Method for starting semi-tank inoculation of anaerobic ammonia oxidation process

Abstract

The invention relates to the field of water treatment, and particularly discloses a method for starting semi-tank inoculation of an anaerobic ammonia oxidation process. The method comprises the following steps that anaerobic ammonium oxidation strains are inoculated into a biochemical pool, a water distribution agent is introduced into the biochemical pool, and the water distribution agent comprises ammonium chloride, sodium nitrite, sodium bicarbonate, magnesium sulfate, monopotassium phosphate, calcium chloride and ferrous sulfate; and when the nitrogen removal volume load in the biochemical pool reaches 0.25-0.35 kgN / m < 3 >. D, introducing wastewater to be treated into the biochemical pool. The anaerobic ammonium oxidation process half-tank inoculation starting method has the advantages that rapid proliferation of anaerobic ammonium oxidation bacteria is realized, and the starting time is short.

Description

Technical Field

[0001] The present application relates to the field of water treatment, and more specifically, to a method for starting up a half-cell inoculation of an anaerobic ammonium oxidation process. Background Art

[0002] High-ammonia-nitrogen wastewater refers to wastewater containing a large amount of ammonia-nitrogen compounds, which usually comes from industries such as chemical engineering, pharmaceuticals, and food processing. If high-ammonia-nitrogen wastewater is directly discharged without effective treatment, it will cause eutrophication of water bodies, leading to the rapid reproduction of algae and other plankton, causing a sharp drop in the dissolved oxygen content of the water body, and then resulting in the massive death of fish and other aquatic organisms, seriously disrupting the water ecological balance.

[0003] The traditional nitrification and denitrification process is a common method for treating high-ammonia-nitrogen wastewater. In this process, ammonia nitrogen is oxidized to nitrite and nitrate by nitrifying bacteria, and then reduced to nitrogen and removed from the water by denitrifying bacteria. However, this process has obvious defects. On the one hand, it requires a large floor area for treatment facilities, and with the increasingly scarce land resources, the cost increases significantly. On the other hand, a large amount of oxygen, alkalinity, and carbon source are consumed during the process operation, resulting in a substantial increase in the treatment cost.

[0004] The anaerobic ammonium oxidation process has great potential in the field of high-ammonia-nitrogen wastewater treatment due to its advantages such as high nitrogen removal load, low energy consumption, and low operating cost, and has been preliminarily applied on an engineering scale. However, the anaerobic ammonium oxidation bacteria relied on by the anaerobic ammonium oxidation process grow extremely slowly, with a doubling time of about 11 days. If started by inoculating activated sludge, it takes at least 6 months, with high start-up costs and a high risk of failure, which greatly limits its wide and efficient application. Summary of the Invention

[0005] In order to achieve the rapid proliferation of anaerobic ammonium oxidation bacteria to meet the water treatment volume requirements, the present application provides a method for starting up a half-cell inoculation of an anaerobic ammonium oxidation process.

[0006] The method for starting up a half-cell inoculation of an anaerobic ammonium oxidation process provided by the present application adopts the following technical scheme: A method for starting up a half-cell inoculation of an anaerobic ammonium oxidation process, comprising the following steps: Inoculate anaerobic ammonium oxidation bacteria into a biochemical pool, and introduce dosing agents into the biochemical pool. The components of the dosing agents include ammonium chloride, sodium nitrite, sodium bicarbonate, magnesium sulfate, potassium dihydrogen phosphate, calcium chloride, and ferrous sulfate; When the nitrogen removal volume load in the biochemical pool reaches 0.25 - 0.35 kgN / m 3 ·d, introduce the wastewater to be treated into the biochemical pool.

[0007] By adopting the above technical scheme, ammonium chloride and sodium nitrite in the water dispensing agent provide two key substrates, ammonia nitrogen and nitrite, for anaerobic ammonia-oxidizing bacteria, respectively. In the anaerobic ammonia oxidation reaction, bacteria use these two substrates to generate nitrogen through a series of complex enzymatic reactions to meet their metabolic energy needs, thereby effectively promoting the growth and reproduction of bacteria. Sodium bicarbonate not only provides the necessary carbon elements for bacterial cell synthesis as an inorganic carbon source, but also maintains a stable pH environment in the biochemical pool by virtue of its acid-base buffering properties, preventing the drastic pH fluctuations from damaging the physiological functions of bacteria. Ingredients such as magnesium sulfate, potassium dihydrogen phosphate, calcium chloride and ferrous sulfate provide a variety of trace elements such as magnesium, phosphorus, calcium, and iron, which participate in the composition of many enzymes in bacteria, ensuring that various physiological and biochemical reactions in the cells, such as respiration and material synthesis, can proceed normally. When the nitrogen removal volume load reaches a specific range, the wastewater to be treated is introduced, which can adapt the bacteria to the complex water quality components in the wastewater, and effectively reduce the risk of inactivation of the strains due to environmental mutations during the startup phase.

[0008] Optionally, after adding the water-adjusting agent to the biochemical pool, the temperature in the biochemical pool is controlled to be 34-36°C, and after adding the water-adjusting agent to the biochemical pool, the pH of the liquid in the biochemical pool is adjusted to 7.5-8.2, the alkalinity to 200-300 mg / L, the dissolved oxygen to <0.1 mg / L, and the conductivity to <15.00 ms / cm.

[0009] By adopting the above technical scheme, the temperature range of 34-36℃ is close to the optimal growth temperature of this type of bacteria. At this temperature, the activity of various enzymes involved in the anaerobic ammonium oxidation reaction in the bacteria, such as hydrazine synthase and nitrite reductase, can be maintained at a high level, accelerating the substrate conversion and energy generation rate, thereby ensuring the efficient metabolic reaction. The pH range of 7.5-8.2 can not only prevent the acidity or alkalinity from damaging the bacterial cells, but also provide a suitable acid-base environment for the enzymatic reaction. Maintaining the alkalinity at 200-300mg / L helps to stabilize the pH, because during the anaerobic ammonium oxidation process, the reaction will cause the pH of the system to change, and the appropriate alkalinity can act as a buffer to ensure that the pH fluctuation is within an acceptable range. Strictly controlling dissolved oxygen <0.1mg / L is because anaerobic ammonium oxidizing bacteria are strictly anaerobic bacteria, and an extremely low dissolved oxygen environment is a necessary condition for their survival and metabolism. Excessive dissolved oxygen will inhibit bacterial growth and even cause its death. Limiting the conductivity to <15.00ms / cm is mainly to avoid excessive salt concentration. Excessively high salt concentration may cause an imbalance in osmotic pressure inside and outside the cells, causing bacterial cells to lose water and affecting their normal physiological functions. Controlling the conductivity within this range can effectively prevent this from happening and create an environment that is conducive to the rapid growth and stable metabolism of anaerobic ammonia-oxidizing bacteria.

[0010] Optionally, the components of the water distribution agent include 0.8 - 1.2 g / L of sodium bicarbonate, 0.2 - 0.4 g / L of magnesium sulfate, 0.025 - 0.03 g / L of potassium dihydrogen phosphate, 0.005 - 0.006 g / L of calcium chloride, and 0.007 - 0.008 g / L of ferrous sulfate.

[0011] By adopting the above technical solution, the concentration of 0.8 - 1.2 g / L of sodium bicarbonate can not only ensure sufficient carbon source supply, enabling bacteria to have enough raw materials for cell substance synthesis, but also maintain effective acid-base buffering capacity and stabilize the pH environment in the biochemical pool. For magnesium sulfate, a content of 0.2 - 0.4 g / L ensures that bacteria obtain sufficient magnesium elements. Magnesium ions participate in the activation process of various enzymes, such as participating in the activation of ATPase and affecting intracellular energy metabolism. The phosphorus element provided by potassium dihydrogen phosphate is an essential element for bacteria to synthesize important biological macromolecules such as nucleic acids and phospholipids. A concentration of 0.025 - 0.03 g / L just meets this requirement. The calcium ions provided by calcium chloride play a role in maintaining the stability of cell structure and regulating cell physiological functions, and avoid adverse effects on bacteria caused by abnormal calcium ion concentration within the concentration range of 0.005 - 0.006 g / L. The iron element in ferrous sulfate is a key component of electron transfer proteins such as cytochromes. A concentration of 0.007 - 0.008 g / L ensures the normal operation of the electron transfer chain, thus ensuring the smooth progress of the energy conversion process of the anaerobic ammonium oxidation reaction. These nutrient components act synergistically within their respective appropriate concentration ranges, not only meeting the growth requirements of bacteria, but also avoiding problems such as growth inhibition and metabolic disorders caused by too high or too low concentrations, ensuring the continuous and stable growth and metabolism of bacteria.

[0012] Optionally, when the nitrogen removal volume load in the biochemical pool reaches 0.3 kgN / m 3 ·d, the added volume of the water distribution agent is reduced by 10% every 72 h, and the reduced amount of the water distribution agent is replaced by an equal volume of the wastewater to be treated and introduced into the biochemical pool until the volume of the wastewater to be treated in the biochemical pool is 100%.

[0013] By adopting the above technical solution, this progressive wastewater replacement strategy avoids the impact on anaerobic ammonium-oxidizing bacteria caused by directly introducing a large amount of wastewater to be treated into the biochemical reactor. The components in the actual wastewater are complex and may contain inhibitory substances such as heavy metals and toxic organic compounds. If a large amount is introduced at once, it is extremely likely to cause a decrease in the activity of the bacterial strain or even death. By reducing the volume of the dosing agent by 10% every 72 hours and replacing it with an equal volume of wastewater to be treated, the bacteria have enough time to adapt to various components in the wastewater. During this process, the bacteria will gradually adjust their own metabolic mechanisms to adapt to different substrate concentrations, nutrient composition ratios, and possible inhibitors in the wastewater. As the proportion of the wastewater to be treated gradually increases, the treatment capacity of the bacteria for the actual wastewater continues to increase, and the stability of the process also improves accordingly. From the perspective of the start-up success rate, this gentle adaptation process greatly reduces the risk of start-up failure caused by environmental mutations, provides a strong guarantee for the stable operation of the anaerobic ammonium-oxidation process, enables the process to reach the designed treatment capacity faster, and is put into practical application.

[0014] Optionally, the calculation method for the amount of ammonium chloride in the dosing agent is The is the mass of ammonium chloride added, the NLR is the nitrogen influent volumetric loading rate, the V is the volume of the biochemical reactor, and the Q is the influent flow rate.

[0015] By adopting the above technical solution, through this calculation method, whether the biochemical reactor is a small-scale experimental device or a large-scale engineering facility, and whether the influent flow rate is stable or has certain fluctuations, it can provide an always suitable and stable ammonia-nitrogen substrate concentration for anaerobic ammonium-oxidizing bacteria according to the actual operating conditions. A suitable ammonia-nitrogen concentration is one of the key factors to ensure the normal metabolism and growth of bacteria. A stable substrate supply can maintain the efficient operation of the treatment process, avoid substrate inhibition caused by too high ammonia-nitrogen concentration, or problems such as slow bacterial growth and insufficient treatment capacity due to too low concentration, ensure the continuous and stable progress of the anaerobic ammonium-oxidation reaction, and improve the reliability and treatment effect of the entire process.

[0016] Optionally, the amount of sodium nitrite in the dosing agent is The is the added mass of sodium nitrite, the NLR is the nitrogen influent volumetric loading rate, the V is the volume of the biochemical reactor, and the Q is the influent flow rate.

[0017] By adopting the above technical solution, the addition amount of sodium nitrite can be matched with the addition amount of ammonium chloride according to the actual process operation parameters. In each operation stage, the anaerobic ammonium oxidation bacteria can obtain a suitable proportion of nitrite substrates, thus ensuring the smooth progress of the anaerobic ammonium oxidation reaction according to the correct stoichiometric relationship. This not only helps to maintain the high efficiency of the reaction and improve the nitrogen removal efficiency, but also can avoid problems such as metabolic disorders and accumulation of intermediate products caused by the imbalance of substrate ratios, further enhancing the overall efficiency of the process, ensuring the stable and efficient operation of the entire anaerobic ammonium oxidation system, and achieving the effective treatment of high-ammonia-nitrogen wastewater.

[0018] Optionally, the carrier for inoculating the anaerobic ammonium oxidation bacteria is a porous ceramic. The pore size of the porous ceramic is 0.1 - 1 μm, the porosity of the porous ceramic is 60 - 70%, and the surface roughness of the porous ceramic is 2 - 4 μm.

[0019] By adopting the above technical solution, selecting a porous ceramic with specific parameters as the carrier has a significant promoting effect on the attachment and growth of anaerobic ammonium oxidation bacteria. The pore size range of 0.1 - 1 μm provides ideal attachment sites for bacteria. On the one hand, the pore size of this size enables the bacteria to fully contact the pore wall and achieve firm attachment through physical actions such as van der Waals forces and electrostatic attractions; on the other hand, the smaller pore size can prevent the bacteria from being easily washed away under the impact of water flow or other external forces. The high porosity makes the interior of the porous ceramic have a rich space, providing a vast place for the growth and reproduction of bacteria, and at the same time greatly increasing the diffusion channels of substrates (such as ammonia nitrogen, nitrite, etc.) and metabolites inside the carrier, facilitating mass exchange and ensuring that bacteria can obtain nutrients in a timely manner and excrete metabolites. The surface roughness of 2 - 4 μm plays an important role in the initial attachment of bacteria and the formation of biofilms. The rough surface increases the contact area between bacteria and the carrier, providing more tiny protrusions and depressions for bacteria to adsorb. The appropriate surface roughness helps the stable formation and development of biofilms, enabling the biofilms to adhere tightly to the surface of the porous ceramic and not easily fall off. Generally speaking, these characteristics significantly improve the attachment stability and growth efficiency of anaerobic ammonium oxidation bacteria on the carrier, accelerate the formation and maturation process of biofilms, thus effectively shortening the start-up time of the anaerobic ammonium oxidation process and improving the start-up efficiency of the process.

[0020] Optionally, the dosing agent further includes 5 - 20 mg / L of short-chain fatty acids.

[0021] By adopting the above technical solutions, short-chain fatty acids, as additional carbon sources and energy substances, contribute to the growth and metabolism of anaerobic ammonium-oxidizing bacteria. These short-chain fatty acids can easily penetrate the bacterial cell membrane and enter the cell interior to participate in the metabolic process. Inside the cell, they can be converted into intermediate products such as acetyl coenzyme A through a series of biochemical reactions, such as the β-oxidation pathway, and then enter the tricarboxylic acid cycle, providing the energy and material basis for the growth and reproduction of bacteria, and accelerating the synthesis of biological macromolecules such as proteins and nucleic acids in the cell. At the same time, short-chain fatty acids may regulate the metabolic pathways of bacteria. Adding 5-20 mg / L of short-chain fatty acids to the dosing agent provides additional nutritional support for anaerobic ammonium-oxidizing bacteria without introducing too many complex components, effectively shortening the start-up time of the process, enabling the anaerobic ammonium-oxidation process to reach a stable operation state faster, and improving the treatment efficiency and economic benefits of the entire process.

[0022] In summary, the present application has the following beneficial effects: 1. Since the present application uses ammonium chloride and sodium nitrite in the dosing agent to provide key substrates for anaerobic ammonium-oxidizing bacteria, meeting their metabolic energy requirements and strongly promoting the growth and reproduction of bacteria. Sodium bicarbonate maintains the carbon source supply and pH stability, and components such as magnesium sulfate provide various trace elements to ensure the normal progress of physiological and biochemical reactions. After the nitrogen removal volume load meets the standard, the wastewater to be treated is introduced, enabling the bacteria to adapt to complex water quality. Overall, it promotes the growth rate of anaerobic ammonium-oxidizing bacteria to accelerate, effectively shortening the start-up cycle of the biochemical pool and reducing the risk of inactivation of the bacterial species due to environmental mutations during the start-up stage.

[0023] 2. The present application preferably adopts a progressive wastewater replacement strategy, which can effectively avoid the impact on anaerobic ammonium-oxidizing bacteria caused by directly introducing a large amount of actual wastewater with complex components, which may contain inhibitors such as heavy metals and toxic organic substances, resulting in a decrease or even death of the bacterial species activity. This method gives the bacteria sufficient time to adapt to various components in the wastewater, prompting them to gradually adjust their metabolic mechanisms to match different substrate concentrations, nutrient component ratios, and inhibitors, thereby continuously enhancing the bacteria's treatment ability for actual wastewater, significantly improving the process stability, greatly reducing the risk of start-up failure caused by environmental mutations, strongly ensuring the stable operation of the anaerobic ammonium-oxidation process, and accelerating its reaching the designed treatment capacity and being put into practical application.

[0024] 3. The method of the present application significantly promotes the attachment and growth of bacteria in multiple aspects by using a porous ceramic with a pore size of 0.1 - 1 μm, a porosity of 60 - 70%, and a surface roughness of 2 - 4 μm as the carrier for anaerobic ammonium oxidation bacteria. The appropriate pore size allows the bacteria to firmly attach and prevents their loss. The high porosity provides a vast growth space and accelerates mass exchange. The suitable surface roughness increases the contact area between the bacteria and the carrier, facilitating the initial attachment and the stable formation of the biofilm. Ultimately, the attachment stability and growth efficiency of anaerobic ammonium oxidation bacteria on the carrier are greatly improved, the formation and maturation of the biofilm are accelerated, the start-up time of the anaerobic ammonium oxidation process is effectively shortened, and the start-up efficiency is enhanced. Detailed Embodiments

[0025] The following further elaborates on the present application in conjunction with embodiments. It should be specifically noted that: for those conditions not specified in the following embodiments, they are carried out according to conventional conditions or the conditions recommended by the manufacturer. Unless otherwise specified, the raw materials used in the following embodiments can all be obtained from ordinary commercial sources. Embodiment

[0026] Embodiment 1 A method for starting the inoculation of a semi-tank of an anaerobic ammonium oxidation process: A 400 m 3 biochemical tank is used. Anaerobic ammonium oxidation bacteria are inoculated in the biochemical tank. The initial nitrogen removal volumetric load of the inoculated anaerobic ammonium oxidation bacteria is 0.1 kgN / m 3 ·d. The carrier for the inoculated anaerobic ammonium oxidation bacteria is a porous ceramic. The pore size of the porous ceramic is 0.5 μm, the porosity is 65%, and the roughness is 3 μm. Water distribution agents are introduced into the biochemical tank and the biochemical tank is operated. The components of the water distribution agents include ammonium chloride, sodium nitrite, 1 g / L sodium bicarbonate, 0.3 g / L magnesium sulfate, 0.028 g / L potassium dihydrogen phosphate, 0.0055 g / L calcium chloride, 0.0075 g / L ferrous sulfate, and 15 mg / L butyric acid. The calculation method for the dosage of ammonium chloride is The dosage of sodium nitrite is where is the mass of ammonium chloride added, is the added mass of sodium nitrite, NLR is the nitrogen influent volumetric load, V is the volume of the biochemical tank, Q is the influent flow rate, and the where cTN is the sum of the ammonia nitrogen and nitrite nitrogen concentrations in the influent water. In this embodiment, cTN is 1500 mg / L; The operating temperature of the biochemical tank is controlled at 35 °C, the pH is maintained between 7.5 - 8.2, the alkalinity is between 200 - 300 mg / L, the dissolved oxygen < 0.1 mg / L, and the conductivity < 15.00 ms / cm. During the operation of the biochemical tank, the amount of anaerobic ammonium oxidation bacteria gradually increases, and the nitrogen removal volumetric load gradually increases.

[0027] When the nitrogen removal volume load in the biochemical pool reaches 0.3 kgN / m 3 ·d, the added volume of the dosing agent is reduced by 10% every 72 h, and the reduced amount of the dosing agent is replaced by the same volume of the wastewater to be treated and introduced into the biochemical pool until the volume of the wastewater to be treated in the biochemical pool is 100%, which means the semi-pool inoculation start-up of the anaerobic ammonium oxidation process is completed.

[0028] Example 2 A method for semi-pool inoculation start-up of the anaerobic ammonium oxidation process: The difference from Example 1 is that the dosing agent contains 0.8 g / L sodium bicarbonate, 0.2 g / L magnesium sulfate, 0.025 g / L potassium dihydrogen phosphate, 0.005 g / L calcium chloride, 0.007 g / L ferrous sulfate and 5 mg / L butyric acid.

[0029] Example 3 A method for semi-pool inoculation start-up of the anaerobic ammonium oxidation process: The difference from Example 1 is that the dosing agent contains 1.2 g / L sodium bicarbonate, 0.4 g / L magnesium sulfate, 0.03 g / L potassium dihydrogen phosphate, 0.006 g / L calcium chloride, 0.008 g / L ferrous sulfate and 20 mg / L butyric acid.

[0030] Example 4 A method for semi-pool inoculation start-up of the anaerobic ammonium oxidation process: The difference from Example 1 is that the dosing agent does not contain butyric acid.

[0031] Example 5 A method for semi-pool inoculation start-up of the anaerobic ammonium oxidation process: The difference from Example 1 is that the carrier for inoculating the anaerobic ammonium oxidation bacteria is sludge.

[0032] Example 6 A method for semi-pool inoculation start-up of the anaerobic ammonium oxidation process: The difference from Example 1 is that when the nitrogen removal volume load in the biochemical pool reaches 0.3 kgN / m3·d, the dosing agent is replaced by the same volume of the wastewater to be treated and introduced into the biochemical pool, which means the semi-pool inoculation start-up of the anaerobic ammonium oxidation process is completed.

[0033] Comparative example Comparative example 1 A method for semi-pool inoculation start-up of the anaerobic ammonium oxidation process: The difference from Example 1 is that the dosage of ammonium chloride is 2.5 g / L.

[0034] Comparative example 2 A method for semi-pool inoculation start-up of the anaerobic ammonium oxidation process: The difference from Example 1 is that the dosage of sodium nitrite is 1.8 g / L.

[0035] Performance detection test Detection method Record the total duration required for the process used in Examples 1-5 to complete the start-up of the anaerobic ammonium oxidation process with half-pool inoculation.

[0036] After the start-up of the anaerobic ammonium oxidation process half-pools in Examples 1-6 and Comparative Examples 1-2 was completed, an equal mass of sludge biogas slurry was introduced into the biochemical pool. The compositions of the sludge biogas slurry used were all the same, and the nitrogen removal volume load within 24 h was measured respectively.

[0037] Table 1 Start-up time test Total duration of semi-pool inoculation start Example 1 60 days Example 2 61 days Example 3 61 days Example 4 62 days Example 5 63 days Table 2 Nitrogen removal volume load test <![CDATA[Volumetric nitrogen removal loading (kgN / m 3 ·d)]]> Example 1 0.65 Example 2 0.60 Example 3 0.63 Example 4 0.61 Example 5 0.58 Example 6 0.57 Comparative Example 1 0.48 Comparative Example 2 0.45 Combining Example 1 and Comparative Examples 1-2 and combining with Table 2, it can be seen that during the start-up of the anaerobic ammonium oxidation process half-pool inoculation, the dosages of ammonium chloride and sodium nitrite in the water distribution agent have a significant impact on the process start-up and nitrogen removal performance. In Example 1, the addition was carried out according to a specific calculation method for the dosages of ammonium chloride and sodium nitrite, and the addition amount varied with the operation of the water distribution in the biochemical pool. While in Comparative Example 1 and Comparative Example 2, the dosages of ammonium chloride and sodium nitrite were fixed values, and the nitrogen removal volume loads of Comparative Examples 1-2 decreased significantly compared with Example 1. This indicates that by adopting the above-mentioned calculation method for the dosages of ammonium chloride and sodium nitrite in this application, the addition amounts of the two can be accurately matched according to the actual operating conditions such as the scale of the biochemical pool, the influent flow rate, and the nitrogen influent volume load. It not only provides a stable and suitable substrate concentration for anaerobic ammonium-oxidizing bacteria, ensures the normal metabolic growth of bacteria, avoids abnormal substrate concentration problems, but also ensures that the substrate ratio conforms to the stoichiometric relationship, maintains the reaction efficiency, prevents metabolic disorders, comprehensively improves the process reliability, treatment effect and overall efficiency, and realizes the effective treatment of high-ammonia-nitrogen wastewater.

[0038] Combining Examples 1-3 and combining with Tables 1-2, it can be seen that when the components such as sodium bicarbonate, magnesium sulfate, potassium dihydrogen phosphate, calcium chloride, ferrous sulfate, and butyric acid in the water distribution agent change within a certain range, they have a certain impact on the process start-up duration and nitrogen removal volume load, but the overall process can still operate efficiently. The contents of these components in Examples 1-3 are different, the start-up duration is between 60 and 61 days, and the nitrogen removal volume load is between 0.60 and 0.65 kgN / m 3 ·d. This shows that when these components fluctuate within the concentration range of this application, different concentration combinations will still cause differences in the start-up efficiency and nitrogen removal effect, and the component ratio in Example 1 is the optimal one in this application.

[0039] Combined with Example 1 and Examples 4 - 5 and in combination with Tables 1 - 2, it can be seen that choosing porous ceramics as the carrier significantly facilitates anaerobic ammonium - oxidizing bacteria. The appropriate pore size allows the bacteria to firmly adhere and prevents their loss. The high porosity provides growth space and a mass diffusion channel. The appropriate roughness increases the contact area, which is conducive to initial attachment and the stable formation of biofilms. These characteristics comprehensively improve the attachment stability and growth efficiency of bacteria, accelerate the biofilm process, effectively shorten the start - up time of the anaerobic ammonium - oxidation process, and improve the start - up efficiency. Adding short - chain fatty acids (butyric acid) to the dosing agent can provide strong support for the growth and metabolism of anaerobic ammonium - oxidizing bacteria, provide energy and substances for the growth and reproduction of bacteria, accelerate the synthesis of biological macromolecules, and may also regulate metabolic pathways. This measure effectively shortens the start - up time of the process without adding too many complex components, helps the process reach stable operation faster, and improves the overall treatment efficiency and economic benefits.

[0040] Combined with Example 1 and Example 6 and in combination with Table 2, it can be seen that in Example 6, the way of replacing wastewater was changed, and the nitrogen removal volume load decreased to 0.57 kgN / m 3 ·d, indicating that the way of gradually replacing the dosing agent is more conducive to process start - up and nitrogen removal performance.

[0041] This specific embodiment is only an interpretation of the present application, and it does not limit the present application. After reading this specification, those skilled in the art can make modifications to this embodiment without creative contributions as needed, but as long as it is within the scope of the claims of the present application, it is protected by the patent law.

Claims

1. A method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process, characterized in that: The following steps are involved: Inoculating the anaerobic ammonia-oxidizing bacteria into the biochemical pool, and introducing a water preparation agent into the biochemical pool, wherein the components of the water preparation agent include ammonium chloride, sodium nitrite, sodium bicarbonate, magnesium sulfate, potassium dihydrogen phosphate, calcium chloride and ferrous sulfate; When the nitrogen removal volume load in the biochemical pool reaches 0.25-0.35kgN / m 3 ·d, the wastewater to be treated is introduced into the biochemical pool.

2. The method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process according to claim 1, characterized in that: After adding the water-adjusting agent to the biochemical pool, the temperature in the biochemical pool is controlled to be 34-36° C., and after adding the water-adjusting agent to the biochemical pool, the pH of the liquid in the biochemical pool is adjusted to be 7.5-8.2, the alkalinity is 200-300 mg / L, the dissolved oxygen is less than 0.1 mg / L, and the conductivity is less than 15.00 ms / cm.

3. The method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process according to claim 1, characterized in that: The components of the water dispensing agent include 0.8-1.2 g / L sodium bicarbonate, 0.2-0.4 g / L magnesium sulfate, 0.025-0.03 g / L potassium dihydrogen phosphate, 0.005-0.006 g / L calcium chloride, and 0.007-0.008 g / L ferrous sulfate.

4. The method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process according to claim 1, characterized in that: When the nitrogen removal volume load in the biochemical pool reaches 0.3 kgN / m 3 ·d, the added volume of the water-distributing agent is reduced by 10% every 72 hours, and the reduced amount of the water-distributing agent is replaced by an equal volume of wastewater to be treated and introduced into the biochemical pool until the volume of wastewater to be treated in the biochemical pool reaches 100%.

5. The method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process according to claim 1, characterized in that: The calculation method of the amount of ammonium chloride in the water preparation agent is: The m NH4Cl is the mass of added ammonium chloride, NLR is the nitrogen inlet volume load, V is the volume of the biochemical pool, and Q is the inlet flow rate.

6. The method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process according to claim 1, characterized in that: The amount of sodium nitrite in the water preparation agent is The m NaNO2 is the added mass of sodium nitrite, the NLR is the nitrogen inlet volume load, the V is the volume of the biochemical pool, and the Q is the inlet flow rate.

7. The method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process according to claim 1, characterized in that: The carrier for inoculating the anaerobic ammonia-oxidizing bacteria is porous ceramics, the pore size of the porous ceramics is 0.1-1 μm, the porosity of the porous ceramics is 60-70%, and the surface roughness of the porous ceramics is 2-4 μm.

8. The method for inoculating and starting a half-tank of an anaerobic ammonium oxidation process according to claim 1, characterized in that: The water distribution agent also includes 5-20 mg / L of short-chain fatty acids.

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