CN111186904B - Method for enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria and application - Google Patents
Method for enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria and application Download PDFInfo
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- C02F3/00—Biological treatment of water, waste water, or sewage
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Abstract
The invention discloses a method for enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria, which comprises the following steps in sequence: step S1, providing a device for bearing activated sludge, adding the activated sludge into the device, and contacting the activated sludge with simulated wastewater containing ammonia nitrogen under a first treatment condition to obtain second activated sludge; step S2, contacting the second activated sludge with simulated wastewater containing ammonia nitrogen under a second treatment condition to obtain second activated sludge; step S3, contacting the third activated sludge with the simulated wastewater containing ammonia nitrogen under a third treatment condition; wherein the dissolved oxygen in the first treatment condition is greater than the dissolved oxygen in the second treatment condition, and the dissolved oxygen in the third treatment condition is greater than the dissolved oxygen in the second treatment condition. The method provided by the invention realizes the accumulation of AOB and the elimination of NOB by controlling dissolved oxygen in stages, and can quickly realize a continuous flow nitrosation process.
Description
Technical Field
The invention belongs to the technical field of ammonia nitrogen treatment, and relates to a method for enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria and application thereof.
Background
Nitrogen pollution is one of the important factors causing water eutrophication, and has attracted extensive attention of people. Ammonia nitrogen removal in traditional wastewater treatment is generally realized through nitrification and denitrification processes, ammonia oxidizing bacteria oxidize ammonia nitrogen into nitrite in a nitrification stage, and nitrite oxidizing bacteria oxidize nitrite into nitrate; the heterotrophic denitrifying bacteria convert nitrified product nitrate into nitrogen gas in the denitrification stage, so that the denitrification treatment of the wastewater is realized. The conversion of ammonia nitrogen into nitrate nitrogen is realized by aeration, a large amount of electric energy is consumed, a sufficient carbon source is required in the denitrification process, carbon sources (organic matters) in urban sewage and certain special sewage are often insufficient, an additional carbon source is required, the operation cost is increased, and secondary pollution is possibly caused. The short-cut nitrification and denitrification process controls the ammonia nitrogen oxidation in the nitrosation stage, and can reduce the consumption of power and carbon source. In the anaerobic ammonia oxidation process, the anaerobic ammonia oxidation bacteria uses CO2As a carbon source, with NO2 -Is an electron acceptor, NH4 +Is an electron donor to generate nitrogen (byproduct of trace nitrate nitrogen) to realize the denitrification of the wastewater. Greatly shortens the process of oxidizing and reducing ammonia nitrogen to nitrogen, thereby saving a large amount of energy and materials and saving the operation cost. However, actual wastewater does not contain nitrite nitrogen, so the realization and operation of the anaerobic ammonia oxidation process need to be established on the basis of stable nitrosation of ammonia nitrogen in wastewater. However, in actual environment, Ammonia Oxidizing Bacteria (AOB) and Nitrite Oxidizing Bacteria (NOB) often coexist, and it is necessary to inhibit NOB and make AOB grow dominantly by optimizing operation parameters to realize stable nitrosation of ammonia nitrogen, however, the control conditions for inhibiting NOB and making AOB grow dominantly are complex and difficult to control.
Disclosure of Invention
The invention provides a method for enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria, which realizes the purposes of enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria by improving the culture conditions of bacteria and optimizing in stages.
According to a first aspect of the present invention, there is provided a method for enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria, comprising the following steps performed in sequence:
step S1, providing a device for bearing activated sludge, adding the activated sludge into the device, and contacting the activated sludge with simulated wastewater containing ammonia nitrogen under a first treatment condition to obtain second activated sludge;
step S2, contacting the second activated sludge with simulated wastewater containing ammonia nitrogen under a second treatment condition to obtain third activated sludge;
step S3, contacting the third activated sludge with simulated wastewater containing ammonia nitrogen under a third treatment condition;
wherein the dissolved oxygen in the first treatment condition is greater than the dissolved oxygen in the second treatment condition, and the dissolved oxygen in the third treatment condition is greater than the dissolved oxygen in the second treatment condition.
According to a preferred embodiment of the present invention, the simulated wastewater containing ammonia nitrogen has the same composition in steps S1 to S3.
According to a preferred embodiment of the present invention, the dissolved oxygen in the third treatment condition is less than the dissolved oxygen in the first treatment condition.
According to a preferred embodiment of the present invention, the dissolved oxygen in the second treatment conditions is not greater than 0.1mg/L, for example, may be not greater than 0.08mg/L, not greater than 0.06mg/L, not greater than 0.05mg/L, not greater than 0.04mg/L, not greater than 0.03mg/L, not greater than 0.02mg/L, not greater than 0.01mg/L and any value therebetween.
According to a preferred embodiment of the present invention, the dissolved oxygen in the first treatment conditions is 1.0-1.5mg/L, and may be, for example, 1.0mg/L, 1.1mg/L, 1.2mg/L, 1.3mg/L, 1.4mg/L, 1.5mg/L, and any value therebetween.
According to a preferred embodiment of the present invention, the dissolved oxygen in the third treatment conditions is 0.3-0.8mg/L, and may be, for example, 0.3mg/L, 0.4mg/L, 0.5mg/L, 0.6mg/L, 0.7mg/L, 0.8mg/L and any value therebetween.
According to a preferred embodiment of the present invention, the activated sludge carrying device is a device comprising a main reaction device and an aeration device with a structure similar to that of the UASB reaction device,
according to a preferred embodiment of the present invention, in the first to third treatment conditions, the temperature is from 31 ℃ to 35 ℃, and/or the pH is from 7.8 to 8.2, and/or the reflux ratio is from 3 to 5.
According to a preferred embodiment of the present invention, the temperature, and/or, the pH, and/or, the reflux ratio in the first, second and third treatment conditions are the same.
According to a preferred embodiment of the present invention, in step S1, the activated sludge and the simulated wastewater containing ammonia nitrogen are contacted under the first treatment condition until the nitrification rate is more than 5%, preferably less than 10%, more preferably less than 9%, less than 8%, less than 7%, less than 6%, less than 5.8%, and the nitrification rate is too high to be beneficial to the subsequent operation. In step S1, at the beginning of the contact between the activated sludge and the simulated wastewater containing ammonia nitrogen, the total nitrogen in the treated wastewater is usually higher than the initial total nitrogen concentration in the simulated wastewater, and does not show nitrification capability or has a low nitrification rate, and when the nitrification rate generally has an upward trend, the total nitrogen concentration in the treated wastewater is no longer higher than the initial total nitrogen concentration in the simulated wastewater.
According to a preferred embodiment of the present invention, in step S2, after the second activated sludge and the simulated wastewater containing ammonia nitrogen are contacted until the ammonia nitrogen concentration in the treated wastewater is less than 10% of the initial ammonia nitrogen concentration in the simulated wastewater, for example, after the ammonia nitrogen concentration in the treated wastewater is less than 8%, 7%, 5%, 4% of the initial ammonia nitrogen concentration in the simulated wastewater, the contacting is continued for 5-8 days under the second treatment condition, and then step S3 is performed.
Through step S2, Ammonia Oxidizing Bacteria (AOB) dominate the system, Nitrite Oxidizing Bacteria (NOB) are substantially eliminated, but dissolved oxygen under the second treatment conditions is not favorable for increasing the nitrosation capacity. Therefore, in step S3, the dissolved oxygen can be supplied to the dissolved oxygen range in the third treatment condition, and the hydraulic retention time can be properly adjusted to improve the nitrosation efficiency of the system.
According to a preferred embodiment of the present invention, in step S3, the third activated sludge and the simulated wastewater containing ammonia nitrogen are contacted under the third treatment condition until the concentrations of nitrite nitrogen and ammonia nitrogen in the treated simulated wastewater are stable.
According to a preferred embodiment of the present invention, the hydraulic retention time is performed in a gradually decreasing method in step S3.
According to the preferred embodiment of the invention, the ammonia nitrogen concentration in the simulated wastewater is 0.77-1.92 g/L. In the invention, the concentration of the ammonia nitrogen is NH3Or NH4 +And (4) counting by a medium N atom.
According to a preferred embodiment of the invention, the amount of activated sludge added is 2/5-3/5 of the volume of the activated sludge carrying device.
According to the preferred embodiment of the invention, the simulated wastewater containing ammonia nitrogen comprises or consists of the following components: NH (NH)4Cl：0.77-1.92g/L，NaHCO3 0.2-1.5g/L，KHCO3 0.5-1.5g/L，KH2PO4 5-20mg/L，CaCl2·2H2O 50-200mg/L，MgSO4·7H2O50-200 mg/L; preferably, the simulated wastewater containing ammonia nitrogen comprises or consists of the following components: NH (NH)4Cl：0.77-1.92g/L，NaHCO3 0.5g/L，KHCO3 0.75g/L，KH2PO410mg/L，CaCl2·2H2O 50mg/L，MgSO4·7H2O 80mg/L。
According to a preferred embodiment of the present invention, the simulated wastewater contains trace elements, and preferably, 1mL of trace element nutrient solution I and 1mL of trace element nutrient solution II are added to each liter of simulated wastewater, wherein the trace element nutrient solution I is a nutrient solution containing Fe, and the trace element nutrient solution II is a nutrient solution containing Mn, Zn, Co, Cu, Mo, Ni and Se.
According to a preferred embodiment of the present invention, the microelement nutrient solution I and the microelement nutrient solution II are composed of:
microelement nutrient solution I: EDTA 5000mg/L, FeSO4 5000mg/L；
And (3) trace element nutrient solution II: EDTA 5000mg/L, MnCl2·4H2O 990mg/L，ZnSO4·7H2O 430mg/L，CoCl2·6H2O 240mg/L，CuSO4·5H2O 250mg/L，NaMoO4·2H2O 220mg/L，NiCl2·6H2O 190mg/L，NaSeO4·10H2O 210mg/L，H3BO4 14mg/L。
According to a preferred embodiment of the invention, the activated sludge is subjected to a concentration and washing treatment before being fed to the plant, preferably washing with an inorganic salt solution, preferably 3-5 times, in order to remove as much as possible the inorganic impurities and the organic contaminants adsorbed on the surface of the activated sludge. The 'activated sludge' adopts aerobic or facultative activated sludge in a conventional sewage treatment system, and has no other special requirements.
According to a preferred embodiment of the present invention, the concentration and washing treatment is to leave the activated sludge at rest, discard the supernatant, and take the bottom concentrated sludge and wash it with an inorganic salt solution.
According to a preferred embodiment of the invention, the inorganic salt comprises NH4Cl：0.77～1.92g/L，NaCl：1000～1500mg/L，KH2PO4:10mg/L，CaCl25.6mg/L and MgSO4:300mg/L。。
The activated sludge bearing device used in the invention comprises a main reaction device and an aeration device which have similar structures with a UASB (upflow anaerobic sludge blanket) reaction device, and the aeration device is arranged at the bottom of the main reaction device. The aeration device comprises an air compressor, an air flow regulating system and an aeration head. The main reaction device comprises a main reactor, and a jacket layer is arranged outside the main reactor; the main reactor is connected with a water inlet pipe, a water discharge pipe and a return pipeline: the jacket layer is connected with the temperature control system and the hot water pump; the simulated wastewater (inlet water) enters the water distribution device of the main reactor through the water inlet pump, the water inlet pipe is also connected with an acid adjusting system and an alkali adjusting system so as to adjust the pH value of the reactor within a set range by adding acid or alkali, the main reactor is provided with a pH, temperature and dissolved oxygen probe interface, and the pH, temperature and dissolved oxygen in the reactor are observed in real time through the probe.
In a preferred embodiment of the present invention, the hydraulic retention time in the third treatment conditions is less than the hydraulic retention time in the second treatment conditions.
According to another aspect of the invention, there is provided the use of the method in the start-up of a nitrosation process.
The method provided by the invention realizes the accumulation of AOB and the elimination of NOB by controlling dissolved oxygen in stages, optimizes the whole process in stages, has simple regulation and control mode and obvious effect, can particularly realize a continuous flow nitrosation process more quickly, and is simpler and easier to control than the operation of an SBR process.
Drawings
FIG. 1 is a schematic structural diagram of an apparatus for carrying activated sludge according to the present invention;
the system comprises a 1-three-phase separator gas outlet, a 2-water outlet, a 3-jacket layer, a 4-pH, temperature and dissolved oxygen probe interface, a 5-sampling port, a 6-acid adjusting pump, a 7-alkali adjusting pump, an 8-water inlet pump, a 9-hot water pump, a 10-reflux pump, a 11-temperature control system, a 12-acid storage tank, a 13-alkali storage tank, a 14-aeration device and a 15-main reactor.
Detailed Description
The present invention will be described in detail with reference to examples, but the present invention is not limited to the examples.
Example 1
The method comprises the following steps:
taking sludge at the bottom of a settling tank in a certain domestic sewage treatment plant, standing and concentrating, removing supernatant, taking bottom concentrated sludge, and using a prepared inorganic salt solution (NH)4Cl：1.90g/L，NaCl：1200mg/L，KH2PO4：10mg/L，CaCl2：5.6mg/L，MgSO4: 300mg/L) for 4 times, and standing for 1.5 hours after each time of elutriation to remove supernatant, so as to remove inorganic impurities and organic pollutants adsorbed on the surface of the sludge as far as possible. And (3) loading the elutriated and concentrated sludge into a UASB reactor, wherein the amount of the sludge accounts for 2/5-3/5 of the effective volume of the reactor.
Step two:
preparing a trace element nutrient solution I and a trace element nutrient solution II:
and (3) a trace element nutrient solution I: EDTA 5000mg/L, FeSO4 5000mg/L；
And (3) trace element nutrient solution II: EDTA 5000mg/L, MnCl2·4H2O 990mg/L，ZnSO4·7H2O 430mg/L，
CoCl2·6H2O 240mg/L，CuSO4·5H2O 250mg/L，NaMoO4·2H2O 220mg/L，NiCl2·6H2O 190mg/L，NaSeO4·10H2O 210mg/L，H3BO4 14mg/L。
Preparing simulated wastewater: NH (NH)4Cl：1.9g/L，NaHCO3 0.5g/L，KHCO3 0.75g/L，KH2PO4 10mg/L，CaCl2·2H2O 50mg/L，MgSO4·7H2O80 mg/L, and 1mL each of the microelement nutrient solutions I and II is added into each liter of water.
The simulated wastewater is sent into the reactor through a water distribution device by a peristaltic pump, the bottom of the three-phase separator is provided with sewage sludge reflux, and the effluent of the system is discharged from an upper outlet of the three-phase separator. The pump flow was adjusted to allow the hydraulic retention time to be 8 hours, the reflux ratio was 3, the internal temperature of the system was controlled at 33 ℃, the pH was controlled at 8.2, and the Dissolved Oxygen (DO) was controlled at about 1.0 mg/L. Sampling and monitoring indexes such as ammonia nitrogen, nitrite nitrogen, nitrate nitrogen and the like of inlet and outlet water of the system every 8 hours, wherein the total nitrogen of outlet water of the system at the initial stage is generally higher than that of inlet water, the outlet water basically does not contain nitrate nitrogen, the nitrate nitrogen is detected in the outlet water after the system operates for one day, the nitrite nitrogen content in the outlet water of the system reaches 185mg/L after the system operates for 40 hours, the nitrate nitrogen content in the outlet water of the system reaches 28mg/L, and the dissolved oxygen of the system is reduced, and then the step III is carried out.
Step three:
the dissolved oxygen of the system is adjusted to be lower than 0.1mg/L, and other parameters are kept unchanged. Sampling and monitoring indexes such as ammonia nitrogen, nitrite nitrogen, nitrate nitrogen and the like of inlet and outlet water of the system every day, wherein the nitrate nitrogen content in outlet water of the system begins to decrease, but the nitrite nitrogen content also decreases to a certain extent in the first two days, the nitrite nitrogen content in the outlet water is 106mg/L at the lowest time, the nitrate nitrogen in the outlet water is lower than the detection limit after the third day, the nitrite nitrogen content begins to increase, when the third step runs to the thirteenth day, the ammonia nitrogen in the outlet water of the system is lower than 20mg/L, and the system is continuously run for 5-6 days. And (5) turning to the step four.
Step four:
the dissolved oxygen is increased to 0.8mg/L, the retention time is shortened to 7 hours, and other parameters are kept unchanged. Taking water samples of inlet water and outlet water after one day for monitoring, wherein the ammonia nitrogen of the outlet water is not obviously increased, and the nitrite nitrogen and the nitrate nitrogen are not obviously changed, which shows that the retention time is possibly reduced, the retention time is continuously reduced to 6 hours, the ammonia nitrogen of the outlet water is increased to be higher than 25mg/L after one day, but the outlet water is recovered to be in a high nitrite nitrogen and low ammonia nitrogen state after two days of continuous operation. And then the system stably operates.
Example 2:
the method comprises the following steps:
taking sludge at the bottom of a settling tank in a certain domestic sewage treatment plant, standing and concentrating, removing supernatant, taking bottom concentrated sludge, and using a prepared inorganic salt solution (NH)4Cl：0.77g/L，NaCl：1000～1500mg/L，KH2PO4：10mg/L，CaCl2：5.6mg/L，MgSO4: 300mg/L) for 4 times, and standing for 1.5 hours after each time of elutriation to remove supernatant, so as to remove inorganic impurities and organic pollutants adsorbed on the surface of the sludge as far as possible. And (3) loading the elutriated and concentrated sludge into a UASB reactor, wherein the amount of the sludge accounts for 2/5-3/5 of the effective volume of the reactor.
Step two:
preparing a trace element nutrient solution I and a trace element nutrient solution II:
and (3) a trace element nutrient solution I: EDTA 5000mg/L, FeSO4 5000mg/L；
And (3) trace element nutrient solution II: EDTA 5000mg/L, MnCl2·4H2O 990mg/L，ZnSO4·7H2O 430mg/L，
CoCl2·6H2O 240mg/L，CuSO4·5H2O 250mg/L，NaMoO4·2H2O 220mg/L，NiCl2·6H2O 190mg/L，NaSeO4·10H2O 210mg/L，H3BO4 14mg/L。
Preparing simulated wastewater: NH (NH)4Cl：0.77g/L，NaHCO3 0.5g/L，KHCO3 0.75g/L，KH2PO4 10mg/L，CaCl2·2H2O 50mg/L，MgSO4·7H2O80 mg/L, and water per liter plus trace elements1mL of each nutrient solution I and II.
The simulated wastewater is sent into the reactor through a water distribution device by a peristaltic pump, the bottom of the three-phase separator is provided with sewage sludge reflux, and the effluent of the system is discharged from an upper outlet of the three-phase separator. The pump flow was adjusted to allow the hydraulic retention time to be 4 hours, the reflux ratio to be 3, the internal temperature of the system to be 33 ℃, the pH to be 8.2, and the Dissolved Oxygen (DO) to be 1.0 mg/L. Sampling and monitoring indexes such as ammonia nitrogen, nitrite nitrogen, nitrate nitrogen and the like of inlet and outlet water of the system every 8 hours, wherein the total nitrogen of outlet water of the system at the initial stage is generally higher than that of inlet water, the outlet water basically does not contain nitrate nitrogen, the nitrate nitrogen is detected in the outlet water after the system operates for one day, the nitrite nitrogen content of the outlet water of the system reaches 75mg/L after the system operates for 40 hours, the nitrate nitrogen content reaches 18mg/L, and the dissolved oxygen of the system is reduced, and then the step III is carried out.
Step three:
the Dissolved Oxygen (DO) of the system is adjusted to be nearly zero, the actual control can be lower than 0.1mg/L as the standard, and the retention time is adjusted to be 6 hours. Sampling and monitoring indexes such as ammonia nitrogen, nitrite nitrogen, nitrate nitrogen and the like of inlet and outlet water of the system every day, wherein the nitrate nitrogen content in outlet water of the system begins to decrease, but the nitrite nitrogen content also decreases to a certain extent in the first two days, the nitrite nitrogen content in the outlet water is 56mg/L at the lowest time, the nitrate nitrogen in the outlet water is lower than the detection limit after the third day, the nitrite nitrogen content begins to increase, when the third step is operated to the tenth day, the ammonia nitrogen in the outlet water of the system is lower than 10mg/L, and the system is continuously operated for 5-6 days. And (5) turning to the step four. .
Step four:
the dissolved oxygen is increased to 0.3mg/L, the retention time is shortened to 5.5 hours, and other parameters are kept unchanged. Taking water samples of inlet water and outlet water after one day for monitoring, wherein the ammonia nitrogen of the outlet water is not obviously increased, and the nitrite nitrogen and the nitrate nitrogen are not obviously changed, which shows that the retention time is possibly reduced, the retention time is continuously reduced to 5 hours, the ammonia nitrogen of the outlet water is increased to be higher than 15mg/L after one day, but the outlet water is recovered to be in a high nitrite nitrogen and low ammonia nitrogen state after continuously running for one day. The final system was run stably with dissolved oxygen of 0.3mg/L and a residence time of 4.5 hours.
Comparative example 1:
the method comprises the following steps:
taking sludge at the bottom of a settling tank in a certain domestic sewage treatment plant, standing and concentrating, removing supernatant, taking bottom concentrated sludge, and using a prepared inorganic salt solution (NH)4Cl：0.77g/L，NaCl：1000～1500mg/L，KH2PO4：10mg/L，CaCl2：5.6mg/L，MgSO4: 300mg/L) for 4 times, and standing for 1.5 hours after each time of elutriation to remove supernatant, so as to remove inorganic impurities and organic pollutants adsorbed on the surface of the sludge as far as possible. And (3) loading the elutriated and concentrated sludge into a UASB reactor, wherein the amount of the sludge accounts for 2/5-3/5 of the effective volume of the reactor.
Step two:
preparing a trace element nutrient solution I and a trace element nutrient solution II:
and (3) a trace element nutrient solution I: EDTA 5000mg/L, FeSO4 5000mg/L；
And (3) trace element nutrient solution II: EDTA 5000mg/L, MnCl2·4H2O 990mg/L，ZnSO4·7H2O 430mg/L，CoCl2·6H2O 240mg/L，CuSO4·5H2O 250mg/L，NaMoO4·2H2O 220mg/L，NiCl2·6H2O 190mg/L，NaSeO4·10H2O 210mg/L，H3BO4 14mg/L。
Preparing simulated wastewater: NH (NH)4Cl：0.77g/L，NaHCO3 0.5g/L，KHCO3 0.75g/L，KH2PO4 10mg/L，CaCl2·2H2O 50mg/L，MgSO4·7H2O80 mg/L, and 1mL each of the trace element nutrient solution I and the trace element nutrient solution II is added into each liter of simulated wastewater.
The simulated wastewater is sent into the reactor through a water distribution device by a peristaltic pump, the bottom of the three-phase separator is provided with sewage sludge reflux, and the effluent of the system is discharged from an upper outlet of the three-phase separator. The pump flow was adjusted to maintain the hydraulic retention time at 4 hours, the reflux ratio was 3, the internal temperature of the system was controlled at 33 ℃, the pH was controlled at about 8.2, and the Dissolved Oxygen (DO) was controlled at about 0.3 mg/L. The system is sampled and monitored every day for the indexes of ammonia nitrogen, nitrite nitrogen, nitrate nitrogen and the like in the inlet and outlet water, the total nitrogen of the outlet water of the system at the initial stage is generally higher than the total nitrogen of the inlet water, the outlet water basically does not contain nitrate nitrogen, and the total nitrogen of the outlet water starts to be equal to the inlet water after the system runs for three days. And (4) continuously operating the system according to the conditions, and after the system is operated for the tenth day, the nitrite nitrogen in the effluent of the system reaches about 140mg/L, namely about 70% of ammonia nitrogen in the inlet water of the system is nitrosated, and the AOB in the system occupies an absolute dominant position. Continuously operating the test device, wherein nitrite nitrogen in the effluent of the device cannot be continuously improved, the concentration of nitrate nitrogen in the effluent begins to gradually increase, and when the 15 th day, the ammonia nitrogen in the effluent of the system is 40mg/L, the nitrite nitrogen is reduced to about 100mg/L, and the concentration of nitrate nitrogen reaches about 56 mg/L; and (3) continuously operating the test device for 5 days, wherein the nitrite nitrogen content in the effluent water of the system still has a descending trend, the nitrate nitrogen content has a slow ascending trend, and the ammonia nitrogen also has a slow ascending trend.
It should be noted that the above-mentioned embodiments are only for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described with reference to exemplary embodiments, but the words which have been used herein are words of description and illustration, rather than words of limitation. The invention can be modified, as prescribed, within the scope of the claims and without departing from the scope and spirit of the invention. Although the invention has been described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, but rather extends to all other methods and applications having the same functionality.
Claims (6)
1. A method for enriching ammonia oxidizing bacteria and inhibiting nitrite oxidizing bacteria comprises the following steps in sequence:
step S1, providing a device for bearing activated sludge, adding the activated sludge into the device, and contacting the activated sludge with simulated wastewater containing ammonia nitrogen under a first treatment condition to obtain second activated sludge; wherein, the activated sludge is contacted with simulated wastewater containing ammonia nitrogen under a first treatment condition until the nitrification rate of the simulated wastewater is more than 5 percent and less than 10 percent;
step S2, contacting the second activated sludge with simulated wastewater containing ammonia nitrogen under a second treatment condition to obtain third activated sludge;
step S3, contacting the third activated sludge with the simulated wastewater containing ammonia nitrogen under a third treatment condition; wherein the dissolved oxygen in the third treatment condition is 0.3-0.8 mg/L;
wherein the dissolved oxygen in the first treatment condition is greater than the dissolved oxygen in the second treatment condition, the dissolved oxygen in the third treatment condition is less than the dissolved oxygen in the first treatment condition,
in step S2, the second activated sludge and the simulated wastewater containing ammonia nitrogen are contacted until the ammonia nitrogen concentration in the treated simulated wastewater is lower than 10% of the initial ammonia nitrogen concentration in the simulated wastewater, and then the second activated sludge and the simulated wastewater are continuously contacted for 5-8 days under the second treatment condition, and then step S3 is carried out.
2. The method of claim 1, wherein the dissolved oxygen in the second treatment condition is no greater than 0.1 mg/L.
3. The method of claim 1 or 2, wherein the dissolved oxygen in the first treatment conditions is 1.0-1.5 mg/L.
4. The method according to claim 1 or 2, wherein in step S3, the third activated sludge is contacted with the simulated wastewater containing ammonia nitrogen under third treatment conditions until the concentrations of nitrite nitrogen and ammonia nitrogen in the treated simulated wastewater are stabilized.
5. The process according to claim 1 or 2, wherein in the first to third treatment conditions, the temperature is from 31 ℃ to 35 ℃, and/or the pH is from 7.8 to 8.2, and/or the reflux ratio is from 3 to 5.
6. Use of the method according to any one of claims 1-5 in the start-up of a nitrosation process.
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