A full-process treatment method and system for chip wastewater based on anaerobic ammonium oxidation

Abstract

The present invention discloses a full-process treatment method and system for chip wastewater based on anaerobic ammonia oxidation, comprising: a water quality and quantity pool connected in sequence, a physicochemical treatment unit, a biochemical treatment unit and a clear water pool, wherein the biochemical treatment unit comprises a third regulating pool, an autotrophic denitrification unit and a deep denitrification unit connected in sequence. The method mixes and neutralizes various wastewaters, thereby reducing the use of acid-base neutralizing agents relative to treating each wastewater separately. The physicochemical unit is then used for physical impurity removal, fluorine removal and hydrogen peroxide removal, and then the biochemical unit is used for biochemical nitrogen removal. At the same time, the present application uses autotrophic denitrification-anaerobic ammonia oxidation reaction for denitrification, which saves a lot of energy consumption and reduces greenhouse gas emissions compared to processes such as ammonia stripping, AO, and MBR. The overall process has the advantages of simple process route, good treatment effect, low investment and operating costs, etc.

Description

Technical Field

[0001] The present invention belongs to the technical field of sewage treatment, and more specifically, relates to a full-process chip wastewater treatment method and system based on anaerobic ammonia oxidation. Background Art

[0002] With the rapid advancement of information technology, the demand for chips, as core components of electronic devices, has increased dramatically. However, chip manufacturing is a highly complex and sophisticated process involving multiple steps, such as cleaning, etching, and electroplating, which generate wastewater containing various pollutants. This type of wastewater has complex composition and high concentration, with large fluctuations in water volume. It contains acidic and alkaline substances, fluoride, hydrogen peroxide, ammonia nitrogen, etc., which are toxic and difficult to treat. Chip companies mostly adopt a method of treating a specific type of wastewater separately, but due to large fluctuations in water quality and volume, stable operation is difficult. In addition, most of the physical and chemical treatment methods used are expensive to use chemical agents and may also cause secondary pollution.

[0003] For the chip manufacturing industry, it is urgent to develop a full-process processing technology with good processing effect, strong impact resistance, and economic and energy-saving properties to solve the problems of unstable processing effect, high investment and operating costs of the current processing technology. Summary of the Invention

[0004] The purpose of the present invention is to address the deficiencies in the prior art and provide a full-process treatment method for chip wastewater based on anaerobic ammonia oxidation, so as to solve the problem that most existing chip companies adopt a method of separate treatment for a certain type of wastewater, but due to large fluctuations in water quality and quantity, it is difficult to operate stably, and most of them adopt physical and chemical treatment methods, the cost of using chemical agents is high, and secondary pollution may also occur.

[0005] In order to achieve the above objectives, the present invention provides a full-process treatment method for chip wastewater based on anaerobic ammonia oxidation, comprising:

[0006] The water quality and quantity pool, physicochemical treatment unit, biochemical treatment unit and clear water pool are connected in sequence;

[0007] The physicochemical treatment unit includes a first regulating tank, a fluorine removal unit, a second regulating tank and a hydrogen peroxide removal unit connected in sequence, the pH value of the first regulating tank is 7.5-8.5, the pH value of the second regulating tank is 10-11, the fluorine removal unit is provided with a calcium salt dosing system, and the hydrogen peroxide removal unit is provided with a manganese sand catalyst dosing system;

[0008] The biochemical treatment unit includes a third regulating tank, an autotrophic denitrification unit, and a deep denitrification unit connected in sequence, wherein the pH value of the third regulating tank is 6.7-8.5, a solidified carrier is provided in the autotrophic denitrification unit, and the filling ratio of the solidified carrier is 5-15%, and the deep denitrification unit includes a first aeration zone, a non-aeration zone, and a second aeration zone with a volume ratio of 3:3:1, and the autotrophic denitrification unit and the second aeration zone are respectively provided with a first built-in sedimentation tank and a second built-in sedimentation tank;

[0009] The water quality and quantity pool is filled with wastewater, wherein the wastewater includes fluorine-containing wastewater, hydrogen peroxide-containing wastewater, ammonia nitrogen-containing wastewater, acid wastewater, and alkaline wastewater;

[0010] Adjust the sludge concentration of the flocculent activated sludge of the autotrophic denitrification unit to 2-5 g / L, adjust the inlet temperature to 28-30° C., the hydraulic retention time to 30-100 h, the dissolved oxygen to 0.1-0.8 mg / L, and the pH to 7.0-8.5 through a temperature control device;

[0011] If the ammonia nitrogen concentration in the autotrophic denitrification unit is higher than 50 mg / L, the dissolved oxygen is adjusted to 0.6-0.8 mg / L through aeration, and / or hydroxylamine hydrochloride is added to the system for controlling the activity of the bacterial strain and regulating the addition of the agent;

[0012] If the ratio of the concentration of nitrate nitrogen generated in the autotrophic denitrification unit to the concentration of ammonia nitrogen removed is greater than 15%, discharging part of the activated sludge;

[0013] Adjust the sludge concentration of the flocculent activated sludge in the deep denitrification unit to 2-5 g / L, the hydraulic retention time to 10-30 h, the dissolved oxygen in the first aeration zone to 0.5-1.0 mg / L, and the dissolved oxygen in the second aeration zone to 0.1-0.8 mg / L;

[0014] The first aeration zone adjusts the carbon source addition according to the nitrate nitrogen concentration to make the nitrate nitrogen concentration within 5-30 mg / L;

[0015] The second aeration zone controls the ammonia nitrogen concentration through aeration. If the ammonia nitrogen concentration of the effluent is greater than 5 mg / L, aeration is used to reduce the ammonia nitrogen concentration.

[0016] Optionally, the manganese sand catalyst dosing system is configured to remove 100 mg / L of hydrogen peroxide with 1 kg of manganese sand, and the content of manganese dioxide, an effective ingredient in the manganese sand, is greater than 40%;

[0017] If the hydrogen peroxide removal efficiency is lower than 80%, backwashing should be performed, the amount of treated water should be reduced, or part of the manganese sand should be replaced.

[0018] The present invention also provides a full-process chip wastewater treatment system based on anaerobic ammonia oxidation, comprising:

[0019] The water quality and quantity pool, physicochemical treatment unit, biochemical treatment unit and clear water pool are connected in sequence;

[0020] The physicochemical treatment unit includes a first regulating tank, a fluorine removal unit, a second regulating tank and a hydrogen peroxide removal unit connected in sequence, the fluorine removal unit is provided with a calcium salt dosing system, and the hydrogen peroxide removal unit is provided with a manganese sand catalyst dosing system;

[0021] The biochemical treatment unit includes a third regulating tank, a temperature regulating device, an autotrophic denitrification unit and a deep denitrification unit connected in sequence, a solidified carrier is provided in the autotrophic denitrification unit, the deep denitrification unit includes a first aeration zone, a non-aeration zone and a second aeration zone with a volume ratio of 3:3:1, and the autotrophic denitrification unit and the second aeration zone are respectively provided with a first built-in sedimentation tank and a second built-in sedimentation tank;

[0022] The first regulating tank is provided with a first online pH monitoring system and a first feedback regulating agent dosing system;

[0023] The defluorination unit is provided with an online fluoride ion monitoring system and a calcium salt agent dosing system;

[0024] The second regulating tank is provided with a second online pH monitoring system and a second feedback regulating agent dosing system;

[0025] The hydrogen peroxide removal unit is provided with an online hydrogen peroxide monitoring system and a manganese sand catalyst dosing system;

[0026] The third regulating tank is provided with a third online pH monitoring system and a third feedback regulating agent dosing system;

[0027] The autotrophic denitrification unit is provided with a fourth online pH monitoring system, a fourth feedback regulating agent dosing system, a first online ammonia nitrogen monitor, a first online nitrate nitrogen monitor, a first online DO monitor and a first built-in sedimentation tank, wherein the first built-in sedimentation tank is arranged at the tail end of the autotrophic denitrification unit and is connected to the head end of the autotrophic denitrification unit through a first sludge return pipe;

[0028] The first aeration zone is provided with a second online nitrate nitrogen monitor and a second online DO monitor;

[0029] The non-aeration zone is provided with a carbon source addition system;

[0030] The second aeration zone is provided with a second online ammonia nitrogen monitor and a third online DO monitor.

[0031] Optionally, the first online DO monitor is arranged at the head end of the autotrophic denitrification unit, and the first online ammonia nitrogen monitor and the first online nitrate nitrogen monitor are arranged at the tail end of the autotrophic denitrification unit, located in the outlet channel of the first built-in sedimentation tank.

[0032] The present invention provides a full-process treatment method for chip wastewater based on anaerobic ammonia oxidation, which has the following beneficial effects:

[0033] This method mixes and neutralizes various wastewaters, reducing the use of acid-base neutralizing agents compared to treating each wastewater separately. The physical and chemical units are then used to physically remove impurities, fluorine, and hydrogen peroxide, followed by biochemical nitrogen removal. This application also uses autotrophic denitrification and anaerobic ammonia oxidation reactions for denitrification, saving significant energy consumption and reducing greenhouse gas emissions compared to processes such as ammonia stripping, AO, and MBR. The overall process has the advantages of a simple process route, good treatment results, and low investment and operating costs.

[0034] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] The above and other objects, features and advantages of the present invention will become more apparent through a more detailed description of exemplary embodiments of the present invention with reference to the accompanying drawings, wherein like reference numerals generally represent like components throughout the exemplary embodiments of the present invention.

[0036] Figure 1 A process flow chart of a full-process chip wastewater treatment method based on anaerobic ammonia oxidation according to an embodiment of the present invention is shown.

[0037] Figure 2 A schematic structural diagram of an autotrophic denitrification unit and a deep denitrification unit of a full-process chip wastewater treatment method based on anaerobic ammonium oxidation according to an embodiment of the present invention is shown.

[0038] Figure 3 A structural schematic diagram of a first built-in sedimentation tank of a full-process chip wastewater treatment method based on anaerobic ammonia oxidation according to an embodiment of the present invention is shown.

[0039] Description of reference numerals:

[0040] 1-water quality and quantity equalization tank; 2-physical and chemical treatment unit; 2.1-first regulating tank; 2.2-fluorine removal unit; 2.3-second regulating tank; 2.4-hydrogen peroxide removal unit; 3-biochemical treatment unit; 3.1-third regulating tank; 3.2-temperature control equipment; 3.3-autotrophic denitrification unit; 3.3.1-immobilized carrier; 3.3.2-first sludge return pipe; 3.3.3-first excess sludge discharge pipe; 3.3.4-microorganism activity control agent dosing system; 3.3.5-fourth feedback control agent dosing system; 3.4-deep denitrification unit; 3.4.1-second sludge return pipe; 3.4.2-second excess sludge discharge pipe; 3.4.3- Carbon source dosing system; 3.5-Variable frequency aeration system; 3.6-First built-in sedimentation tank; 3.6.1-Water collection port; 3.6.2-Outlet weir and outlet channel; 3.6.3-Outlet; 3.6.4-Sludge collection pipe; 3.6.5-Second built-in sedimentation tank; 3.7.1-First online DO monitor; 3.7.2-Second online DO monitor; 3.7.3-Third online DO monitor; 3.8-First online pH monitor; 3.9.1-First online ammonia nitrogen monitor; 3.9.2-Second online ammonia nitrogen monitor; 3.10.1-First online nitrate nitrogen monitor; 3.10.2-Second online nitrate nitrogen monitor; 4-Clear water tank. DETAILED DESCRIPTION

[0041] The preferred embodiments of the present invention will be described in more detail below. Although the preferred embodiments of the present invention are described below, it should be understood that the present invention can be implemented in various forms and should not be limited by the embodiments set forth herein. Instead, these embodiments are provided to make the present invention more thorough and complete and to fully convey the scope of the present invention to those skilled in the art.

[0042] like Figure 1-3 As shown, a full-process treatment method for chip wastewater based on anaerobic ammonium oxidation includes:

[0043] The water quality and quantity pool, physicochemical treatment unit, biochemical treatment unit and clear water pool are connected in sequence;

[0044] The physicochemical treatment unit includes a first regulating tank, a fluorine removal unit, a second regulating tank and a hydrogen peroxide removal unit connected in sequence. The pH value of the first regulating tank is 7.5-8.5, and the pH value of the second regulating tank is 10-11. The fluorine removal unit is provided with a calcium salt dosing system, and the hydrogen peroxide removal unit is provided with a manganese sand catalyst dosing system.

[0045] The biochemical treatment unit includes a third regulating tank, an autotrophic denitrification unit, and a deep denitrification unit connected in sequence. The pH value of the third regulating tank is 6.7-8.5. A solidified carrier is provided in the autotrophic denitrification unit, and the filling ratio of the solidified carrier is 5-15%. The deep denitrification unit includes a first aeration zone, a non-aeration zone, and a second aeration zone with a volume ratio of 3:3:1. The autotrophic denitrification unit and the second aeration zone are respectively provided with a first built-in sedimentation tank and a second built-in sedimentation tank;

[0046] The water quality and quantity pool is filled with wastewater, including fluorine-containing wastewater, hydrogen peroxide-containing wastewater, ammonia nitrogen-containing wastewater, acid wastewater, and alkaline wastewater;

[0047] Adjust the sludge concentration of the flocculent activated sludge in the autotrophic denitrification unit to 2-5 g / L, adjust the inlet water temperature to 28-30°C, the hydraulic retention time to 30-100 hours, the dissolved oxygen to 0.1-0.8 mg / L, and the pH to 7.0-8.5 through the temperature control equipment;

[0048] If the ammonia nitrogen concentration in the autotrophic denitrification unit is higher than 50 mg / L, the dissolved oxygen is adjusted to 0.6-0.8 mg / L by aeration, and / or hydroxylamine hydrochloride is added to the system for controlling the activity of the bacterial strain and regulating the addition of the agent;

[0049] If the ratio of the concentration of nitrate nitrogen generated in the autotrophic denitrification unit to the concentration of ammonia nitrogen removed is greater than 15%, part of the activated sludge is discharged;

[0050] Adjust the sludge concentration of the flocculent activated sludge in the deep denitrification unit to 2-5 g / L, the hydraulic retention time to 10-30 h, the dissolved oxygen in the first aeration zone to 0.5-1.0 mg / L, and the dissolved oxygen in the second aeration zone to 0.1-0.8 mg / L;

[0051] In the first aeration zone, the carbon source dosage is adjusted according to the nitrate nitrogen concentration to keep the nitrate nitrogen concentration within 5-30 mg / L;

[0052] The second aeration zone controls the ammonia nitrogen concentration through aeration. If the ammonia nitrogen concentration of the effluent is greater than 5 mg / L, aeration will reduce the ammonia nitrogen concentration.

[0053] Specifically, various wastewaters are mixed and neutralized, which reduces the use of acid-base neutralizing agents compared to treating each wastewater separately. The physical and chemical units are then used to physically remove impurities, fluorine, and hydrogen peroxide, and then the biochemical units are used to biochemically remove nitrogen. At the same time, this application uses autotrophic denitrification - anaerobic ammonia oxidation reaction for denitrification, which saves a lot of energy consumption and reduces greenhouse gas emissions compared to ammonia stripping, AO, MBR and other processes. The overall process has the advantages of a simple process route, good treatment effect, and low investment and operating costs.

[0054] Furthermore, the first and second built-in sedimentation tanks have the same structure. The defluorination unit of this application includes a primary or secondary defluorination unit, preferably a secondary defluorination unit. Fluoride ions are removed by adding calcium salts, flocculants, and coagulants to generate calcium fluoride precipitates. The hydrogen peroxide removal unit utilizes manganese sand as a catalytic reaction to decompose hydrogen peroxide into water and oxygen. Neither of these reactants produces substances that could affect subsequent sludge formation and denitrification reactions, thereby gradually reducing the water treatment load and difficulty.

[0055] Furthermore, the acidic substance used to adjust the pH in each regulating tank can be acidic wastewater, dilute sulfuric acid or dilute hydrochloric acid, and the alkaline substance can be alkaline wastewater, sodium hydroxide or lime.

[0056] In this embodiment, the manganese sand catalyst dosing system is configured to remove 100 mg / L of hydrogen peroxide with 1 kg of manganese sand, and the content of manganese dioxide, an effective ingredient in the manganese sand, is greater than 40%;

[0057] If the hydrogen peroxide removal efficiency is lower than 80%, backwashing should be performed, the amount of treated water should be reduced, or part of the manganese sand should be replaced.

[0058] Specifically, the hydrogen peroxide removal unit has a hydraulic retention time of at least 3 minutes. Manganese sand is used to catalyze the decomposition of hydrogen peroxide into water and oxygen. The manganese sand is added at a ratio such that 1 kg of sand removes 100 mg / L of hydrogen peroxide, and the manganese dioxide content in the sand is greater than 40%. When the hydrogen peroxide removal efficiency falls below 80%, backwashing and reduced treatment water volume are performed. If the catalytic capacity cannot be restored and the hydrogen peroxide removal efficiency remains below 80%, 10% of the manganese sand is replaced until the catalytic effect is restored.

[0059] The present invention also provides a full-process chip wastewater treatment system based on anaerobic ammonia oxidation, comprising:

[0060] The water quality and quantity pool, physicochemical treatment unit, biochemical treatment unit and clear water pool are connected in sequence;

[0061] The physicochemical treatment unit includes a first regulating tank, a fluorine removal unit, a second regulating tank and a hydrogen peroxide removal unit connected in sequence. The fluorine removal unit is provided with a calcium salt dosing system, and the hydrogen peroxide removal unit is provided with a manganese sand catalyst dosing system.

[0062] The biochemical treatment unit includes a third regulating tank, a temperature control device, an autotrophic denitrification unit and a deep denitrification unit connected in sequence. A solidified carrier is provided in the autotrophic denitrification unit. The deep denitrification unit includes a first aeration zone, a non-aeration zone and a second aeration zone with a volume ratio of 3:3:1. The autotrophic denitrification unit and the second aeration zone are respectively provided with a first built-in sedimentation tank and a second built-in sedimentation tank;

[0063] The first regulating tank is provided with a first online pH monitoring system and a first feedback regulating agent dosing system;

[0064] The defluorination unit is equipped with an online fluoride ion monitoring system and a calcium salt agent dosing system;

[0065] The second regulating tank is provided with a second online pH monitoring system and a second feedback regulating agent dosing system;

[0066] The hydrogen peroxide removal unit is equipped with an online hydrogen peroxide monitoring system and a manganese sand catalyst dosing system;

[0067] The third regulating tank is provided with a third online pH monitoring system and a third feedback regulating agent dosing system;

[0068] The autotrophic denitrification unit is provided with a fourth online pH monitoring system, a fourth feedback regulating agent dosing system, a first online ammonia nitrogen monitor, a first online nitrate nitrogen monitor, a first online DO monitor and a first built-in sedimentation tank. The first built-in sedimentation tank is provided at the tail end of the autotrophic denitrification unit and is connected to the head end of the autotrophic denitrification unit through a first sludge return pipe;

[0069] The first aeration zone is provided with a second online nitrate nitrogen monitor and a second online DO monitor;

[0070] The non-aeration area is equipped with a carbon source dosing system;

[0071] The second aeration zone is provided with a second online ammonia nitrogen monitor and a third online DO monitor.

[0072] Specifically, wastewater flows sequentially through the water quality and quantity equalization tank, the first regulating tank, the fluoride removal unit, the second regulating tank, the hydrogen peroxide removal unit, the third regulating tank, the temperature control equipment, the autotrophic denitrification unit, the deep denitrification unit, and the clear water tank. Neutralization, fluoride removal, hydrogen peroxide removal, autotrophic denitrification, and anaerobic ammonia oxidation deep denitrification ensure that the wastewater meets discharge requirements. Each feedback regulating agent dosing system adds acid, alkaline agents, or acid or alkaline solutions as needed to adjust the pH.

[0073] In this embodiment, the first online DO monitor is arranged at the head end of the autotrophic denitrification unit, and the first online ammonia nitrogen monitor and the first online nitrate nitrogen monitor are arranged at the tail end of the autotrophic denitrification unit, located in the outlet channel of the first built-in sedimentation tank.

[0074] Specifically, the water outlet status at the tail end is monitored to confirm the final denitrification efficiency, so as to avoid the influence of the volume of the autotrophic denitrification unit and the distribution of the water body on the monitoring accuracy.

[0075] Example

[0076] This embodiment provides a full-process chip wastewater treatment method based on anaerobic ammonium oxidation, using a full-process chip wastewater treatment system based on anaerobic ammonium oxidation:

[0077] The wastewater containing various pollutants generated in the chip manufacturing process is first mixed into the 1-water quality and quantity pool, and then enters the 2.1-first regulating pool, 2.2-fluorine removal unit, 2.3-second regulating pool and 2.4-hydrogen peroxide removal unit of the 2-physical and chemical treatment unit in sequence. The wastewater treated in the 2-physical and chemical treatment unit enters the 3.1-third regulating pool, 3.2-temperature control equipment, 3.3-autotrophic denitrification unit and 3.4-deep denitrification unit of the 3-biochemical treatment unit in sequence, and finally flows into the 4-clear water pool to meet the discharge standards. Among them, the 3.3-autotrophic denitrification unit and the 3.4-deep denitrification unit share a 3.5-variable frequency aeration system.

[0078] Both the 2nd and 3rd physicochemical treatment units are equipped with control systems, enabling online parameter monitoring and real-time feedback adjustments based on varying treatment requirements. The pH of the wastewater in the 2.1st regulating tank, the 2.3nd regulating tank, and the 3.1st regulating tank is controlled at 7.5-8.5, 10-11, and 6.7-8.5, respectively. pH adjustment is achieved using a 30% hydrochloric acid solution and a 30% caustic soda solution.

[0079] The 2.2-fluoride removal unit is a two-stage defluoridation unit. A concentration of 20% calcium chloride, 2% flocculant PAC, and 0.1% coagulant PAM are added to form calcium fluoride precipitate to remove fluoride ions. Online fluoride ion monitoring is used to monitor the fluoride ion concentration in the inlet and outlet water. The calcium chloride dosage is calculated based on the solubility product of the inlet fluoride ion concentration and CaF2. If the concentration is greater than 10 mg / L, the calcium chloride dosage is increased until the effluent fluoride ion concentration meets the required effluent fluoride level.

[0080] 2.4 - Hydrogen peroxide removal unit, with a residence time of 3 minutes, utilizes manganese sand to catalyze the decomposition of hydrogen peroxide into water and oxygen. The manganese sand is dosed at a ratio such that 1 kg removes 100 mg / L of hydrogen peroxide, and the manganese dioxide content in the sand is greater than 40%. If the hydrogen peroxide removal efficiency falls below 80%, backwashing and reduced treatment water volume are performed. If catalytic performance fails to recover and the hydrogen peroxide removal efficiency remains below 80%, 10% of the manganese sand is replaced until the catalytic effect is restored.

[0081] 3.2- Temperature control equipment, through online monitoring of inlet and outlet water temperatures, automatically adjusts equipment parameters to raise the wastewater temperature to 28-30℃, ensuring that subsequent microorganisms can carry out pollutant removal operations within the most suitable temperature range.

[0082] 3.3 - Autotrophic denitrification unit, the residence time is set to 82h, the concentration of flocculent activated sludge in the pool is 4-5g / L, the filling ratio of 3.3.1 - immobilized carrier is 15%, and the aeration volume is controlled online by 3.5 - variable frequency aeration system so that the dissolved oxygen in the pool detected by 3.7.1 - first online DO monitor is 0.2-0.5mg / L; the pH in the pool is monitored by 3.8 - first online pH monitor at 2 / 3 of 3.3 - Autotrophic denitrification unit. If the pH is lower than 6.7, the 3.3.5 - fourth feedback adjustment reagent dosing system is feedback-adjusted to control the pH in the pool The alkali-supplementing agent can be 30% liquid sodium hydroxide; 3.6-the first built-in sedimentation tank is set at the end 1 / 3 of the 3.3-autotrophic denitrification unit. The liquid in the tank enters through the 3.6.1-water collection port and flows into the 3.6.3-outlet through the 3.6.2-outlet weir and the outlet channel after sedimentation and separation, and flows out of the 3.3-autotrophic denitrification unit. The precipitated sludge flows into the 3.3.2-first sludge return pipe through the 3.6.4-sludge collection pipe. When the sludge concentration is too high, resulting in too high nitrite concentration in the effluent, part of the activated sludge is discharged through the 3.3.3-first residual sludge discharge pipe.

[0083] 3.6.2-3.9.1-First online ammonia nitrogen (NH4 + ) monitor and 3.10.1-First online nitrate nitrogen (NO3 - ) monitors monitor ammonia nitrogen and nitrate nitrogen in the effluent, respectively. If the ammonia nitrogen concentration exceeds 50 mg / L, first adjust the aeration rate in the online variable frequency aeration system (3.5) to ensure that the dissolved oxygen in the tank, as measured by the first online DO monitor (3.7.1), is between 0.6 and 0.8 mg / L. If the ammonia nitrogen concentration shows no downward trend, then adjust the system (3.3.4) to enhance the biological function within the tank and improve the system's denitrification capacity. If the calculated ratio of the generated nitrate nitrogen concentration to the removed ammonia nitrogen concentration is greater than 15%, discharge some activated sludge through the residual sludge discharge pipe (3.3.3).

[0084] The residence time of the 3.4-deep denitrification unit is 14 hours, and the volume ratio of the first aeration zone, the non-aeration zone and the second aeration zone is 3:3:1. The concentration of flocculent activated sludge in the pool is 3-4 g / L. The aeration volume is controlled online by the 3.5-variable frequency aeration system so that the dissolved oxygen in the pool detected by the 3.7.2-second online DO monitor and the 3.7.3-third online DO monitor are 0.5-0.8 mg / L and 0.1-0.5 mg / L respectively. If the 3.9.2-second online ammonia nitrogen (NH4 + ) The monitor detects that the ammonia nitrogen concentration in the effluent is greater than 5 mg / L. The aeration volume in the aeration zone is increased through the 3.5-variable frequency aeration system until the ammonia nitrogen concentration meets the standard; the 3.10.2-second online nitrate nitrogen (NO3- ) The nitrate-nitrogen concentration in the pool detected by the monitor is adjusted in real time to the 3.4.3 - Carbon Source Dosing System to ensure that the nitrate-nitrogen concentration is within the range of 5-30 mg / L (this range is the control range in this embodiment due to the total nitrogen requirements and cost considerations. If the concentration is to be lower than 5 mg / L or even completely removed, it is also possible, but the cost of the carbon source will increase dramatically); the liquid in the pool enters through the 3.6.1 - Water Collecting Port, undergoes sedimentation and separation, and then flows into the 3.6.2 - Outlet Weir and the Outlet Channel to flow out of the 3.4 - Deep Denitrification Unit at the 3.6.3 - Outlet. The precipitated sludge flows into the 3.4.1 - Second Sludge Return Pipe through the 3.6.4 - Sludge Collection Pipe. When the sludge concentration exceeds the set control range, it is discharged through the 3.4.2 - Second Residual Sludge Discharge Pipe.

[0085] The present invention collects wastewater from all sources and treats it together in a centralized manner, making full use of the properties of each wastewater to carry out mixed acid-base reactions, reducing the amount of reagents required for classified treatment, simplifying the treatment units and reducing operating operations. At the same time, it can regulate water quantity and quality, ensure the treatment effect of subsequent treatment process units, and change the removal of ammonia nitrogen from the physical and chemical stripping method to the anaerobic ammonia oxidation biological denitrification technology, thereby minimizing investment and operating costs.

[0086] Among biological denitrification technologies, the anaerobic ammonia oxidation process is currently recognized internationally as the most economical and efficient denitrification technology. Compared with traditional nitrification and denitrification, it saves 65% of aeration energy consumption and more than 90% of carbon source addition. It basically solves the problems of high energy consumption, high drug consumption and high sludge production caused by the traditional nitrification and denitrification process in the denitrification of high ammonia nitrogen wastewater. It can reduce operating costs, drug dosage and sludge production as much as possible. Therefore, the present invention uses a combined process based on anaerobic ammonia oxidation technology with stable and reliable treatment effect and good effluent water quality to achieve full-process treatment of chip wastewater.

[0087] This process is used to collect and treat chip wastewater in a unified manner throughout the entire process, with a total treatment scale of 500m 3 / d, 1-average water quality and water volume The main water quality characteristics of the wastewater in the pool and the water quality characteristics of the treated effluent are shown in the following table:

[0088]

[0089] While various embodiments of the present invention have been described above, the above description is intended to be illustrative, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A full-process treatment method for chip wastewater based on anaerobic ammonium oxidation, characterized in that: include: The water quality and quantity pool, physicochemical treatment unit, biochemical treatment unit and clear water pool are connected in sequence; The physicochemical treatment unit includes a first regulating tank, a fluorine removal unit, a second regulating tank and a hydrogen peroxide removal unit connected in sequence, the pH value of the first regulating tank is 7.5-8.5, the pH value of the second regulating tank is 10-11, the fluorine removal unit is provided with a calcium salt dosing system, and the hydrogen peroxide removal unit is provided with a manganese sand catalyst dosing system; The biochemical treatment unit includes a third regulating tank, an autotrophic denitrification unit, and a deep denitrification unit connected in sequence, wherein the pH value of the third regulating tank is 6.7-8.5, a solidified carrier is provided in the autotrophic denitrification unit, and the filling ratio of the solidified carrier is 5-15%, and the deep denitrification unit includes a first aeration zone, a non-aeration zone, and a second aeration zone with a volume ratio of 3:3:1, and the autotrophic denitrification unit and the second aeration zone are respectively provided with a first built-in sedimentation tank and a second built-in sedimentation tank; The water quality and quantity pool is filled with wastewater, wherein the wastewater includes fluorine-containing wastewater, hydrogen peroxide-containing wastewater, ammonia nitrogen-containing wastewater, acid wastewater, and alkaline wastewater; Adjust the sludge concentration of the flocculent activated sludge of the autotrophic denitrification unit to 2-5 g / L, adjust the inlet temperature to 28-30° C., the hydraulic retention time to 30-100 h, the dissolved oxygen to 0.1-0.8 mg / L, and the pH to 7.0-8.0 through a temperature control device; If the ammonia nitrogen concentration in the autotrophic denitrification unit is higher than 50 mg / L, the dissolved oxygen is adjusted to 0.6-0.8 mg / L through aeration, and / or hydroxylamine hydrochloride is added to the system for controlling the activity of the bacterial strain and regulating the addition of the agent; If the ratio of the concentration of nitrate nitrogen generated in the autotrophic denitrification unit to the concentration of ammonia nitrogen removed is greater than 15%, a portion of the activated sludge is discharged; Adjust the sludge concentration of the flocculent activated sludge in the deep denitrification unit to 2-5 g / L, the hydraulic retention time to 10-30 h, the dissolved oxygen in the first aeration zone to 0.5-1.0 mg / L, and the dissolved oxygen in the second aeration zone to 0.1-0.8 mg / L; The first aeration zone adjusts the carbon source addition according to the nitrate nitrogen concentration to make the nitrate nitrogen concentration within 5-30 mg / L; The second aeration zone controls the ammonia nitrogen concentration by aeration. If the ammonia nitrogen concentration of the effluent is greater than 5 mg / L, aeration is used to reduce the ammonia nitrogen concentration. The manganese sand catalyst dosing system is configured to remove 100 mg / L of hydrogen peroxide with 1 kg of manganese sand, and the content of manganese dioxide, an effective ingredient in the manganese sand, is greater than 40%; If the hydrogen peroxide removal efficiency is lower than 80%, backwashing should be performed, the amount of treated water should be reduced, or part of the manganese sand should be replaced.

2. A chip wastewater full-process treatment system based on anaerobic ammonium oxidation, used for the chip wastewater full-process treatment method based on anaerobic ammonium oxidation according to claim 1, characterized in that: include: The water quality and quantity pool, physicochemical treatment unit, biochemical treatment unit and clear water pool are connected in sequence; The physicochemical treatment unit includes a first regulating tank, a fluorine removal unit, a second regulating tank and a hydrogen peroxide removal unit connected in sequence, the fluorine removal unit is provided with a calcium salt dosing system, and the hydrogen peroxide removal unit is provided with a manganese sand catalyst dosing system; The biochemical treatment unit includes a third regulating tank, a temperature regulating device, an autotrophic denitrification unit and a deep denitrification unit connected in sequence, a solidified carrier is provided in the autotrophic denitrification unit, the deep denitrification unit includes a first aeration zone, a non-aeration zone and a second aeration zone with a volume ratio of 3:3:1, and the autotrophic denitrification unit and the second aeration zone are respectively provided with a first built-in sedimentation tank and a second built-in sedimentation tank; The first regulating tank is provided with a first online pH monitoring system and a first feedback regulating agent dosing system; The defluorination unit is provided with an online fluoride ion monitoring system and a calcium salt agent dosing system; The second regulating tank is provided with a second online pH monitoring system and a second feedback regulating agent dosing system; The hydrogen peroxide removal unit is provided with an online hydrogen peroxide monitoring system and a manganese sand catalyst dosing system; The third regulating tank is provided with a third online pH monitoring system and a third feedback regulating agent dosing system; The autotrophic denitrification unit is provided with a fourth online pH monitoring system, a fourth feedback regulating agent dosing system, a first online ammonia nitrogen monitor, a first online nitrate nitrogen monitor, a first online DO monitor and a first built-in sedimentation tank, wherein the first built-in sedimentation tank is arranged at the tail end of the autotrophic denitrification unit and is connected to the head end of the autotrophic denitrification unit through a first sludge return pipe; The first aeration zone is provided with a second online nitrate nitrogen monitor and a second online DO monitor; The non-aeration zone is provided with a carbon source addition system; The second aeration zone is provided with a second online ammonia nitrogen monitor and a third online DO monitor.

3. A chip wastewater full-process treatment system based on anaerobic ammonium oxidation according to claim 2, characterized in that: The first online DO monitor is arranged at the head end of the autotrophic denitrification unit, and the first online ammonia nitrogen monitor and the first online nitrate nitrogen monitor are arranged at the tail end of the autotrophic denitrification unit, located in the outlet channel of the first built-in sedimentation tank.

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