A sulfate-type anaerobic ammonium oxidation power generation device and control method thereof

Abstract

A sulfate-type anaerobic ammonium oxidation power generation device and control method, belonging to the technical field of sewage treatment. The power generation device utilizes a UASB anaerobic reactor, which is sequentially connected to an aerobic tank, an anoxic tank, and a final sedimentation tank. A sulfate-type anaerobic ammonium oxidation reaction suitable for aged landfill leachate is initiated in the UASB anaerobic reactor. The UASB anaerobic reactor is separated from the aerobic tank and the anoxic tank by a proton exchange membrane, and then is externally connected to a resistance box through a carbon felt electrode enriched with a large amount of microorganisms and a copper wire to form a closed loop, constituting a two-chamber microbial fuel cell. The inventive device can simultaneously remove high-concentration SO4 2‑ , NH4 + in aged landfill leachate and improve the power generation efficiency of the microbial fuel cell, and can effectively solve the problems of low denitrification and desulfurization efficiency, high operation energy consumption, large floor area, and high sludge production in the existing process.

Description

Technical Field

[0001] The present invention belongs to the technical field of sewage treatment, and in particular to a sulfate-type anaerobic ammonium oxidation power generation device and a control method thereof, which utilizes a UASB anaerobic reactor to simultaneously remove high-concentration SO4 in old garbage leachate. 2 -, NH4+ and improve the efficiency of electricity generation in microbial fuel cells. Background Art

[0002] With the continuous development of industry, some SO4 2 -, NH4+ wastewater discharged into the water body poses a threat to the environment. 2 -, NH4+, etc. The treatment of various types of sewage mainly adopts biological treatment measures, such as old garbage leachate. This type of sewage has complex components, not only containing organic pollutants, but also containing metal ions and other toxic and harmful pollutants, SO4 2 -, high NH4+ content, serious imbalance of carbon-nitrogen ratio, low COD content, and extremely poor biodegradability make it more difficult to choose conventional treatment processes. 2 -, NH4+ The treatment of old landfill leachate generally adopts biological method, which is carried out in steps of denitrification and then desulfurization. Although a single process or a chaotic combination of multiple processes can solve the problem, there are generally problems such as complex process, poor stability, large land occupation, high wastewater treatment cost, and substandard effluent.

[0003] Treatment of such high concentrations of SO4 2 -, NH4+, and aged landfill leachate urgently need more effective and feasible process methods. Sulfate-type anaerobic ammonium oxidation is a new technology that can achieve SO4 in a reactor. 2 - and NH4+ are removed simultaneously, with a high removal capacity, and the intermediate products can be used for reaction to reduce the pressure for subsequent treatment, and no external organic carbon source is required, saving costs.

[0004] However, research on sulfate anaerobic ammonium oxidation is still in its early stages, and a quick and effective startup method has not yet been found. The current startup method is to first realize the nitrite anaerobic ammonium oxidation reaction, and then gradually convert it to the sulfate anaerobic ammonium oxidation reaction. However, the nitrite anaerobic ammonium oxidation process itself has problems such as long startup time. Secondly, there is a lack of understanding of the changes in the microbial community structure during the startup of the sulfate anaerobic ammonium oxidation reaction, and there is no reasonable explanation at the microbial level. Therefore, exploring rapid startup methods and microbial community characteristics is of great significance to promoting the engineering application of sulfate anaerobic ammonium oxidation.

[0005] Studies have found that in anaerobic ammonium oxidation reactors containing fillers, some fillers may provide a micro-electricity environment for microorganisms, and confirmed that the extracellular electron transfer of some electrogenic microorganisms in anaerobic ammonium oxidation reactors provides a possible conversion pathway for sulfate-type anaerobic ammonium oxidation. Microbial fuel cells are one of the new technologies that organically combine solving environmental pollution problems with producing new energy sources. It is a device that uses microorganisms as biocatalysts to convert organic matter that pollutes the environment into electrical energy. It can use various sewage as raw materials and can produce clean energy. It has the advantages of diversified fuel sources, no pollution, high energy utilization efficiency, mild operating conditions, safety and efficiency. Although microbial fuel cells have application prospects in many aspects, in reality, the output power of microbial fuel cells is too low. It is still in the laboratory research and development stage. It is still far away from being used as a power source in actual production and life, which seriously hinders the promotion and use of microbial batteries. Summary of the invention

[0006] In view of the above-mentioned technical problems, in order to quickly start the sulfate-type anaerobic ammonium oxidation process suitable for aged landfill leachate and improve the power generation efficiency of microbial fuel cells, the present invention provides a sulfate-type anaerobic ammonium oxidation power generation device and a control method thereof. The device uses a UASB anaerobic reactor to first cultivate nitrite-type anaerobic ammonium oxidation bacteria suitable for aged landfill leachate, and gradually convert them into sulfate-type anaerobic ammonium oxidation bacteria. The UASB anaerobic reactor of the sulfate-type anaerobic ammonium oxidation process has the conditions required for the anode chamber of the microbial fuel cell, and the aerobic tank and the anoxic tank both have the conditions required for the cathode chamber of the microbial fuel cell, so that a dual-chamber microbial fuel cell can be formed. The extracellular electron transfer of certain power-producing microorganisms in the anaerobic ammonium oxidation reactor provides a possible conversion pathway for sulfate-type anaerobic ammonium oxidation, which is coupled with the microbial fuel cell to simultaneously remove high-concentration SO4 2 -, NH4+ and improve the efficiency of electricity generation in microbial fuel cells.

[0007] The objective of the present invention is achieved through the following technical solutions:

[0008] The invention discloses a sulfate-type anaerobic ammonium oxidation power generation device, comprising an UASB anaerobic reactor, an aerobic tank, an anoxic tank and a sedimentation tank which are connected in sequence through water pipes, and the UASB anaerobic reactor is separated from the aerobic tank and the anoxic tank by proton exchange membranes. The UASB anaerobic reactor is used as an anode chamber of a microbial fuel cell, and an AMC particle carrier filler is added therein as a microbial attachment membrane. The aerobic tank and the anoxic tank are used as cathode chambers of the microbial fuel cell to form a double-chamber microbial fuel cell. The anode chamber and the cathode chamber are respectively connected to a resistance box through a carbon felt electrode enriched with a large number of microorganisms and a copper wire, so as to form a closed loop. The sedimentation tank is provided with a water outlet, and the wastewater after the reaction is discharged from the top of the sedimentation tank, and the sludge is discharged from the sludge outlet at the bottom of the sedimentation tank. The UASB anaerobic reactor is provided with a water inlet at the bottom, which is connected to a sewage tank through a pipeline, and a gas outlet is provided at the top, and the gas after the reaction is discharged to a drying bottle through the gas outlet.

[0009] Furthermore, the bottom of the UASB anaerobic reactor is a conical structure, and a constant temperature circulating water bath is arranged on the periphery and bottom that are not adjacent to the aerobic tank and the anoxic tank, and is provided with a heat-insulating water inlet and a heat-insulating water outlet. The constant temperature circulating water bath is connected to the heat-insulating water inlet below the UASB anaerobic reactor through a pipeline, and water is discharged through the heat-insulating water outlet arranged above the UASB anaerobic reactor after circulation, forming a constant temperature water circulation around the periphery of the UASB anaerobic reactor.

[0010] Furthermore, the sludge suspension zone of the UASB anaerobic reactor is provided with a water outlet, which is connected to the water inlet pipe at the bottom of the UASB anaerobic reactor through a circulation pipeline. A circulation pump is arranged on the circulation pipeline. The effluent from the sludge suspension zone of the UASB anaerobic reactor is mixed with the sewage stock solution and inlet through the bottom of the reactor to circulate inside the UASB anaerobic reactor to ensure that the microorganisms are fully in contact with the sludge.

[0011] Furthermore, the temperature of the constant temperature circulating water bath is maintained at (35±5)°C.

[0012] Furthermore, a three-phase separator is arranged on the top of the UASB anaerobic reactor. After the sewage reacts in the UASB anaerobic reactor, the gas generated after separation by the three-phase separator is discharged through the gas outlet, and the generated supernatant flows to the aerobic tank, the anoxic tank and the sedimentation tank in sequence through the liquid pipeline. The wastewater is discharged through the water outlet above the sedimentation tank, and the sludge is discharged through the sludge outlet at the bottom of the sedimentation tank.

[0013] The present invention adopts the control method of the sulfate-type anaerobic ammonium oxidation power generation device, which comprises the following steps:

[0014] Step 1: In the UASB anaerobic reactor, anaerobic digestion sludge is used as the bacterial source and landfill leachate raw water is used as the influent, so that the NH4+-N concentration in the UASB anaerobic reactor ranges from 80mg / L to 100mg / L, and sodium nitrite is added at a molar ratio of NH4+-N: NO2--N = 1: (1.32-1.5);

[0015] Step 2: If the molar ratio of NH4+-N consumption, NO2-N consumption and NO3-N production in the effluent of the USAB reactor is 1:1.32:0.26, anaerobic ammonium oxidation reaction will occur on the surface, and then the inflow of landfill leachate raw water will be increased to increase the concentration of the reaction matrix inside the UASB anaerobic reactor, so that the NH4+-N concentration in the UASB anaerobic reactor is increased to 150mg / L~160mg / L, and sodium nitrite is added at a molar ratio of NH4+-N:NO2--N=1:1.32-1.5;

[0016] At the same time, the temperature of the thermostatic circulating water bath was controlled to maintain the internal temperature of the UASB anaerobic reactor at (35±5)°C, and AMC granular carrier filler was added to the UASB anaerobic reactor, and the filler accounted for 30% of the volume of the anaerobic reactor; at the same time, the effluent from the sludge suspension zone of the UASB anaerobic reactor was mixed with the effluent from the sewage pool, and then water was introduced from the bottom of the UASB anaerobic reactor for internal circulation, so that the microorganisms and the sludge were fully in contact;

[0017] Step 3: After the nitrite-type anaerobic ammonium oxidation reaction is stable, that is, after the removal rate of NH4+-N and NO2--N in the UASB anaerobic reactor reaches 80% to 90%, the NO2--N concentration in the UASB anaerobic reactor is reduced to 0mg / L to 40mg / L by reducing the amount of sodium nitrite added, and the NH4+-N concentration is 60mg / L to 70mg / L. At this time, the molar ratio of NH4+-N: NO2--N is 1: (0.5-0.6), and the sulfate concentration is 260mg / L to 280mg / L, so that sulfate replaces part of the nitrite addition;

[0018] When SO4 2 -After the removal rate reaches 30% to 45%, no more sodium nitrite is added to the UASB anaerobic reactor. At the same time, by increasing the inflow of landfill leachate raw water and the dosage of sulfate, the NH4+-N and SO4 in the UASB anaerobic reactor are increased. 2 -Concentrations increased to 130mg / L~150mg / L,

[0019] 500mg / L~550mg / L, SO4 2 - Become the electron acceptor of anaerobic ammonium oxidation, NH4+-N, SO4 2-If the removal rate gradually increases and stabilizes at more than 50%, it means that the sulfate-type anaerobic ammonium oxidation has been successfully started, and the sulfate and ammonia nitrogen can be removed simultaneously without adding an external carbon source to produce electricity.

[0020] The beneficial effects of the present invention are:

[0021] The present invention can cultivate nitrite-type anaerobic ammonium-oxidizing bacteria suitable for old landfill leachate, and then gradually transform them into sulfate-type anaerobic ammonium-oxidizing bacteria, which can simultaneously remove high-concentration SO4 in old landfill leachate. 2 -, NH4+, and improve the power generation efficiency of microbial fuel cells. No external carbon source is required, which saves the cost of leachate treatment and realizes the resource utilization of sewage. It has the characteristics of energy saving, high efficiency, low investment and operation costs, etc. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 It is a top view of the overall device of one embodiment of the present invention.

[0023] Figure 2 It is a schematic diagram of the process flow of one embodiment of the present invention.

[0024] Figure 3 This is a structural diagram of the power generation part of an embodiment of the present invention.

[0025] In the figure: 1. sewage tank, 2. UASB anaerobic reactor (anode chamber), 3. aerobic tank (cathode chamber), 4. anoxic tank (cathode chamber), 5. sedimentation tank, 6. water outlet, 7. carbon felt, 8. proton exchange membrane, 9. resistance box, 10. wet gas flow meter, 11. drying bottle, 12. lifting pump, 13. circulation pump, 14. insulation water inlet, 15. gas outlet, 16. insulation water outlet, 17. sampling port, 18. three-phase separator, 19. sludge outlet. DETAILED DESCRIPTION

[0026] The present invention is described in detail below with reference to the accompanying drawings and embodiments.

[0027] like Figure 1 As shown, with the UASB anaerobic reactor 2 as the basic equipment, the nitrite-type anaerobic ammonium oxidation is coupled with the microbial fuel cell in the early stage, and after the nitrite-type anaerobic ammonium oxidation runs stably, it is gradually converted to sulfate-type anaerobic ammonium oxidation, and later a sulfate-type anaerobic ammonium oxidation combined with a microbial fuel cell power generation device is formed.

[0028] The present invention comprises a UASB anaerobic reactor 2, an aerobic tank 3, an anoxic tank 4 and a sedimentation tank 5 which are connected in sequence through water pipes, and the UASB anaerobic reactor 2 is separated from the aerobic tank 3 and the anoxic tank 4 by a proton exchange membrane 8. The UASB anaerobic reactor 2 is used as an anode chamber of a microbial fuel cell, and an AMC particle carrier filler is added therein as a microbial attachment membrane. The aerobic tank 3 and the anoxic tank 4 are used as cathode chambers of the microbial fuel cell to form a double-chamber microbial fuel cell. The anode chamber and the cathode chamber are respectively connected to a carbon felt electrode 7 enriched with a large number of microorganisms and a copper wire external resistor box 9 to form a closed loop. The sedimentation tank 5 is provided with a water outlet, and the wastewater after the reaction is discharged from the top of the sedimentation tank 5, and the sludge is discharged from the sludge outlet at the bottom of the sedimentation tank 5. The UASB anaerobic reactor 2 is provided with a water inlet at the bottom, which is connected to the sewage tank through a pipeline, and a gas outlet is provided at the top, and the gas after the reaction is discharged to a drying bottle through the gas outlet.

[0029] The bottom of the UASB anaerobic reactor 2 is a conical structure, and a constant temperature circulating water bath is arranged at the periphery and bottom that are not adjacent to the aerobic tank 3 and the anoxic tank 4, and an insulating water inlet and an insulating water outlet are opened on the water bath. The constant temperature circulating water bath is connected to the insulating water inlet 14 below the UASB anaerobic reactor through a pipeline, and the water is discharged through the insulating water outlet 16 arranged above the UASB anaerobic reactor 2 after circulation, forming a constant temperature water circulation around the UASB anaerobic reactor 2. The bottom-in and top-out setting can make the insulating water always fill the pipeline. In order to maintain the internal temperature of the UASB anaerobic reactor 2, the present invention can adopt various forms, such as spraying insulating materials on the outer layer of the UASB anaerobic reactor 2, wrapping insulating materials on the surface, etc. The temperature of the constant temperature circulating water bath of the present invention is maintained at 35±5°C.

[0030] The sludge suspension zone of the UASB anaerobic reactor 2 is provided with a water outlet, which is connected to the water inlet at the bottom of the UASB anaerobic reactor 2 through a circulation pipeline. A circulation pump 13 is arranged on the circulation pipeline. Water is discharged from the sludge suspension zone of the UASB anaerobic reactor 2, mixed with the sewage stock solution, and then introduced into the water inlet at the bottom of the UASB anaerobic reactor 2. The internal circulation of the UASB anaerobic reactor 2 can make the microorganisms fully contact with the sludge, thereby increasing the reaction rate.

[0031] A three-phase separator 18 is arranged on the top of the UASB anaerobic reactor 2. The sewage is pumped into the bottom of the UASB anaerobic reactor 2 by the lifting pump 12, and flows through the UASB anaerobic reactor 2 from bottom to top. After reacting in the UASB anaerobic reactor 2, the gas generated after separation by the gas, solid and liquid three-phase separator 18 is discharged through the gas outlet 15, and the generated supernatant flows to the aerobic tank 3, the anoxic tank 4 and the sedimentation tank 5 in sequence through the liquid pipeline. The wastewater is discharged through the water outlet above the sedimentation tank 5, and the sludge is discharged through the sludge outlet 19 at the bottom of the sedimentation tank 5.

[0032] The internal temperature of the UASB anaerobic reactor 2 is maintained at 35±5°C by using a constant temperature circulating water bath, and AMC particle carrier filler is added into the UASB anaerobic reactor 2, and the filler accounts for 30% of the volume of the anaerobic reactor 2. At the same time, due to the arrangement of the circulation pipeline and the circulation pump 13, water discharged from the sludge suspension area of ​​the reactor 2 is mixed with the effluent from the sewage pool 5 and then enters the bottom of the reactor 2 and circulates to the sludge bed area of ​​the reactor 2, so that the microorganisms can fully contact with the sludge. The three-phase separator 18 collects the gas generated by the reaction, and after being dried by the drying bottle 11, it enters the wet gas flowmeter 10 to measure the gas volume.

[0033] Under anaerobic conditions, the UASB anaerobic reactor 2 is used to start the nitrite-type anaerobic ammonium oxidation reaction, and then ammonium sulfate is used as a substrate to gradually replace sodium nitrite to achieve a sulfate-type anaerobic ammonium oxidation reaction for simultaneous nitrogen removal and sulfur removal; the control method of the sulfate-type anaerobic ammonium oxidation power generation device of the present invention comprises the following steps:

[0034] Step 1: In the UASB anaerobic reactor 2, anaerobic digestion sludge is used as the bacterial source, and the leachate raw water is used as the influent. The calculation is performed based on the influent volume of the leachate raw water, the influent NH4+-N concentration, and the effective volume of the UASB anaerobic reactor. The specific calculation method is: NH4+-N concentration in the UASB anaerobic reactor = influent volume of the leachate raw water x influent NH4+-N concentration / effective volume of the UASB anaerobic reactor. By controlling the influent volume, the NH4+-N concentration in the UASB anaerobic reactor 2 is increased. The range is controlled at 80mg / L-100mg / L, and sodium nitrite is added at a molar ratio of NH4+-N:NO2--N=1:1.5. Due to the increase in the amount of NO2--N added, the anaerobic ammonium oxidation reaction can be promoted to a certain extent. During the operation of the device, a multi-function multimeter is used to measure the voltage and current generated by the double-chamber microbial fuel cell at regular intervals to compare the power generation effects of the three reaction types of conventional denitrification, nitrite-type anaerobic ammonium oxidation, and sulfate-type anaerobic ammonium oxidation on the microbial fuel cell.

[0035] Step 2: Since NO2--N is toxic to microorganisms and will inhibit the anaerobic ammonium oxidation process, it cannot be accumulated in large quantities in the reactor. Therefore, after the anaerobic ammonium oxidation reaction occurs, the water intake should be increased to increase the concentration of the reaction substrate. According to the principle of anaerobic ammonium oxidation reaction, if the molar ratio of NH4+-N consumption, NO2--N consumption and NO3--N production in the effluent of the USAB reactor is 1:1.32:0.26, anaerobic ammonium oxidation reaction will occur on the surface. Then, the water intake of the landfill leachate raw water will be increased to increase the concentration of the reaction substrate inside the UASB anaerobic reactor, so that the NH4+-N concentration in the UASB anaerobic reactor is increased to 150mg / L~160mg / L, and sodium nitrite is added at a molar ratio of NH4+-N:NO2--N=1:1.32-1.5.

[0036] At the same time, the temperature of the thermostatic circulating water bath is controlled to maintain the internal temperature of the UASB anaerobic reactor 2 at (35±5)°C, and AMC particle carrier filler is added into the UASB anaerobic reactor, and the filler is 30% of the volume of the anaerobic reactor; at the same time, the effluent from the sludge suspension area of ​​the UASB anaerobic reactor 2 is mixed with the effluent from the sewage pool, and then water is introduced from the bottom of the UASB anaerobic reactor 2 for internal circulation, so that the microorganisms and the sludge are fully in contact with each other 2;

[0037] Step 3: After the nitrite-type anaerobic ammonium oxidation reaction is stable, that is, after the removal rate of NH4+-N and NO2--N in the UASB anaerobic reactor reaches 80% to 90%, the NO2--N concentration in the UASB anaerobic reactor is reduced to 0mg / L to 40mg / L by reducing the amount of sodium nitrite added, and the NH4+-N concentration is 60mg / L to 70mg / L. At this time, the molar ratio of NH4+-N: NO2--N is 1: (0.5-0.6), and the sulfate concentration is 260mg / L to 280mg / L, so that sulfate replaces part of the nitrite addition;

[0038] When SO4 2 -After the removal rate reaches 30% to 45%, no more sodium nitrite is added to the UASB anaerobic reactor. At the same time, by increasing the inflow of landfill leachate raw water and the dosage of sulfate, the NH4+-N and SO4 in the UASB anaerobic reactor are increased. 2 -Concentrations increased to 130mg / L~150mg / L,

[0039] 500mg / L~550mg / L, SO4 2 - Become the electron acceptor of anaerobic ammonium oxidation, NH4+-N, SO4 2-If the removal rate gradually increases and stabilizes at more than 50%, it means that the sulfate-type anaerobic ammonium oxidation has been successfully started, and the sulfate and ammonia nitrogen can be removed simultaneously without adding an external carbon source to produce electricity.

[0040] Embodiment 1: The specific control method of the present invention is:

[0041] Step 1: In the UASB anaerobic reactor 2, anaerobic digestion sludge is used as the bacterial source, and the landfill leachate raw water is used as the influent. The influent volume is controlled so that the NH4+-N concentration in the UASB anaerobic reactor 2 is controlled within the range of 80 mg / L, and sodium nitrite is added at a molar ratio of NH4+-N: NO2--N=1:1.5;

[0042] Step 2: When the molar ratio of NH4+-N consumption, NO2--N consumption and NO3--N production in the effluent of the USAB reactor is 1:1.32:0.26, the inflow of the landfill leachate raw water is increased to increase the NH4+-N concentration in the UASB anaerobic reactor to 150 mg / L, and sodium nitrite is added at a molar ratio of NH4+-N:NO2--N=1:1.32-1.5; the internal temperature of the UASB anaerobic reactor 2 is controlled to be maintained at 35°C, and the AMC particle carrier filler is added to the UASB anaerobic reactor to be 30% of the volume of the anaerobic reactor; at the same time, after the effluent from the sludge suspension zone of the UASB anaerobic reactor 2 is mixed with the effluent from the sewage pool, water is fed from the bottom of the UASB anaerobic reactor 2 for internal circulation, so that the microorganisms and the sludge are fully in contact;

[0043] Step 3: After the nitrite-type anaerobic ammonium oxidation reaction is stable, that is, after the removal rate of NH4+-N and NO2--N in the UASB anaerobic reactor reaches 80%, the NO2--N concentration in the UASB anaerobic reactor is reduced to 40 mg / L and the NH4+-N concentration is 60 mg / L by reducing the dosage of sodium nitrite. At this time, the molar ratio of NH4+-N: NO2--N is 1:0.5, and the sulfate concentration is 260 mg / L, so that sulfate replaces part of the nitrite addition;

[0044] When SO4 2 -After the removal rate reaches 30%, no more sodium nitrite is added to the UASB anaerobic reactor. At the same time, by increasing the inflow of landfill leachate raw water and the dosage of sulfate, the NH4+-N and SO4 in the UASB anaerobic reactor are increased. 2 - concentrations were increased to 130mg / L and 500mg / L, respectively, making SO4 2 - Become the electron acceptor of anaerobic ammonium oxidation, NH4+-N, SO4 2-The removal rate gradually increases and stabilizes at more than 50%, indicating that the sulfate-type anaerobic ammonia oxidation is successfully started. After the system runs stably, the power generation efficiency is stable and efficient. The voltage value is 0.60V and the current intensity is 6.31mA. The highest voltage value and current intensity reach 0.65V and 7.69mA, respectively. It is obtained that sulfate and ammonia nitrogen can be removed at the same time, and there is no need to add an external carbon source to produce electricity.

[0045] Embodiment 2: The specific control method of the present invention is:

[0046] Step 1: In the UASB anaerobic reactor 2, anaerobic digestion sludge is used as the bacterial source, and the landfill leachate raw water is used as the influent. The influent volume is controlled so that the NH4+-N concentration in the UASB anaerobic reactor 2 is controlled within the range of 100 mg / L, and sodium nitrite is added at a molar ratio of NH4+-N: NO2--N=1:1.5;

[0047] Step 2: When the molar ratio of NH4+-N consumption, NO2--N consumption and NO3--N production in the effluent of the USAB reactor is 1:1.32:0.26, the inflow of the leachate raw water is increased to increase the NH4+-N concentration in the UASB anaerobic reactor to 160 mg / L, and sodium nitrite is added at a molar ratio of NH4+-N:NO2--N=1:1.32-1.5; the internal temperature of the UASB anaerobic reactor 2 is controlled to be maintained at 40°C, and the AMC particle carrier filler is added to the UASB anaerobic reactor to be 30% of the volume of the anaerobic reactor; at the same time, after the effluent from the sludge suspension zone of the UASB anaerobic reactor 2 is mixed with the effluent from the sewage pool, water is fed from the bottom of the UASB anaerobic reactor 2 for internal circulation, so that the microorganisms and the sludge are fully in contact;

[0048] Step 3: After the nitrite-type anaerobic ammonium oxidation reaction is stable, that is, after the removal rate of NH4+-N and NO2--N in the UASB anaerobic reactor reaches 90%, the NO2--N concentration in the UASB anaerobic reactor is reduced to 30 mg / L and the NH4+-N concentration is 80 mg / L by reducing the dosage of sodium nitrite. At this time, the molar ratio of NH4+-N: NO2--N is 1:0.6, and the sulfate concentration is 280 mg / L, so that sulfate replaces part of the nitrite addition;

[0049] When SO4 2 After the removal rate of - reaches 45%, no more sodium nitrite is added to the UASB anaerobic reactor. At the same time, by increasing the inflow of landfill leachate raw water and the dosage of sulfate, the NH4+-N and SO4 in the UASB anaerobic reactor are increased. 2 - concentrations were increased to 150mg / L and 550mg / L, respectively, making SO4 2- Become the electron acceptor of anaerobic ammonium oxidation, NH4+-N, SO4 2 -The removal rate gradually increases and stabilizes at more than 50%, indicating that the sulfate-type anaerobic ammonia oxidation is successfully started. After the system runs stably, the power generation efficiency is stable and efficient. The voltage value is 0.71V and the current intensity is 8.26mA. The highest voltage value and current intensity reach 0.78V and 8.82mA, respectively. It is obtained that sulfate and ammonia nitrogen can be removed at the same time without adding an external carbon source.

[0050] Embodiment 3: The specific control method of the present invention is:

[0051] Step 1: In the UASB anaerobic reactor 2, anaerobic digestion sludge is used as the bacterial source, and the landfill leachate raw water is used as the influent. The influent volume is controlled so that the NH4+-N concentration in the UASB anaerobic reactor 2 is controlled within the range of 90 mg / L, and sodium nitrite is added at a molar ratio of NH4+-N: NO2--N=1:1.5;

[0052] Step 2: When the molar ratio of NH4+-N consumption, NO2--N consumption and NO3--N production in the effluent of the USAB reactor is 1:1.32:0.26, the inflow of the landfill leachate raw water is increased to increase the NH4+-N concentration in the UASB anaerobic reactor to 155 mg / L, and sodium nitrite is added at a molar ratio of NH4+-N:NO2--N=1:1.32-1.5; and the internal temperature of the UASB anaerobic reactor 2 is controlled to be maintained at 38°C, and the AMC particle carrier filler is added to the UASB anaerobic reactor to be 30% of the volume of the anaerobic reactor; at the same time, after the effluent from the sludge suspension zone of the UASB anaerobic reactor 2 is mixed with the effluent from the sewage pool, water is fed from the bottom of the UASB anaerobic reactor 2 for internal circulation, so that the microorganisms and the sludge are fully in contact;

[0053] Step 3: After the nitrite-type anaerobic ammonium oxidation reaction is stable, that is, the removal rate of NH4+-N and NO2--N in the UASB anaerobic reactor reaches 85%, the NO2--N concentration in the UASB anaerobic reactor is reduced to 0 mg / L and the NH4+-N concentration is 65 mg / L by reducing the amount of sodium nitrite added. At this time, the molar ratio of NH4+-N: NO2--N = 1:

[0054] (0.5-0.6), the sulfate concentration is 270 mg / L, so that sulfate replaces part of the nitrite addition;

[0055] When SO4 2 -After the removal rate reaches 40%, no more sodium nitrite is added to the UASB anaerobic reactor. At the same time, by increasing the inflow of landfill leachate raw water and the dosage of sulfate, the NH4+-N and SO4 in the UASB anaerobic reactor are increased.2 - concentrations were increased to 140mg / L and 520mg / L, respectively, making SO4 2 - Become the electron acceptor of anaerobic ammonium oxidation, NH4+-N, SO4 2 -The removal rate gradually increases and stabilizes at more than 50%, indicating that the sulfate-type anaerobic ammonia oxidation is successfully started. After the system runs stably, the power generation efficiency is stable and efficient. The voltage value is 0.65V and the current intensity is 7.54mA. The highest voltage value and current intensity reach 0.74V and 8.39mA, respectively. Sulfate and ammonia nitrogen can be removed at the same time, and there is no need to add an external carbon source to produce electricity.

[0056] It can be understood that the above specific description of the present invention is only used to illustrate the present invention and is not limited to the technical solutions described in the embodiments of the present invention. Those skilled in the art should understand that the present invention can still be modified or replaced by equivalents to achieve the same technical effects; as long as the use requirements are met, they are within the protection scope of the present invention.

Claims

1. A control method for a sulfate-based anaerobic ammonium oxidation power generation device, characterized in that: The steps include: Step 1: The anaerobic digestion sludge in the UASB anaerobic reactor is used as the bacterial source and the leachate water is used as the influent water to make the NH4 + -N concentration range is 80mg / L~100mg / L, and the molar ratio of NH4 + -N:NO2 - -N=1:(1.32-1.5), add sodium nitrite; Step 2: If the USAB reactor effluent, NH4 + -N consumption, NO2 - -N consumption and NO3 - The molar ratio of -N production is 1:1.32:0.26, then anaerobic ammonia oxidation reaction occurs on the surface, and then the inflow of landfill leachate raw water is increased, the concentration of the reaction matrix inside the UASB anaerobic reactor is increased, and the NH4 + -N concentration was increased to 150mg / L~160mg / L, and the molar ratio of NH4 + -N:NO2 - -N=1:1.32-1.5, add sodium nitrite; At the same time, the temperature of the thermostatic circulating water bath was controlled to maintain the internal temperature of the UASB anaerobic reactor at (35±5)°C, and AMC granular carrier filler was added to the UASB anaerobic reactor, and the filler accounted for 30% of the volume of the anaerobic reactor; at the same time, the effluent from the sludge suspension zone of the UASB anaerobic reactor was mixed with the effluent from the sewage pool, and then water was introduced from the bottom of the UASB anaerobic reactor for internal circulation, so that the microorganisms and the sludge were fully in contact; Step 3: After the nitrite-type anaerobic ammonium oxidation reaction is stabilized, that is, NH4 + -N and NO2 - After the removal rate of -N reaches 80% to 90%, the amount of sodium nitrite added is reduced to make the NO2 - -N concentration drops to 0mg / L~40mg / L, NH4 + -N concentration is 60mg / L~70mg / L, at this time the molar ratio of NH4 + -N:NO2 - -N=1: (0.5-0.6), sulfate concentration is 260mg / L~280mg / L, so that sulfate replaces part of the nitrite addition; When SO4 2- When the removal rate reaches 30% to 45%, no more sodium nitrite is added to the UASB anaerobic reactor. At the same time, by increasing the inflow of landfill leachate raw water and the dosage of sulfate, the NH4 + -N、SO4 2- The concentrations were increased to 130mg / L~150mg / L, 500mg / L~550mg / L, SO4 2- Become the electron acceptor of anaerobic ammonium oxidation, NH4 + -N、SO4 2- If the removal rate gradually increases and stabilizes at more than 50%, it means that the sulfate-type anaerobic ammonium oxidation has been successfully started, and a power generation device can be obtained by removing sulfate and ammonia nitrogen at the same time without adding an external carbon source.

2. The control method according to claim 1, characterized in that: The sulfate-type anaerobic ammonium oxidation power generation device comprises an UASB anaerobic reactor (2), an aerobic tank (3), an anoxic tank (4) and a sedimentation tank (5) which are connected in sequence through water pipes, and the UASB anaerobic reactor (2) is separated from the aerobic tank (3) and the anoxic tank (4) by a proton exchange membrane (8) on the side wall, wherein the UASB anaerobic reactor (2) serves as an anode chamber of a microbial fuel cell, and an AMC particle carrier filler is added therein as a microbial attachment membrane, and the aerobic tank (3) and the anoxic tank (4) serve as microbial The cathode chamber of the fuel cell constitutes a double-chamber microbial fuel cell; the anode chamber and the cathode chamber are respectively connected to a carbon felt electrode (7) enriched with a large number of microorganisms and a copper wire external resistance box (9) to form a closed loop; the sedimentation tank (5) is provided with a water outlet, and the wastewater after the reaction is discharged from the top of the sedimentation tank (5); the sludge is discharged from the sludge outlet at the bottom of the sedimentation tank (5); the UASB anaerobic reactor (2) is provided with a water inlet at the bottom, which is connected to the sewage tank through a pipeline; and a gas outlet is provided at the top, and the gas after the reaction is discharged to a drying bottle through the gas outlet.

3. The control method according to claim 2, characterized in that: The bottom of the UASB anaerobic reactor is a conical structure, and a constant temperature circulating water bath is arranged at the periphery and bottom that are not adjacent to the aerobic tank (3) and the anoxic tank (4), and a heat preservation water inlet and a heat preservation water outlet are opened on the water bath. The constant temperature circulating water bath is connected to the heat preservation water inlet (14) below the UASB anaerobic reactor through a pipeline, and water is discharged through the heat preservation water outlet (16) arranged above the UASB anaerobic reactor after circulation, so that a constant temperature water circulation is formed around the periphery of the UASB anaerobic reactor.

4. The control method according to claim 3, characterized in that: The sludge suspension zone of the UASB anaerobic reactor is provided with a water outlet, which is connected to the water inlet pipe at the bottom of the UASB anaerobic reactor through a circulation pipeline. A circulation pump is arranged on the circulation pipeline. The effluent from the sludge suspension zone of the UASB anaerobic reactor is mixed with the sewage stock solution and flows through the water inlet at the bottom of the reactor to circulate inside the UASB anaerobic reactor to ensure that the microorganisms are fully in contact with the sludge.

5. The control method according to claim 3, characterized in that: The temperature of the constant temperature circulating water bath was maintained at (35±5)°C.

6. The control method according to claim 2, characterized in that: A three-phase separator is arranged on the top of the UASB anaerobic reactor. After the sewage reacts in the UASB anaerobic reactor, the gas generated after separation by the three-phase separator is discharged through the gas outlet, and the generated supernatant flows to the aerobic tank (3), the anoxic tank (4) and the sedimentation tank (5) in sequence through the liquid pipeline. The wastewater is discharged through the water outlet above the sedimentation tank, and the sludge is discharged through the sludge outlet at the bottom of the sedimentation tank (5).

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