meshes and more to intercept. The nitrifying pond 2 is used as a nitrosation pond in the system and adopts a sequencing batch operation mode.
The system of the invention uses fine bacteria particles and starting factors contained in the drainage of the anaerobic ammonia oxidation test device as inoculation starting sources, and uses the partially improved nitrification and denitrification tank body as the places of two reaction stages of anaerobic ammonia oxidation respectively, and simultaneously, each parameter of the system is adjusted to realize automatic control.
The following is an application example of the method and system for starting, culturing and running anaerobic ammonia oxidation in this embodiment, and the water quality index of the digestion liquid of a municipal sludge project is as follows: the ammonia nitrogen concentration is 1900mg/L, the total nitrogen concentration is 2000mg/L, COD and 2200mg/L, the total alkalinity is 2800mg/L, the water temperature is 45 ℃, the pH is 7.9, and the wastewater with high ammonia nitrogen and low C/N ratio is typical. The project digestive juice treatment process adopts two stages of AO, the invention uses one stage of AO, and the effective volume of pool A is 425m 3 (specific size is lbh=8.0×7.6×7.0, unit m), and effective volume of pool O is 453m 3 (specific dimensions are l×b×h=8.0×8.1×7.0), implemented according to the procedure of this example:
s1, start-up phase
And (3) carrying out isolation transformation on the pool A (the denitrification pool 1) and the pool O (the nitrification pool 2), and emptying the pool A. Normally draining water of some anaerobic ammonia oxidation pilot test device around the project for 20m 3 And/d is introduced into the pool A through a first water inlet pump 7, wherein the pool A adopts a hyperboloid stirrer, and the rotating speed is 31rpm/min. Because the liquid level in the initial pond is low and the temperature is difficult to maintain, adding a certain amount of RO purified water every day to control the water temperature in the culture pond to be 33-35 ℃, simultaneously adding sodium nitrite, ammonium chloride and sodium bicarbonate medicament, maintaining the ammonia nitrogen concentration in the pond to be 50-80mg/L, the nitrite nitrogen concentration to be 30-50mg/L, the total alkalinity to be 300-500mg/L, regulating the pH range in the pond to be 7.5-8.0, simultaneously adding configuration nutrient elements, and adding CaCl 2 ·2H 2 O concentration is 0.01g/L, feSO 4 The concentration is 0.01g/L, mgSO 4 ·7H 2 O concentration is 0.3g/L, KH 2 PO 4 The concentration is 0.03g/L, and the stirrer 4 is started to keep the stirring state in the tank. Stopping stirring and standing for 10min when the water level of the pool A reaches the water level (the water level is 7.0 m), discharging supernatant to a low parameter level (the water level is 6.0 m) by a water outlet pump 10, then continuously introducing water discharge and external medicine adding, starting stirring, stopping stirring and standing, and dischargingWater, and repeating the steps until anammox activity occurs.
After 3 months of operation, in a water inlet and outlet period, ammonia nitrogen and nitrite nitrogen in the tank synchronously drop, and the removal ratio of m (nitrite nitrogen) to m (ammonia nitrogen) is 1.3, which indicates that the anaerobic ammonia oxidation activity is successfully started.
S2, culture stage
The reaction matrix is provided in a dosing and water distribution mode, and dosing is carried out 2 batches per day with an interval time of 12 hours. Adding ammonium chloride and sodium nitrite medicaments into each batch, wherein NH in the added ammonium chloride 4 + And NO in sodium nitrite 2 - According to the mass ratio of 1:1.2. Diluting water with RO purified water, controlling water temperature in the tank to be 30-35deg.C for 2 batches each day, adding the same nutrition elements as in step S1, and adding sodium bicarbonate to control alkalinity to be 500-1000mg/L.
According to the rise of the pH in the tank, the PLC system controls the acid adding device 16 to add the diluted hydrochloric acid solution to control the pH in the tank to be 7.5-8.0. When the pH curve is not increased any more and is leveled, the moment is the end point of the batch reaction, stirring is stopped, standing is carried out for 10min, supernatant is discharged to a low-parameter liquid level through a water outlet pump, water is intercepted by an interception barrel 11 (a 80-mesh filter screen), and the intercepted strain returns to the tank. By adjusting the adding proportion and the adding amount of sodium nitrite and ammonium chloride, the concentration of ammonia nitrogen at the reaction end point in the tank in each batch of detection data is ensured to be 50-100mg/L, and the concentration of nitrite nitrogen is ensured to be 0-10mg/L.
After 3 months of operation, the total nitrogen removal load in the pool A reaches 0.35 kgN/(m) 3 D) and the strain concentration reaches 2.3g/L.
S3, operation stage
1. O pool start-up
The conventional nitrified sludge in the O tank is domesticated, the sludge digestion liquid enters through a third water inlet pump 9, MLSS in the tank is 5g/L, four steps of water inlet denitrification, aeration nitrosation, standing and drainage are adopted to run in sequence, DO is controlled to be 0.5-1.0mg/L through an aeration device 5 in the aeration nitrosation stage, the water inlet temperature is regulated through the start and stop of a cooling tower 6 to ensure that the water temperature in the tank runs at 30-35 ℃, and an alkali adding device 17 is controlled to add liquid alkali to maintain the pH value in the tank to be 7.0 through a PLC (programmable logic controller) 15-7.5 range. After 1 month of acclimatization, c (NO 2 - ) 800mg/L, c (NH) 4 + ) 650mg/L, c (NO 3 - ) The concentration is 50mg/L, which represents successful short-range sludge acclimation, and the concentration ratio of nitrite nitrogen to ammonia nitrogen is 1.23.
2. The pool A is connected in series with the pool O
The tank A and the tank O are in a sequencing batch operation mode, the tank A operates according to four steps of water inlet and medicine adding, stirring reaction, stopping stirring standing and supernatant discharging, the tank O operates according to four steps of water inlet denitrification, aeration nitrosation, standing and drainage, the PLC controller 15 controls in a sequencing batch period, the pH in the tank A is controlled to be 7.5-8.0 along with the rising of the pH in the tank A, the PLC system controls the acid adding device 16 to add diluted hydrochloric acid solution, stirring and standing are stopped for 10min, supernatant is discharged through the water outlet pump 10 until the liquid level is low, the water outlet is intercepted by the interception barrel 11 (80-mesh filter screen), the intercepted strain returns to the tank, then the second water inlet pump 8 introduces the supernatant of the tank O to the tank A to the liquid level of the tank Gao Canshu, the tank O starts to enter sludge digestion liquid, the aeration nitrosation is performed for 6 hours, the water inlet nitrosation is performed for 14 hours, the standing is performed for 1 hour, the water drainage is performed for 3 hours, the sequencing batch operation mode is controlled, DO is 0.3mg/L in the water inlet nitrosation process, the DO is 1.0mg/L in the water temperature is controlled to be 7.0 mg/L, and the pH is controlled to be 7.0.0.0.
The early stage is carried out by combining partial wastewater and partial dosing, wherein the first week is carried out according to the method that the wastewater provides 20% of nitrogen load and the dosing provides 80% of nitrogen load, the second week is carried out according to the method that the wastewater gradually increases and the dosing gradually decreases, and the full wastewater operation is realized until the 5 th week. After 6 months of operation, the treatment load of the pool A was increased to 0.8 kgN/(m) 3 D), the sludge digestion liquid is processed by the system to reach 200m 3 And/d, and meanwhile, the sludge concentration of the anaerobic ammonia oxidation granule bacteria is increased to 3.5g/L.
The above description is only of the preferred embodiment of the present invention, and is not intended to limit the present invention in any way. While the invention has been described in terms of preferred embodiments, it is not intended to be limiting. Any person skilled in the art can make many possible variations and modifications to the technical solution of the present invention or equivalent embodiments using the method and technical solution disclosed above without departing from the spirit and technical solution of the present invention. Therefore, any simple modification, equivalent substitution, equivalent variation and modification of the above embodiments according to the technical substance of the present invention, which do not depart from the technical solution of the present invention, still fall within the scope of the technical solution of the present invention.
Claims (10)
1. A method for starting, culturing and operating anaerobic ammoxidation, which is characterized by comprising the following steps:
s1, starting: introducing the drainage of the anaerobic ammonia oxidation test device (3) into a denitrification tank (1), controlling the water temperature in the tank to be 30-35 ℃, adding a medicament to maintain the ammonia nitrogen concentration in the tank to be 50-100mg/L, the nitrite nitrogen concentration to be 10-50mg/L, and regulating the pH value in the tank to be 7.0-8.0 according to the total alkalinity of 100-1000mg/L, wherein the pH value in the tank is regulated to be in a stirring state, stopping stirring and standing when the high liquid level set by the denitrification tank (1) is reached, discharging supernatant until the low liquid level set by the denitrification tank (1) is reached, introducing drainage-dosing stirring reaction, stopping stirring and standing, discharging supernatant to be a sequencing batch period, and performing sequencing batch operation until anaerobic ammonia oxidation activity appears, and finishing the starting stage;
s2, culturing: after the start-up stage is completed, a reaction matrix is provided in the denitrification tank (1) in a mode of adding medicines and water, the concentration of nitrite nitrogen in the tank is ensured to be not higher than 200mg/L, the water temperature in the denitrification tank (1) is controlled to be 30-35 ℃, acid is added along with the rise of the pH value in the tank to control the pH value in the tank to be 7.0-8.0, when the pH value is not risen any more and is in a normal state, the reaction end point is a sequencing batch period reaction end point, the concentration of ammonia nitrogen in the reaction end point in each sequencing batch period tank is ensured to be 50-100mg/L, the concentration of nitrite nitrogen is 0-10mg/L, and after a period of operation, the total nitrogen removal load in the tank is not less than 0.3 kgN/(m) 3 D) or when the strain concentration is more than or equal to 1g/L, entering the next step;
s3, operation phase:
s3.1, nitroStarting the chemical tank (2): introducing inoculated nitrified sludge and wastewater into a nitrifying pond (2), and performing sequencing batch operation according to four steps of water inlet denitrification, aeration nitrosation, standing and water discharge, wherein the biochemical conditions of aeration nitrosation are as follows: the dissolved oxygen DO is 0.5 mg/L-1.0 mg/L, the water temperature is 30 ℃ to 35 ℃, the pH is maintained at 7.0-8.0, and c (NO) is contained in the nitrifying pond (2) 2 - ）/c（NH 4 + ) > 1.0, and c (NO 2 - ）/c（NO 3 - ) When the ratio of the nitrite nitrogen mass concentration to the ammonia nitrogen mass concentration in the effluent is more than 10, the characteristic of successful short-cut nitrification sludge domestication is adjusted to be 1.1-1.3;
s3.2, the denitrification tank (1) is connected with the nitrification tank (2) in series: the denitrification tank (1) and the nitrification tank (2) are connected in series, the denitrification tank (1) performs sequencing batch operation according to four steps of water inlet and chemical adding-stirring reaction-stopping stirring standing-supernatant discharging, the nitrification tank (2) performs sequencing batch operation according to four steps of water inlet denitrification-aeration nitrosation-standing-supernatant discharging, and in a single sequencing batch period, when the supernatant is discharged from the denitrification tank (1) until reaching a set low liquid level, the supernatant of the nitrification tank (2) is introduced into the denitrification tank (1) until reaching a set high liquid level of the denitrification tank (1), and then the nitrification tank (2) starts to feed wastewater; the method comprises the steps of gradually increasing the nitrogen load of a nitrifying tank (2) to a denitrifying tank (1) and gradually reducing the external dosing to provide the nitrogen load, wherein the total nitrogen amount of nitrite nitrogen and ammonia nitrogen provided by the nitrifying tank (2) is gradually increased according to the proportion of 10% -20%, and the total nitrogen amount provided by the external dosing is gradually decreased according to the proportion of 10% -20%, until the whole wastewater operation is realized.
2. The method for starting, culturing and operating anaerobic ammonium oxidation according to claim 1, wherein in step S1, the determination mark for the occurrence of the anaerobic ammonium oxidation activity is: in a sequencing batch period, the ammonia nitrogen concentration and the nitrite nitrogen concentration synchronously drop, and the removal amount m (nitrite nitrogen) of the nitrite nitrogen and the removal amount m (ammonia nitrogen) of the ammonia nitrogen are 1.2-1.4.
3. The method according to claim 1A method for starting, culturing and operating anaerobic ammoxidation, which is characterized in that in the step S1, the medicaments comprise medicaments containing nitrogen elements, inorganic carbon and medicaments containing nutrient elements; the nitrogen-containing agent comprises nitrite and ammonium salt, wherein the nitrite comprises sodium nitrite and/or potassium nitrite, and the ammonium salt comprises ammonium chloride and/or ammonium sulfate; the inorganic carbon is sodium bicarbonate, and the medicament containing nutrient elements comprises CaCl 2 ·2H 2 O、FeSO 4 、MgSO 4 ·7H 2 O、KH 2 PO 4 、EDTA、KHCO 3 、MnCl 2 ·4H 2 O、ZnSO 4 ·7H 2 O、NiCl 2 ·6H 2 O、CuSO 4 ·5H 2 O and NaMoO 4 ·2H 2 O, and the agent added in the steps S2 and S3 is the same as the agent added in the step S1.
4. The method for starting, culturing and operating anaerobic ammonia oxidation according to claim 1, wherein in the step S1, the water temperature in the tank is controlled at 33-35 ℃, the ammonia nitrogen concentration in the tank is maintained at 50-80mg/L, the nitrite nitrogen concentration is maintained at 30-50mg/L, the total alkalinity is 300-500mg/L, and the pH value is controlled at 7.5-8.0;
and/or in the step S2, controlling the pH value in the tank to be 7.5-8.0, and controlling the total alkalinity in the tank to be 500-1000mg/L based on calcium carbonate.
5. The method for starting, culturing and operating anaerobic ammonia oxidation according to any one of claims 1 to 4, wherein in step S1 and step S2, the water temperature in the denitrification tank (1) is controlled by adding RO purified water, wastewater discharged from a sewage plant or tap water, the time for stopping stirring and standing is 10min to 60min, and the pH value is controlled by adding hydrochloric acid or sulfuric acid; and/or in the steps S1, S2 and S3, strain interception and strain recycling are carried out on the supernatant discharged from the denitrification tank (1).
6. The method for starting, culturing and operating anaerobic ammonia oxidation according to any one of claims 1 to 4, characterized in that in step S3.1, the water temperature of the nitrification tank (2) is regulated by a cooling device, and the pH value in the tank is maintained by adding alkali; and/or, in step S3.2, the increasing period is 7 days to 30 days, and the decreasing period is 7 days to 30 days.
7. A system for anaerobic ammoxidation start-up, cultivation and operation, implemented using the method for anaerobic ammoxidation start-up, cultivation and operation as claimed in any one of claims 1 to 6, comprising a denitrification tank (1), a nitrification tank (2) and an anaerobic ammoxidation test apparatus (3), wherein the anaerobic ammoxidation test apparatus (3) is in communication with the denitrification tank (1), and the nitrification tank (2) is in communication with the denitrification tank (1).
8. The anaerobic ammonia oxidation starting, culturing and running system according to claim 7, wherein the anaerobic ammonia oxidation test device (3) is communicated with the denitrification tank (1) through a first water inlet pump (7), the nitrification tank (2) is communicated with the denitrification tank (1) through a second water inlet pump (8), the nitrification tank (2) is connected with a third water inlet pump (9), and the denitrification tank (1) is connected with a water outlet pump (10).
9. The anaerobic ammonia oxidation starting, culturing and operating system according to claim 7 or 8, wherein the denitrification tank (1) is provided with a stirrer (4), a first pH meter (12), a first temperature meter (13) and a first liquid level meter (14), the denitrification tank (1) is communicated with an acid adding device (16), and the denitrification tank (1) is communicated with a interception barrel (11) through a water outlet pump (10);
and/or be equipped with aeration equipment (5) in nitrifying pond (2), nitrify pond (2) still be equipped with second pH appearance (18), second thermometer (19) and second liquid level meter (20), nitrify pond (2) and an alkali throw-in device (17) intercommunication, be equipped with cooling tower (6) between nitrify pond (2) and third intake pump (9).
10. The anaerobic ammonia oxidation starting, culturing and running system according to claim 9, further comprising a PLC controller (15), wherein the first pH meter (12), the first thermometer (13), the first liquid level meter (14), the second pH meter (18), the second thermometer (19) and the second liquid level meter (20) are respectively connected with an input end of the PLC controller (15), and an output end of the PLC controller (15) is respectively connected with the acid adding device (16), the nitrification tank (2), the second water inlet pump (8), the water outlet pump (10), the alkali adding device (17), the cooling tower (6) and the third water inlet pump (9).
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