Method for quick fluidization of carrier filler based on MBBR process

Abstract

The application discloses a kind of based on MBBR process's carrier filler quick fluidization method, solve the problem that carrier filler non-fluidized state leads to biofilm formation speed slow, start time long;Technical solutions include: S1.MBBR process sewage treatment equipment starts, temporarily not access sewage;S2.in reactor, carrier filler is thrown and water is added;S3.quantitative inoculation sludge or aerobic bacteria agent is thrown into reactor;S4.open aeration, after setting time, add quantitative edible glucose, ammonium chloride and potassium dihydrogen phosphate, and water is supplemented to set volume;S5.continuous muffle 24 hours, and carrier filler in equipment is in fluidized state;Again quantitative edible glucose is added, and continue muffle setting time;S6.after again quantitative edible glucose, ammonium chloride and potassium dihydrogen phosphate are added, continue muffle, and maintain the fluidized state of carrier filler;S7.when carrier filler is in fluidized operation state and not add domestic sewage, need regularly supplement quantitative carbon source, nitrogen, phosphorus, guarantee that carrier filler is in sustained fluidized state.

Description

Technical Field

[0001] This invention belongs to the field of rural domestic sewage treatment technology, specifically relating to a method for rapid fluidization of carrier packing material based on MBBR process. Background Technology

[0002] The statements in this section are merely background information related to the present invention and do not necessarily constitute prior art.

[0003] As rural living standards improve, the volume of domestic sewage discharge increases, severely impacting the ecological environment. Therefore, integrated rural sewage treatment equipment is widely used. However, rural sewage is characterized by high nitrogen and phosphorus content and large fluctuations in discharge quality, making traditional processes and equipment difficult to adapt to. Thus, the MBBR (Medium-Boiler Bioreactor) process was introduced. The MBBR process combines the advantages of traditional fluidized bed and biological contact oxidation methods, using lightweight porous packing as a carrier. It reduces investment, energy consumption, and costs, adapts to fluctuations in water volume and quality, and exhibits good stability and reliability. It has become a mainstream technology suitable for rural working conditions.

[0004] However, a problem with commonly used MBBR carrier packing materials is that their density is close to that of the wastewater. Initially, they tend to float and accumulate on the surface, resulting in a long fluidization time, which can reach 7-15 days or even longer, affecting the biofilm formation rate and equipment start-up time. Existing related technology applications CN201010179153.9, CN201910497550.1, and CN2202311523273.X all involve methods for rapid biofilm formation using carrier packing materials. The methods provided in these three patents are all biofilm formation methods researched to accelerate biofilm formation and improve biofilm quality. They emphasize biofilm formation and still require approximately 7 days, lacking a method to enable "universal" carrier packing materials within the equipment to achieve fluidized operation in a short initial period.

[0005] In summary, the urgent problem to be solved is to design a low-cost, easy-to-operate method suitable for the operation and management of rural domestic sewage treatment equipment using the MBBR process, so as to prevent the carrier packing material inside the equipment from accumulating and overflowing during the initial use, achieve rapid fluidization, and lay the foundation for stable biofilm formation and efficient start-up of the equipment in the future. Summary of the Invention

[0006] To address the aforementioned problems, this invention provides a method for rapid fluidization of carrier packing material based on MBBR technology. This method solves the problem that during the initial start-up and operation of MBBR rural domestic sewage treatment equipment, the carrier packing material inside the equipment is completely suspended and piled up on the liquid surface, resulting in low biofilm formation speed and efficiency and long start-up time due to the non-fluidized state of the carrier packing material.

[0007] To achieve the above objectives, the present invention is implemented through the following technical solution:

[0008] This invention provides a method for rapid fluidization of carrier packing based on MBBR technology, comprising the following steps:

[0009] S1.MBBR process wastewater treatment equipment is being started up initially, and wastewater is not being connected to it yet;

[0010] S2. Load the packing material into the reactor and add water;

[0011] S3. Add a measured amount of inoculated sludge to the reactor, or add a measured amount of aerobic bacterial agent to the reactor;

[0012] S4. Turn on aeration, and after the set aeration time, add the set weight of edible glucose, ammonium chloride and potassium dihydrogen phosphate, and add water to the set volume;

[0013] S5. Continuous aeration is set for a set time, and the carrier packing inside the equipment is in a fluidized state to achieve rapid fluidization; after adding a certain amount of edible glucose, the aeration continues for the set time.

[0014] S6. After the initial aeration, the carrier packing in the reactor remains in a fluidized state. Then, a measured amount of edible glucose, ammonium chloride, and potassium dihydrogen phosphate are added, and the aeration continues to maintain the fluidized state of the carrier packing.

[0015] S7. After the carrier packing is in a fluidized state, when no domestic sewage is added, it is necessary to regularly add a certain amount of carbon source, and regularly add a certain amount of nitrogen and phosphorus to maintain the continuous fluidized movement of the carrier packing.

[0016] Preferably, the filler content of the carrier in S2 is 30%-35%.

[0017] Preferably, the concentration of inoculated sludge in S2 is 7800 mg / L, and the sludge concentration in the reactor after adding the inoculated sludge is 800 mg / L.

[0018] Preferably, when aeration is started in S4, the initial concentrations of COD, ammonia nitrogen, and total phosphorus in the reactor are controlled at 400 mg / L, 40 mg / L, and 5 mg / L, respectively.

[0019] Preferably, the continuous aeration time in S5 is 24h, and the air-to-water ratio in the reactor is controlled to be no less than 200:1; when the water temperature is 28℃-32℃ in summer, the DO in the water is maintained at 4-6mg / L; when the water temperature is 10℃-14℃ in winter, the DO in the water is maintained at 6-8mg / L.

[0020] Preferably, after continuous aeration in S5 for a set duration, the concentration of COD in the supernatant inside the equipment is 190-230 mg / L, the concentration of ammonia nitrogen is 22-35 mg / L, and the concentration of total phosphorus is 2.5-4.2 mg / L.

[0021] Preferably, after adding edible glucose again in S5, the aeration continues for the set duration.

[0022] Preferably, after aeration in S6, the concentration of COD in the supernatant of the reactor is 200-250 mg / L, the concentration of ammonia nitrogen is 20-29 mg / L, and the concentration of total phosphorus is 2.5-2.8 mg / L.

[0023] Preferably, the aerobic bacterial agent added in S3 is a dry powder aerobic bacterial agent.

[0024] Preferably, the concentration of the aerobic bacterial agent in the reactor is not less than 8 g / L, and the viable bacteria content in the aerobic bacterial agent is not less than 20 billion / gram.

[0025] Compared with the prior art, the advantages and positive effects of this invention are:

[0026] This invention enables rapid fluidization of the carrier packing material in the aerobic zone of MBBR (Multi-Bio Bioreactor) process rural domestic wastewater treatment equipment. It requires only the addition of a small amount of inoculum sludge or aerobic bacteria agent, supplemented with small amounts of nutrients such as glucose, ammonium chloride, and potassium dihydrogen phosphate, followed by aeration. This process requires minimal power, is low-cost, and is simple and feasible. Fluidization of the carrier packing material can be achieved in just 24 hours, a very short time. This lays a solid foundation for stable biofilm formation and efficient start-up operation of the equipment.

[0027] This invention is widely applicable to the start-up phase of MBBR process wastewater treatment equipment. It enables rapid fluidization of the mobile carrier packing material, ensuring full contact between the carrier packing and the liquid phase, thereby guaranteeing subsequent biofilm formation efficiency. Furthermore, this method is low-cost, simple to operate, and particularly suited to the practical needs of rural domestic wastewater treatment, possessing significant social benefits and promotional value. Detailed Implementation

[0028] It should be noted that the following detailed description is illustrative and intended to provide further explanation of the invention. Unless otherwise specified, all technical and scientific terms used in this invention have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains.

[0029] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the scope of exemplary embodiments according to the invention. As used herein, unless otherwise expressly indicated by the invention, the singular form is also intended to include the plural form. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0030] Example 1

[0031] Under summer water temperatures of 28℃-32℃, 12L of carrier packing material was added to a 50L reactor, with a packing filling rate of 30%. Water was added to bring the total volume to 35L. 4.1L of inoculum sludge with a concentration of 7800mg / L was added to the reactor, equivalent to a sludge concentration of 800mg / L. Aeration was started, and after 3 hours of aeration, 13.6g of edible glucose, 5.6g of ammonium chloride, and 0.88g of potassium dihydrogen phosphate were added, and water was added to bring the total volume to 40L (the initial concentrations of COD, ammonia nitrogen, and total phosphorus in the reactor were approximately 400mg / L, 40mg / L, and 5mg / L, respectively; the initial COD was chemical oxygen demand). Aeration was continued for 24 hours, with the air-to-water ratio in the reactor controlled to be no less than 200:1, and the dissolved oxygen (DO) in the water maintained at 4-6mg / L.

[0032] After 24 hours: the carrier packing in the reactor was in a fluidized state; the concentrations of COD, ammonia nitrogen and total phosphorus in the supernatant in the reactor were 220 mg / L, 30 mg / L and 4 mg / L, respectively; after adding 6.8 g of edible glucose, the reactor was aerated for another 24 hours.

[0033] After a cumulative run of 48 hours: the carrier packing in the reactor remained in a fluidized state; the concentrations of COD, ammonia nitrogen, and total phosphorus in the supernatant of the reactor were 220 mg / L, 23 mg / L, and 2.8 mg / L, respectively. After adding 6.8 g of edible glucose, 2.8 g of ammonium chloride, and 0.44 g of potassium dihydrogen phosphate, the reactor was further aerated.

[0034] According to the method in Example 1 above, under summer water temperatures of approximately 30°C, inoculating a fixed amount of sludge can achieve rapid fluidization of the carrier packing material for 24 hours. In practical applications, domestic sewage can then be continuously introduced for start-up operation. After the carrier packing material reaches a fluidized state, without the addition of domestic sewage, a fixed amount of carbon source needs to be added every 24 hours, and a fixed amount of nitrogen and phosphorus needs to be added every 48 hours to maintain the continuous fluidization of the carrier packing material.

[0035] Example 2

[0036] Under summer water temperatures of 28℃-32℃, 12L of carrier packing material was added to a 50L reactor, with a packing filling rate of 30%. Water was added to bring the total volume to 35L. 320g of aerobic bacteria agent (equivalent to 8g / L) was added to the reactor. Aeration was started, and after 3 hours of aeration, 13.6g of edible glucose, 5.6g of ammonium chloride, and 0.88g of potassium dihydrogen phosphate were added, and water was added to bring the total volume to 40L. The initial concentrations of COD, ammonia nitrogen, and total phosphorus in the reactor were approximately 400mg / L, 40mg / L, and 5mg / L, respectively. Aeration was continued for 24 hours, and the air-to-water ratio in the reactor was controlled to be no less than 200:1, with DO in the water maintained at 4-6mg / L.

[0037] After 24 hours: the carrier packing in the reactor was in a fluidized state; the concentrations of COD, ammonia nitrogen and total phosphorus in the supernatant in the reactor were 190 mg / L, 22 mg / L and 3 mg / L, respectively; after adding 6.8 g of edible glucose, the reactor was aerated for another 24 hours.

[0038] After a cumulative run of 48 hours: the carrier packing in the reactor remained in a fluidized state; the concentrations of COD, ammonia nitrogen, and total phosphorus in the supernatant of the reactor were 200 mg / L, 20 mg / L, and 2.5 mg / L, respectively. After adding 6.8 g of edible glucose, 2.8 g of ammonium chloride, and 0.44 g of potassium dihydrogen phosphate, the reactor was further aerated.

[0039] According to the method in Example 2 above, under summer water temperatures of approximately 30°C, adding a measured amount of aerobic bacteria agent can achieve rapid fluidization of the carrier packing material for 24 hours. In practical applications, it can then continuously be introduced into the system for startup with domestic sewage. After the carrier reaches a fluidized state, when no domestic sewage is introduced, a measured amount of carbon source needs to be added every 24 hours, and a measured amount of nitrogen and phosphorus needs to be added every 48 hours to maintain the continuous fluidization of the carrier packing material.

[0040] The aerobic bacterial agent is composed of nitrifying bacteria, Acinetobacter calcium acetate, Bacillus spores, highly efficient flocculants, yeast, micrococcus, enzymes, and nutrients, with a live bacteria content of not less than 20 billion / gram. The nitrifying bacteria, Acinetobacter calcium acetate, Bacillus spores, highly efficient flocculants, yeast, micrococcus, enzymes, and nutrients are all existing materials.

[0041] Example 3

[0042] Under winter water temperature conditions of 10℃-14℃, add 12L of carrier packing material to a 50L reactor, with a packing filling rate of 30%, and add water to a total volume of 35L. Add 320g of aerobic bacteria agent to the reactor, equivalent to 8g / L of aerobic bacteria agent. Start aeration and allow it to stand still for 3 hours. Then add 13.6g of edible glucose, 5.6g of ammonium chloride, and 0.88g of potassium dihydrogen phosphate, and add water to a total volume of 40L (the initial concentrations of COD, ammonia nitrogen, and total phosphorus in the reactor are approximately 400mg / L, 40mg / L, and 5mg / L, respectively). Allow it to stand still for 24 hours, controlling the air-to-water ratio in the reactor to be no less than 200:1, and maintaining the dissolved oxygen (DO) in the water at 6-8mg / L.

[0043] After 24 hours: the carrier packing in the reactor was in a fluidized state; the concentrations of COD, ammonia nitrogen and total phosphorus in the supernatant in the reactor were 230 mg / L, 35 mg / L and 4 mg / L, respectively; after adding 6.8 g of edible glucose, the reactor was aerated for another 24 hours.

[0044] After a cumulative run of 48 hours: the carrier packing in the reactor remained in a fluidized state; the concentrations of COD, ammonia nitrogen, and total phosphorus in the supernatant of the reactor were 250 mg / L, 29 mg / L, and 2.5 mg / L, respectively. After adding 6.8 g of edible glucose, 2.8 g of ammonium chloride, and 0.44 g of potassium dihydrogen phosphate, the reactor was further aerated.

[0045] According to the method in Example 3 above, under winter water temperature conditions of approximately 12°C, adding a fixed amount of aerobic bacteria agent can achieve rapid fluidization of the carrier packing material for 24 hours. In practical applications, it can then continuously be introduced into the system for startup with domestic sewage. After the carrier packing material reaches a fluidized state, when no domestic sewage is added, a fixed amount of carbon source needs to be added every 24 hours, and a fixed amount of nitrogen and phosphorus needs to be added every 48 hours to maintain the continuous fluidization of the carrier packing material.

[0046] Example 4

[0047] Under winter water temperatures of 10℃-14℃, 0.84m³ of aerobic bacteria agent was added to a 2.8m³ cylindrical horizontal tank with a packing filling rate of 30%. The carrier packing was added and water was brought to the effective water level line. 22.40kg of aerobic bacteria agent (equivalent to 8g / L) was added to the equipment. Aeration was started, and after 3 hours of aeration, 952g of edible glucose, 392g of ammonium chloride, and 61.6g of potassium dihydrogen phosphate were added (the initial concentrations of COD, ammonia nitrogen, and total phosphorus in the equipment were approximately 400mg / L, 40mg / L, and 5mg / L, respectively). Aeration was continued for 24 hours, and the air-to-water ratio in the equipment was controlled to be no less than 200:1, with the dissolved oxygen (DO) in the water maintained at 6-8mg / L.

[0048] After 24 hours: the carrier packing inside the equipment was in a fluidized state; the concentrations of COD, ammonia nitrogen and total phosphorus in the supernatant inside the equipment were 220 mg / L, 33 mg / L and 4.2 mg / L, respectively; after adding 476 g of edible glucose, the equipment was aerated for another 24 hours.

[0049] After a cumulative run of 48 hours: the carrier packing inside the equipment remained in fluidized operation; the concentrations of COD, ammonia nitrogen, and total phosphorus in the supernatant inside the equipment were 240 mg / L, 26 mg / L, and 2.6 mg / L, respectively. After adding 476 g of edible glucose, 196 g of ammonium chloride, and 30.8 g of potassium dihydrogen phosphate, aeration continued.

[0050] According to the method in Example 4 above, under winter water temperature conditions of approximately 12°C, adding a fixed amount of aerobic bacteria agent can achieve a rapid fluidized state of the carrier packing material inside the sewage treatment equipment for 24 hours. In practical applications, domestic sewage can then be continuously introduced for start-up operation. After the carrier packing material reaches a fluidized state, when no domestic sewage is added, a fixed amount of carbon source needs to be added every 24 hours, and a fixed amount of nitrogen and phosphorus needs to be added every 48 hours to maintain the continuous fluidized movement of the carrier packing material.

[0051] While the specific embodiments of the present invention have been described above, they are not intended to limit the scope of protection of the present invention. Those skilled in the art should understand that various modifications or variations that can be made by those skilled in the art without creative effort based on the technical solutions of the present invention are still within the scope of protection of the present invention.

Claims

1. A method for rapid fluidization of carrier packing based on MBBR process, characterized in that, Includes the following steps: S1.MBBR process wastewater treatment equipment is being started up initially, and wastewater is not being connected to it yet; S2. Load the packing material into the reactor and add water; S3. A measured amount of inoculated sludge is added to the reactor, or a measured amount of aerobic bacterial agent is added to the reactor; the aerobic bacterial agent is composed of nitrifying bacteria, Acinetobacter calcium acetate, Bacillus spp., highly efficient flocculants, yeast, Micrococcus spp., enzymes, and nutrients, and the concentration of the aerobic bacterial agent in the reactor is not less than 8 g / L, and the viable bacteria content in the aerobic bacterial agent is not less than 20 billion / gram; the concentration of inoculated sludge in S3 is 7800 mg / L, and the sludge concentration in the reactor after adding the inoculated sludge is 800 mg / L; S4. Turn on aeration, and after the set aeration time, add the set weight of edible glucose, ammonium chloride and potassium dihydrogen phosphate, and add water to the set volume; S5. Continuous aeration is set for a set time, controlling the air-to-water ratio in the reactor to be no less than 200:

1. In summer, when the water temperature is 28℃-32℃, the dissolved oxygen (DO) in the water is maintained at 4-6 mg / L. In winter, when the water temperature is 10℃-14℃, the DO in the water is maintained at 6-8 mg / L. The carrier packing in the equipment is in a fluidized state to achieve rapid fluidization. After adding a certain amount of edible glucose, continue the set aeration time. S6. After initial aeration, the carrier packing material in the reactor remains in a fluidized state. Then, a measured amount of edible glucose, ammonium chloride, and potassium dihydrogen phosphate are added, and the aeration continues to maintain the carrier packing material in a fluidized state. S7. After the carrier packing is in a fluidized state, when no domestic sewage is added, it is necessary to regularly add a certain amount of carbon source, and regularly add a certain amount of nitrogen and phosphorus to maintain the continuous fluidized movement of the carrier packing.

2. The method for rapid fluidization of carrier packing based on MBBR process as described in claim 1, characterized in that, In S2, the filler material of the carrier is 30%-35%.

3. The method for rapid fluidization of carrier packing based on MBBR process as described in claim 1, characterized in that, When aeration is started in S4, the initial concentrations of COD, ammonia nitrogen, and total phosphorus in the reactor are controlled at 400 mg / L, 40 mg / L, and 5 mg / L, respectively.

4. The method for rapid fluidization of carrier packing based on MBBR process as described in claim 1, characterized in that, The continuous exposure time in S5 is 24 hours.

5. The method for rapid fluidization of carrier packing based on MBBR process as described in claim 1, characterized in that, After setting the continuous aeration time in S5, the concentration of COD in the supernatant inside the equipment is 190-230 mg / L, the concentration of ammonia nitrogen is 22-35 mg / L, and the concentration of total phosphorus is 2.5-4.2 mg / L.

6. The method for rapid fluidization of carrier packing based on MBBR process as described in claim 1, characterized in that, After being aerated in S6, the concentration of COD in the supernatant of the reactor is 200-250 mg / L, the concentration of ammonia nitrogen is 20-29 mg / L, and the concentration of total phosphorus is 2.5-2.8 mg / L.

7. The method for rapid fluidization of carrier packing based on MBBR process as described in claim 1, characterized in that, The aerobic bacterial agent added in S3 is a dry powder aerobic bacterial agent.