Device and method for realizing anaerobic ammonia oxidation denitrification of high-temperature wastewater based on up-flow anaerobic sludge blanket reactor
By acclimating thermophilic anammox sludge in an upflow anammox sludge bed reactor, the problems of poor sludge adaptability, low efficiency, and high cost in high-temperature wastewater denitrification technology have been solved, achieving efficient and stable high-temperature wastewater denitrification and reducing energy consumption and costs.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2026-03-09
- Publication Date
- 2026-04-14
AI Technical Summary
Existing high-temperature wastewater denitrification technologies suffer from poor sludge adaptability, low denitrification efficiency, high cost, and inhibited microbial metabolic activity under high-temperature conditions, making it difficult to maintain process stability, resulting in low mass transfer efficiency, limited material selection, and high energy consumption.
Fresh hot spring sediments were used as inoculum to acclimate thermophilic anammox sludge in an upflow anammox sludge bed reactor. Through gradient temperature increase and acclimatization, anammox denitrification of high-temperature wastewater was achieved. The acclimatized sludge was used to operate stably in the range of 45-65 ℃, and the process design and material selection were optimized.
It achieves efficient nitrogen removal at 45-65 ℃, with a total nitrogen removal rate of 606.1-592.2 mg N L-1·d-1, low NH4+-N and NO2--N concentrations in the effluent, good operational stability, reduced energy consumption by 3.0-5.0 kWh/kg-N, and 100% cost reduction, thus expanding the temperature range for high-temperature wastewater treatment.
Smart Images
Figure CN121850192A_ABST
Abstract
Description
Technical Field
[0001] This invention belongs to the field of wastewater biological denitrification technology, specifically relating to a device and method for achieving high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor. Background Technology
[0002] With the continuous expansion of industrial production and the accelerating pace of urbanization, large quantities of wastewater with significantly high temperatures are being discharged from industrial settings such as food processing, geothermal power generation systems, and high-temperature sludge digestion facilities. This type of high-temperature wastewater typically exceeds 40°C and contains high levels of NH4+. + -N pollutant concentrations are extremely high, generally ranging from 200 to 1000 mg NL. -1 If discharged directly into natural water bodies without proper treatment, it will not only cause excessive accumulation of nutrients in the water, leading to a series of ecological problems such as algal blooms and eutrophication, but will also seriously damage the stability and biodiversity of aquatic ecosystems.
[0003] In recent years, researchers have discovered and confirmed the existence of multiple microbial nitrogen transformation pathways, including anaerobic ammonium oxidation, nitrification, and denitrification, in various high-temperature natural ecological environments—such as geothermal hot springs and deep-sea hydrothermal vent areas with temperatures ranging from 50 to 90 °C. These findings indicate that high-temperature biological nitrogen removal technology, with anaerobic ammonium oxidation as its core mechanism, has the potential for practical application in treating high-temperature industrial wastewater. However, many challenges remain in truly promoting such processes to engineering applications: high temperatures significantly inhibit microbial metabolic activity, affecting microbial domestication and functional expression; simultaneously, the stability of process operation is difficult to maintain under high-temperature conditions, and the system's ability to withstand load fluctuations decreases; furthermore, high temperatures limit the selection of reactor materials—common metals are easily corroded more quickly, often necessitating the use of expensive materials such as titanium alloys or special ceramic coatings, increasing construction costs by 2 to 3 times. High temperatures also reduce dissolved oxygen concentration in water, requiring aerobic processes to increase aeration rates, leading to increased energy consumption and decreased mass transfer efficiency.
[0004] Therefore, there is an urgent need to develop a series of cutting-edge technologies for the efficient denitrification treatment of high-temperature wastewater, including screening and cultivating heat-resistant functional microorganisms, optimizing high-temperature adaptability process design, promoting the coupling and integration of multiple processes, and exploring ways to recover waste heat and utilize resources, so as to achieve simultaneous improvement in treatment efficiency and economic benefits. Summary of the Invention
[0005] The purpose of this invention is to overcome the shortcomings of existing high-temperature wastewater denitrification technologies, such as poor sludge adaptability, low denitrification efficiency, and high cost, and to provide a high-efficiency denitrification technology based on high-temperature anaerobic ammonia oxidation.
[0006] To achieve the above objectives, this invention uses fresh natural hot spring sediment as inoculum, which is acclimated and cultivated in an upflow anaerobic sludge bed reactor. The thermophilic anaerobic ammonia oxidation sludge obtained through this acclimation and cultivation is then used for efficient denitrification of high-temperature wastewater. The technical solution for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor described in this invention is implemented as follows:
[0007] The present invention provides a device for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor. The device includes an inlet tank, an inlet pump, a reactor body, a circulation pump, a pH meter, a water seal device, a three-phase separator, a constant temperature water bath, an inlet, and an outlet.
[0008] The top and middle of the reactor body are cylindrical, with the top diameter being larger than the middle diameter. The connection between the top and middle of the reactor body is an inverted frustum shape, and the bottom of the reactor body is conical.
[0009] The reactor body is divided into two layers: the inner layer is the sludge reactor zone, and the outer layer is the water bath heating zone connected to the constant temperature water bath.
[0010] The reactor body has an inlet at the bottom, which is connected to a liquid inlet pump via a pipeline. The liquid inlet pump is connected to a liquid inlet tank. A three-phase separator is located at the top of the reactor body. The three-phase separator is connected to a water seal device via a pipeline. The water seal device has an air outlet. A water outlet is located on the top side wall. The water outlet is connected to a pH meter via a pipeline and to a circulation pump. The outlet of the circulation pump is connected to the inlet at the bottom of the reactor body.
[0011] The three-phase separator is placed on top of the reactor body and is connected to the water outlet and gas outlet at the top of the reactor body.
[0012] Furthermore, the upper side wall of the reactor body is provided with a gas sample collection port, and the lower side wall is provided with a water sample collection port.
[0013] Furthermore, the total volume of the reactor is set to 2000~4000 mL.
[0014] Method of using the apparatus of the present invention, which is based on an upflow anaerobic sludge bed reactor for high-temperature wastewater anaerobic ammonia oxidation denitrification:
[0015] Step 1: Collect hot spring sediment as inoculum and mix it with synthetic culture medium to form a homogeneous mud. Filter the mud to remove large particulate impurities and obtain filtered hot spring sediment.
[0016] Step 2: Add filtered hot spring sediment and fresh synthetic culture medium to the reactor body, respectively, and acclimatize it in the dark. Aerate the reactor body thoroughly with an argon-mixed gas to ensure an anaerobic environment. Control the operating temperature of the reactor body at 44-46 ℃ and maintain the pH at 7.2-7.8, then add the synthetic culture medium.
[0017] Step 3: During the 0-64 day operation of the main reactor, manually add NH4 in batches. + -N and NO2 - -N concentrate;
[0018] During reactor operation for 65–177 days, NH4 was supplied using a continuous flow feed method. + -N and NO2 - -N concentrate, and adjust the influent load to 126.0~154.0 mg NO2. - -NL -1 ·d -1 and 95.0~105.0 mg NH4 + -NL -1 ·d -1 The HRT is 14-16 days. During days 92-176, the influent load is increased by 189.0-231.0 mg NO2. - -NL -1 ·d -1 and 95.0~105.0 mg NH4 + -NL -1 ·d -1 HRT is 10-12 days;
[0019] During reactor operation for 177-530 days, the influent load was increased by 1070.0~1312.0 mg NO2. - -NL -1 ·d -1 and 812.0~994.0 mg NH4 + -NL -1 ·d -1 The initial HRT was 104-108 days; during later stages of operation, the HRT was gradually shortened, decreasing to 5-6 days from day 474 until NH4 + -N and NO2 - -N metabolism rate and substrate consumption have reached a stable state, thus successfully domesticating thermophilic anaerobic ammonia oxidizing bacteria and realizing a stable denitrification process of anaerobic ammonia oxidation under high temperature conditions.
[0020] The synthetic culture medium is composed of 0.07~0.08 g·L⁻¹. -1KH2PO4, 0.2~0.4 g·L -1 CaCl2·2H2O, 0.1~0.2 g·L -1 MgCl2·6H2O, 0.2~0.3 g·L -1 KHCO3, 0.7~0.9 g·L -1 NaHCO3, 0.4~0.6 mL·L -1 Acidic trace element solution and 0.2 mL·L -1 Composition of alkaline trace element solution.
[0021] Furthermore, the aforementioned up to NH4 + -N and NO2 - -N metabolic rate, substrate consumption reaching a steady state refers to NH4+ metabolism rate. + -N and NO2 - -N metabolic rates reached 143.0–173.0 mg NH4. + -NL -1 ·d -1 and 181.0~222.0 mg NO2 - -NL -1 ·d -1 NO2 - -N and NH4 + The -N molar ratio was maintained at 1.27~1.29.
[0022] Furthermore, the acidic trace element solution is composed of 100 mM HCl and 5~6 g·L⁻¹. -1 FeSO4·7H2O, 0.06~0.07 g·L -1 ZnSO4·7H2O, 0.1~0.2 g·L -1 CoCl2·6H2O, 0.4~0.6 g·L -1 MnCl2·4H2O, 1.5~1.7 g·L -1 CuSO4, 0.09~0.10 g·L -1 NiCl2·6H2O and 0.01~0.02 g·L -1 The alkaline trace element solution is composed of 10 mM NaOH and 0.06~0.07 g·L⁻¹. -1 SeO2, 0.04~0.06 g·L -1 Na₂WO₄·2H₂O, 0.2~0.3 g·L -1 Composition: Na2MoO4.
[0023] Furthermore, the hot spring deposits are from hot springs where the natural water temperature is maintained at 45~49 ℃ all year round.
[0024] An apparatus and method for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to the present invention:
[0025] Step 1: Collect hot spring sediment as inoculum and mix it with synthetic culture medium to form a homogeneous mud. Filter the mud to remove large particulate impurities and obtain filtered hot spring sediment.
[0026] Step 2: Add filtered hot spring sediment and fresh synthetic culture medium to the reactor body, acclimatize and cultivate it in the dark, and fully aerate the reactor body with argon gas mixture to ensure the anaerobic environment of the reactor body; control the operating temperature of the reactor body at 53~57 ℃ and maintain the pH at 7.2~7.8, and then add synthetic culture medium;
[0027] Step 3: During the 0-94 day operation of the main reactor, manually add NH4 in batches. + -N and NO2 - -N concentrate;
[0028] During reactor operation, NH4 was supplied using a continuous flow feed method for 97–296 days. + -N and NO2 - -N concentrate, and adjust the influent load to 282.0~315.0 mg NO2. - -NL -1 ·d -1 and 214.0~261.0 mg NH4 + -NL -1 ·d -1 HRT is 107-111 days;
[0029] During reactor operation for 297-490 days, the influent load was increased by 1710.0~1890.0 mg NO2. - -NL -1 ·d -1 and 1583~1750mg NH4 + -NL -1 ·d -1 The initial HRT (Heat Retention Time) is 107-111 days; after 306 days, the HRT is gradually shortened, until 406 days when the HRT is reduced to 8-9 days, until NH4 + -N and NO2 - -N metabolic rate, substrate consumption enters a steady state, thus successfully domesticating thermophilic anaerobic ammonia oxidizing bacteria and realizing a stable anaerobic ammonia oxidation denitrification process under high temperature conditions;
[0030] The synthetic culture medium is composed of 0.07~0.08 g·L⁻¹. -1 KH2PO4, 0.2~0.4 g·L -1 CaCl2·2H2O, 0.1~0.2 g·L -1 MgCl2·6H2O, 0.2~0.3 g·L -1 KHCO3, 0.7~0.9 g·L -1 NaHCO3, 0.4~0.6 mL·L -1 Acidic trace element solution and 0.2~0.3 mL·L -1 Composition of alkaline trace element solution.
[0031] Furthermore, the acidic trace element solution is composed of 100 mM HCl and 5~6 g·L⁻¹. -1 FeSO4·7H2O, 0.06~0.07 g·L -1 ZnSO4·7H2O, 0.1~0.2 g·L -1 CoCl2·6H2O, 0.4~0.6 g·L -1 MnCl2·4H2O, 1.5~1.7 g·L -1 CuSO4, 0.09~0.10 g·L -1 NiCl2·6H2O and 0.01~0.02 g·L -1 The alkaline trace element solution is composed of 10 mM NaOH and 0.06~0.07 g·L⁻¹. -1 SeO2, 0.04~0.06 g·L -1 Na₂WO₄·2H₂O, 0.2~0.3 g·L -1 Composition: Na2MoO4.
[0032] Furthermore, the hot spring sediments were collected from wild hot springs where the natural water temperature remains at 55-60 ℃ year-round.
[0033] The beneficial effects of this invention are as follows:
[0034] (a) Excellent nitrogen removal performance. When treating high-temperature wastewater at 45 °C and 55 °C, the total nitrogen removal rate reached 606.1 mg NL, respectively. -1 ·d -1 and 592.2 mg NL -1 ·d -1 NH4 in the effluent + -N and NO2 --N concentrations remained stable between 1.0 and 15.0 mg NH4. + -NL -1 ·d -1 and 1.0~2.0 mg NO2 - -NL -1 ·d -1 It meets the "Integrated Wastewater Discharge Standard" (NH4). + -N ≤ 15 mg NL -1 Stable denitrification of high-temperature wastewater at 55~65 ℃ can be achieved through gradient heating, expanding the application temperature range.
[0035] (b) Good operational stability. The thermophilic anammox sludge acclimated by the present invention has strong adaptability to temperature fluctuations and substrate load shocks. There is no sludge disintegration during the gradient heating process. It can quickly recover stable denitrification after each increase in substrate load, thus solving the stability defects of mesophilic sludge acclimation technology.
[0036] (c) Energy and cost reduction. The anaerobic ammonia oxidation sludge acclimated by this invention can operate stably at 45-65 ℃ directly without complex temperature acclimation and control, simplifying the process control flow and reducing the energy consumption of the temperature control system; no external carbon source or acid-base neutralization reagent is required, reducing operating costs. Compared with the traditional nitrification-denitrification process, energy consumption can be reduced by 3.0~5.0 kWh / kg-N, and carbon source cost is reduced by 100%.
[0037] In summary, this invention successfully domesticated thermophilic anaerobic ammonia oxidation sludge, achieving a stable denitrification process under high-temperature conditions, filling the resource gap in thermophilic anaerobic ammonia oxidation functional microorganisms. The constructed high-temperature denitrification device and process eliminate the need for cooling of high-temperature wastewater and the addition of additional carbon sources, achieving cost reduction, energy saving, and carbon reduction in high-temperature wastewater treatment from a technical perspective. It solves the problems of high energy consumption, high cost, and high risk of secondary pollution associated with traditional processes. This provides a novel technical approach for high-temperature wastewater treatment in fields such as food processing, geothermal power generation, and sludge digestion. Attached Figure Description
[0038] Figure 1 This is a schematic diagram of the acclimation method of thermophilic anammox sludge and the structure of the upflow anammox sludge bed reactor for implementing the method according to the present invention; in the figure, there is an inlet tank 1, an inlet pump 2, a reactor body 3, a circulation pump 4, a pH meter 5, a water seal device 6, a three-phase separator 7, a constant temperature water bath 8, an inlet 9, and an outlet 10. Detailed Implementation
[0039] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the spirit of the contents disclosed in the present invention will be described in detail below. After understanding the embodiments of the present invention, any person skilled in the art can make changes and modifications based on the technology taught in the present invention without departing from the spirit and scope of the present invention.
[0040] The illustrative embodiments and descriptions of the present invention are used to explain the present invention, but are not intended to limit the present invention.
[0041] Example 1
[0042] Combination Figure 1 This embodiment describes a thermophilic anammox sludge acclimation method. The method utilizes an upflow anammox sludge bed reactor (UASB reactor body 3), a circulating pump 4, a pH meter 5, a water seal device 6, a three-phase separator 7, a constant temperature water bath 8, an inlet tank 1, an inlet pump 2, an inlet 9, and an outlet 10.
[0043] The liquid inlet tank 1 is connected to the liquid inlet pump 2 through a pipeline. The liquid inlet pump 2 transports the liquid in the liquid inlet tank 1 to the bottom inlet 9 of the UASB reactor 3 through a pipeline.
[0044] The liquid in the UASB reactor body 3 is connected to the circulation pump 4 through a pipe, and the circulation pump 4 sends the liquid back to the UASB reactor 3 through a pipe, forming a circulation loop. The pH meter 5 is connected to the pipe between the circulation pump 4 and the outlet 10 at the top of the UASB reactor body 3.
[0045] The top of the UASB reactor body 3 is connected to the water seal device 6 through a pipe. The water seal device 6 can collect the biogas produced by the UASB reactor body 3. The water seal device 6 is then connected to the gas outlet of the three-phase separator 7 through a pipe.
[0046] The water bath device 8 is connected to the outer layer of the UASB reactor body 3 via a pipe and is used to control the temperature inside the UASB reactor body 3.
[0047] Example 2
[0048] An anaerobic ammonia oxidation denitrification system for high-temperature wastewater at 45°C was constructed based on the apparatus of Example 1.
[0049] (a) Preparation of inoculum sludge. Sediment samples were collected from a wild hot spring (29°N; 100°E) in Gaocheng City, Sichuan Province, China, as inoculum for sludge inoculation at 45°C. The natural temperature of the hot spring is maintained at around 47°C year-round. The distance between the surface layer of the collected sediment and the surface water surface was approximately 40 cm. The collected samples were sediments less than 10 cm thick from the surface. The freshly collected sediment was mixed with synthetic culture medium to form a homogeneous slurry. The slurry was filtered using filters of different mesh sizes to remove large particles before being transferred to a reactor for acclimatization and cultivation.
[0050] (b) Reactor operating conditions. To achieve stable operation of anaerobic ammonia oxidation denitrification in 45 ℃ high-temperature wastewater, 500 mL of filtered hot spring sediment and 2500 mL of synthetic culture medium were added to the UASB reactor. The reactor was wrapped with a black light-blocking cloth to prevent light exposure during cultivation, and a mixture of argon gas was used to fully aerate the reactor for 30 min to ensure a strictly anaerobic environment. The reactor operating temperature was controlled at 45 ± 1 ℃, while the pH was maintained at 7.5 ± 0.3. Subsequently, synthetic culture medium was added, and the reactor was started up at 45 ℃.
[0051] (c) During the initial operation of the reactor (0-64 days), NH4 is manually added in batches. + -N and NO2 - -N concentrate provides substrate while avoiding excessive biomass loss and microbial activity inhibition caused by high substrate concentration. Initially, the NH4+ in the reactor effluent... + -N concentration gradually increases, then begins a slow decline starting on day 32, reaching a peak on day 64. - -N and NH4 + The metabolic rate of -N reached 4.4 mg NO2. - -NL -1 ·d -1 and 1.8 mg NH4 + -NL -1 ·d -1 The reactor operated in Phase II (days 65-177), with NH4 supplied via continuous flow from day 65 onwards. + -N and NO2 - -N concentrate, influent load is 140.0 mg NO2 - -NL -1 ·d -1 and 106.0 mg NH4 + -NL -1 ·d -1The HRT is 15.1 days. From day 92 to 176, the influent load is increased (210.0 mg NO2). - -NL -1 ·d -1 and 106.0 mg NH4 + -NL -1 ·d -1 Simultaneously, the HRT was gradually shortened to 11.8 days to further rapidly enhance the anaerobic ammonia oxidation activity within the culture system, NH4+. + -N and NO2 - The metabolic rate of -N increases to approximately 5.0 mg NH4. + -NL -1 ·d -1 and 17.0 mg NO2 - -NL -1 ·d -1 The total nitrogen metabolism rate increased by approximately 22.9%. During reactor operation in Phase III (days 177-530), the influent load was further increased (1192.2 mg NO2). - -NL -1 ·d -1 and 903.2 mg NH4 + -NL -1 ·d -1 The HRT was extended to 106.0 days to reduce biomass loss and maintain a stable total nitrogen loading rate during the transition between the two phases. As the microorganisms gradually adapted to the high influent concentration and high HRT, the HRT was gradually shortened during subsequent long-term operation to provide sufficient substrate for the microorganisms in the culture reactor. From day 474, the HRT was shortened to 5.9 days, and finally from day 494, NH4+ was reduced. + -N and NO2 - The metabolic rate of -N reached 158.0 mg NH4. + -NL -1 ·d -1 and 202.0 mg NO2 - -NL -1 ·d -1 The molar ratio of substrate consumed (NO2) - -N / NH4 + The nitrogen content (N) was maintained at 1.28, reaching a stable state, and the stable operation of the anaerobic ammonia oxidation denitrification process in wastewater under high temperature conditions of 45 ℃ was successfully achieved.
[0052] Example 3
[0053] An anaerobic ammonia oxidation denitrification system for high-temperature wastewater at 55°C was constructed based on the apparatus of Example 1.
[0054] (a) Preparation of inoculum sludge. Sediments from a wild hot spring (21.36°N; 98.63°E) in Tengchong City, Yunnan Province, China, were collected as inoculum for inoculation at 55°C. The natural temperature of the hot spring is maintained at approximately 55-60°C year-round. The distance between the surface layer of the collected sediment and the surface water surface was approximately 37 cm. The collected samples were the sediments less than 10 cm deep from the surface layer, and the processing method was the same as in Scheme 1.
[0055] (b) Reactor operating conditions. To achieve stable operation of anaerobic ammonia oxidation denitrification in high-temperature wastewater at 55°C, 500 mL of filtered hot spring sediment and 2500 mL of synthetic culture medium were added to the UASB reactor. The reactor was wrapped with a black light-blocking cloth to prevent light exposure during cultivation, and a mixture of argon gas was used to fully aerate the reactor for 30 min to ensure a strictly anaerobic environment. The reactor operating temperature was controlled at 55 ± 2°C, and the pH was maintained at 7.4 ± 0.2 by manually adding 1 M HCl solution. Subsequently, synthetic culture medium (the same as in Example 2) was added, and the reactor was started at 55°C.
[0056] (c) During reactor operation phase I (days 0-94), NH4 is manually added in batches according to the consumption within the reactor. + -N and NO2 - -N concentrate, to avoid excessive accumulation, NH4 in the effluent after 45 days. + -N concentration increases with NO2 - The -N content gradually decreases with the addition of -N, while NO3... - -N began to gradually accumulate in the effluent. By day 94, the culture reactor was nearing stable operation, and NO2... - -N and NH4 + The metabolic rate of -N was 0.5 mg NO2. - -NL -1 ·d -1 and 0.3 mg NH4 + -NL -1 ·d -1 The reactor operated in Phase II (days 97-296), switching to continuous substrate supply mode from day 97 onwards, with an influent load of 314.4 mg NO2. - -NL -1 ·d -1 and 238.2 mg NH4 + -NL -1·d -1 The initial HRT was 109.2 days to rapidly increase the anaerobic ammonia oxidation activity in the culture system, after which the HRT was gradually shortened to 18.2 days, finally reaching the end of the second stage, where NO2... - -N and NH4 + The metabolic rate of -N reached 11.0 mg NO2. - -NL -1 ·d -1 and 8 mg NH4 + -NL -1 ·d -1 The substrate consumption molar ratio (NO2) of this reactor - -N / NH4 + The NO3- (-N) value was 1.38. NO3 was observed in the effluent. - -N concentration gradually accumulated with increasing substrate metabolic rate, indicating that the high-temperature anaerobic ammonia oxidation process within the reactor was gradually increasing. During reactor operation phase III (days 297-490), the influent load was further increased (1800.0 mg NO2). - -NL -1 ·d -1 and 1666.7 mg NH4 + -NL -1 ·d -1 The HRT was subsequently extended to 109.2 days to prevent excessive sludge loss and maintain a stable substrate influent load during the transition between the two phases. After 306 days, the HRT was gradually shortened, and from day 466 onwards, it was reduced to 8.4 days. NH4 + -N and NO2 - The metabolic rate of -N reached 198.0 mg NH4. + -NL -1 ·d -1 and 214.0 mg NO2 - -NL -1 ·d -1 Stable operation of the anaerobic ammonia oxidation denitrification process in wastewater was successfully achieved under high temperature conditions of 55 ℃.
Claims
1. A device for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge blanket reactor, characterized in that, The device includes an inlet tank (1), an inlet pump (2), a reactor body (3), a circulation pump (4), a pH meter (5), a water seal device (6), a three-phase separator (7), a constant temperature water bath (8), an inlet (9), and an outlet (10). The top and middle of the reactor body (3) are cylindrical, and the diameter of the top is larger than the diameter of the middle of the reactor body. The connection between the top of the reactor body (3) and the middle of the reactor body is an inverted frustum shape, and the bottom of the reactor body (3) is conical. The reactor body (3) is divided into two layers, an inner layer and an outer layer. The inner layer is the sludge reactor area, and the outer layer is the water bath heating area and is connected to the constant temperature water bath (8). The reactor body (3) has an inlet (9) at the bottom and is connected to the liquid inlet pump (2) through a pipeline. The liquid inlet pump (2) is connected to the liquid inlet tank (1). The reactor body (3) has a three-phase separator (7) at the top. The three-phase separator (7) is connected to the water seal device (6) through a pipeline. The water seal device (6) has an air outlet. The top side wall has an outlet (10). The outlet (10) is connected to the pH meter (5) through a pipeline and is connected to the circulation pump (4). The outlet of the circulation pump (4) is connected to the inlet (9) at the bottom of the reactor body (3). The three-phase separator (7) is placed on top of the reactor body (3) and is connected to the water outlet and gas outlet at the top of the reactor body (3).
2. The apparatus for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to claim 1, characterized in that, The upper side wall of the reactor body (3) is provided with a gas sample collection port, and the lower side wall is provided with a water sample collection port.
3. The apparatus for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to claim 1, characterized in that, The total volume of the reactor is set to 2000~4000 mL.
4. A method of using the apparatus for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor as described in claim 1, characterized in that, It is done according to the following steps: Step 1: Collect hot spring sediment as inoculum and mix it with synthetic culture medium to form a homogeneous mud. Filter the mud to remove large particulate impurities and obtain filtered hot spring sediment. Step 2: Add filtered hot spring sediment and fresh synthetic culture medium to the reactor body (3), and acclimatize it in the dark. Aerate the reactor body (3) with an argon mixture to ensure an anaerobic environment. Control the operating temperature of the reactor body (3) at 44~46 ℃ and maintain the pH at 7.2~7.
8. Then add the synthetic culture medium. Step 3: During the operation of the reactor body (3) for 0-64 days, manually add NH4 in batches. + -N and NO2 - -N concentrate; During reactor operation for 65–177 days, NH4 was supplied using a continuous flow feed method. + -N and NO2 - -N concentrate, and adjust the influent load to 126.0~154.0 mg NO2. - -NL -1 ·d -1 and 95.0~105.0 mg NH4 + -NL -1 ·d -1 The HRT is 14-16 days. During days 92-176, the influent load is increased by 189.0-231.0 mg NO2. - -NL -1 ·d -1 and 95.0~105.0 mg NH4 + -NL -1 ·d -1 HRT is 10-12 days; During reactor operation for 177-530 days, the influent load was increased by 1070.0~1312.0 mg NO2. - -NL -1 ·d -1 and 812.0~994.0 mg NH4 + -NL -1 ·d -1 The initial HRT was 104-108 days; during later stages of operation, the HRT was gradually shortened, decreasing to 5-6 days from day 474 until NH4 + -N and NO2 - -N metabolism rate and substrate consumption have reached a stable state, thus successfully domesticating thermophilic anaerobic ammonia oxidizing bacteria and realizing a stable denitrification process of anaerobic ammonia oxidation under high temperature conditions. The synthetic culture medium is composed of 0.07~0.08 g·L⁻¹. -1 KH2PO4, 0.2~0.4 g·L -1 CaCl2·2H2O, 0.1~0.2 g·L -1 MgCl2·6H2O, 0.2~0.3 g·L -1 KHCO3, 0.7~0.9 g·L -1 NaHCO3, 0.4~0.6 mL·L -1 Acidic trace element solution and 0.2 mL·L -1 Composition of alkaline trace element solution.
5. The method of using the device for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to claim 4, characterized in that, The term up to NH4 + -N and NO2 - -N metabolic rate and substrate consumption reach a steady state when NH4+ + -N and NO2 - -N metabolic rates reached 143.0–173.0 mg NH4. + -NL -1 ·d -1 and 181.0~222.0 mg NO2 - -NL -1 ·d -1 NO2 - -N and NH4 + The -N molar ratio was maintained at 1.27~1.
29.
6. The method of using the device for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to claim 4, characterized in that, The acidic trace element solution is composed of 100 mM HCl and 5~6 g·L⁻¹. -1 FeSO4·7H2O, 0.06~0.07 g·L -1 ZnSO4·7H2O, 0.1~0.2 g·L -1 CoCl2·6H2O, 0.4~0.6 g·L -1 MnCl2·4H2O, 1.5~1.7 g·L -1 CuSO4, 0.09~0.10 g·L -1 NiCl2·6H2O and 0.01~0.02 g·L -1 The alkaline trace element solution is composed of 10 mM NaOH and 0.06~0.07 g·L⁻¹. -1 SeO2, 0.04~0.06 g·L -1 Na₂WO₄·2H₂O, 0.2~0.3 g·L -1 Composition: Na2MoO4.
7. The method of using the device for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to claim 4, characterized in that, The hot spring deposits mentioned above come from hot springs where the natural water temperature is maintained at 45~49℃ all year round.
8. A method for using the apparatus for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor as described in claim 1, characterized in that, The method is as follows: Step 1: Collect hot spring sediment as inoculum and mix it with synthetic culture medium to form a homogeneous mud. Filter the mud to remove large particulate impurities and obtain filtered hot spring sediment. Step 2: Add filtered hot spring sediment and fresh synthetic culture medium to the reactor body (3), acclimatize and cultivate in the dark, and fully aerate the reactor body (3) with argon gas mixture to ensure the anaerobic environment of the reactor body (3); control the operating temperature of the reactor body (3) at 53~57 ℃ and the pH at 7.2~7.8, and then add synthetic culture medium; Step 3: During the operation of the reactor body (3) for 0-94 days, manually add NH4 in batches. + -N and NO2 - -N concentrate; During reactor operation, NH4 was supplied using a continuous flow feed method for 97–296 days. + -N and NO2 - -N concentrate, and adjust the influent load to 282.0~315.0 mg NO2. - -NL -1 ·d -1 and 214.0~261.0 mg NH4 + -NL -1 ·d -1 HRT is 107-111 days; During reactor operation for 297-490 days, the influent load was increased by 1710.0~1890.0 mg NO2. - -NL -1 ·d -1 and 1583.0~1750.0 mg NH4 + -NL -1 ·d -1 The initial HRT (Heat Retention Time) is 107-111 days; after 306 days, the HRT is gradually shortened, until 406 days when the HRT is reduced to 8-9 days, until NH4 + -N and NO2 - -N metabolism rate and substrate consumption have reached a stable state, thus successfully domesticating thermophilic anaerobic ammonia oxidizing bacteria and realizing a stable denitrification process of anaerobic ammonia oxidation under high temperature conditions; The synthetic culture medium is composed of 0.07~0.08 g·L⁻¹. -1 KH2PO4, 0.2~0.4 g·L -1 CaCl2·2H2O, 0.1~0.2 g·L -1 MgCl2·6H2O, 0.2~0.3 g·L -1 KHCO3, 0.7~0.9 g·L -1 NaHCO3, 0.4~0.6 mL·L -1 Acidic trace element solution and 0.2~0.3 mL·L -1 Composition of alkaline trace element solution.
9. The method of using the device for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to claim 7, characterized in that, The acidic trace element solution is composed of 100 mM HCl and 5~6 g·L⁻¹. -1 FeSO4·7H2O, 0.06~0.07 g·L -1 ZnSO4·7H2O, 0.1~0.2 g·L -1 CoCl2·6H2O, 0.4~0.6 g·L -1 MnCl2·4H2O, 1.5~1.7 g·L -1 CuSO4, 0.09~0.10 g·L -1 NiCl2·6H2O and 0.01~0.02 g·L -1 The alkaline trace element solution is composed of 10 mM NaOH and 0.06~0.07 g·L⁻¹. -1 SeO2, 0.04~0.06 g·L -1 Na₂WO₄·2H₂O, 0.2~0.3 g·L -1 Composition: Na2MoO4.
10. The method of using the device for high-temperature wastewater anaerobic ammonia oxidation denitrification based on an upflow anaerobic sludge bed reactor according to claim 7, characterized in that, The hot spring sediments were collected from wild hot springs where the natural water temperature remains at 55-60℃ year-round.