CN114291962B - Device and method for treating late landfill leachate by three-stage plug flow type PN-PNA-DE process - Google Patents
Device and method for treating late landfill leachate by three-stage plug flow type PN-PNA-DE process Download PDFInfo
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Abstract
A device and a method for treating late landfill leachate by a three-stage plug-flow PN-PNA-DE process belong to the field of biological treatment of high ammonia nitrogen wastewater. The leachate raw water and the effluent of the third-level biochemical treatment are mixed in the first-level regulating tank and then enter the PN biochemical tank, the hydrolysis and denitrification reaction of organic matters is carried out in an anoxic zone, the short-range nitrification reaction is carried out in an aerobic zone, the anoxic zone in-situ FA treatment and the aerobic zone in-situ FNA treatment are the keys for maintaining stable short-range nitrification and hydrolysis and acidification of the organic matters in the PN biochemical tank, and the start of the backflow of the effluent of the third-level biochemical treatment relieves the inhibition of FA and FNA on AOB and denitrifying bacteria in the PN biochemical tank. Effluent from the first-stage biochemical treatment enters a PNA biochemical tank for autotrophic denitrification, the inhibition of FA on the ANAOB is relieved by a sectional water inlet strategy, the utilization efficiency of inlet organic matters is improved, and sufficient nitrite nitrogen is provided for the anaerobic ammonia oxidation process by the grading arrangement of the PN biochemical tank and the PNA biochemical tank. The invention realizes low-carbon high-efficiency deep denitrification.
Description
Technical Field
The invention relates to a method for deeply denitrifying advanced landfill leachate with high efficiency and low cost by taking a three-stage plug-flow type short-cut nitrification/denitrification-short-cut nitrification coupled anaerobic ammonia oxidation-deep denitrification technology as a core and aiming at relieving the inhibition of in-situ free ammonia and free nitrous acid treatment on key functional bacteria while realizing stable short-cut nitrification, and belongs to the technical field of biological treatment of high ammonia nitrogen wastewater.
Background
From 2004 to 2020, the annual clearing and transporting amount of urban domestic garbage in China is 1.55 multiplied by 10 4 Increased to 2.35X 10 4 Ten thousand tons, the harmless treatment rate is increased from 52.1 percent to 99.7 percent, the harmless treatment mode is gradually changed from sanitary landfill to incineration, but both the harmless treatment mode and the sanitary landfill generate landfill leachate. Wherein the biological treatment method is the most economical and low-carbon method for the denitrification of the landfill leachate.
Compared with the traditional nitrification-denitrification biological denitrification process, the short-cut nitrification coupled anaerobic ammonia oxidation (PNA) process can save about 60% of aeration energy consumption and 100% of carbon source addition amount theoretically, and is more and more widely used in the biological treatment research of the landfill leachate. However, the technology for denitrification of late landfill leachate also faces the following problems: how to obtain a stable short-cut nitrification effect; how to ensure that the anaerobic ammonia oxidation process has sufficient nitrite sources; the method is used for treating and inhibiting Nitrite Oxidizing Bacteria (NOB) by using in-situ Free Ammonia (FA) and Free Nitrous Acid (FNA), and simultaneously, how to relieve the inhibition of Ammonia Oxidizing Bacteria (AOB) and anaerobic ammonia oxidizing bacteria (ANAOB); how to realize effective retention of AnAOB in the system; and how to further remove nitrate generated by the PNA process.
Disclosure of Invention
The invention provides a device and a method for treating late landfill leachate by a three-stage plug flow type PN-PNA-DE process. Leachate raw water firstly enters a PN biochemical pool, NOB is inhibited and elutriated under anoxic in-situ FA treatment and aerobic in-situ FNA treatment, and organic matter hydrolysis and denitrification are carried out in an anoxic zone of the PN biochemical pool; mixing the effluent of the primary biochemical treatment and raw water of leachate, dividing into three sections, continuously feeding the three sections into a PNA biochemical tank, carrying out anaerobic ammonia oxidation and denitrification reactions in an anoxic zone of the PNA biochemical tank, and carrying out synchronous shortcut nitrification coupled anaerobic ammonia oxidation reactions in an aerobic zone of the PNA biochemical tank; the effluent of the secondary biochemical treatment enters a DE biochemical tank for deep denitrification; and after the effluent of the three-stage biochemical treatment is stable, optimizing parameters of the system, starting an effluent reflux device, mixing the effluent of the three-stage biochemical treatment with raw leachate, and pumping the mixed effluent into a PN biochemical pool, thereby improving the ammonia nitrogen removal efficiency.
The device for treating the landfill leachate at the late stage by the three-stage plug-flow PN-PNA-DE process is characterized by comprising the following contents: a primary regulating tank (1); a PN biochemical pool (2); a primary sedimentation tank (3); a secondary regulating tank (4); a PNA biochemical pool (5); a secondary sedimentation tank (6); a third-stage regulating tank (7); a DE biochemical pool (8); a third-stage sedimentation tank (9);
wherein, a PN biochemical pool water inlet pump (2.10) continuously pumps the raw leachate and the mixed liquor (1.2) of the three-stage biochemical treatment effluent 1 from the primary regulating pool (1) through a PN biochemical pool water inlet pipeline (2.11) into a PN biochemical pool cell I (2.1) to be mixed with activated sludge, and flows out of the PN biochemical pool cell II (2.9) to enter a PN biochemical pool water outlet pipeline (2.19) and a primary sedimentation pool (3); after precipitation, supernatant enters a secondary regulating tank (4) through a primary biochemical treatment water outlet pump (4.3) and a primary biochemical treatment water outlet pipeline (3.1), and sludge in the primary sedimentation tank (3) flows back to a PN biochemical pool grid chamber I (2.1) through a primary sludge return pump (3.2) and a primary sludge return pipeline (3.3); raw leachate is pumped into a secondary regulating reservoir (4) through a secondary regulating reservoir water inlet pump (4.1) and a secondary regulating reservoir water inlet pipeline (4.2) to be mixed with effluent of primary biochemical treatment; mixed liquid in the secondary regulating tank (4) respectively enters a PNA biochemical pool cell first (5.1), a PNA biochemical pool cell fourth (5.4) and a PNA biochemical pool cell seventh (5.7) of the PNA biochemical pool (5) through a PNA biochemical pool water inlet pump I (5.10) and a PNA biochemical pool water inlet pipeline I (5.11), a PNA biochemical pool water inlet pump II (5.12) and a PNA biochemical pool water inlet pipeline II (5.13), a PNA biochemical pool water inlet pump III (5.14) and a PNA biochemical pool water inlet pipeline III (5.15); the sludge-water mixed liquid of the PNA biochemical tank (5) enters a secondary sedimentation tank (6) through a PNA biochemical tank water outlet pipeline (5.25); after precipitation, supernatant in the secondary sedimentation tank (6) enters a tertiary regulating tank (7) through a secondary biochemical treatment water outlet pipeline (6.1); sludge at the bottom of the secondary sedimentation tank (6) reflows to a first PNA biochemical tank cell (5.1) through a secondary sludge reflow pump (6.2) and a secondary sludge reflow pipeline (6.3); sodium acetate solution enters a third-stage regulating tank (7) through an external carbon source feeding pump (7.1) and an external carbon source feeding pipeline (7.2) to be mixed with effluent of the second-stage biochemical treatment; the mixed liquid in the third-stage regulating tank (7) enters the front end of an anoxic zone (8.8) of the DE biochemical tank through a DE biochemical tank water inlet pump (8.1) and a DE biochemical tank water inlet pipeline (8.2), and water is discharged from the tail end of an aerobic zone (8.9) of the DE biochemical tank and enters a third-stage sedimentation tank (9) through a DE biochemical tank water outlet pipeline (8.10); after precipitation, 50% of the supernatant enters a water outlet pipeline (9.1) of the three-stage biochemical treatment, and 50% of the supernatant enters a first-stage regulating tank (1) through a water outlet reflux pump (9.5) and a water outlet reflux pipeline (9.6); the sludge in the third-stage sedimentation tank (9) flows back to an anoxic zone (8.8) of the DE biochemical tank through a third-stage sludge return pump (9.3) and a third-stage sludge return pipeline (9.4);
in addition, the primary regulating tank (1) also comprises a percolate raw water pipeline (1.1); the PN biochemical pool (2) further comprises a PN biochemical pool cell II (2.2), a PN biochemical pool cell III (2.3), a PN biochemical pool cell IV (2.4), a PN biochemical pool cell V (2.5), a PN biochemical pool cell VI (2.6), a PN biochemical pool cell seven (2.7), a PN biochemical pool cell eight (2.8), a PN biochemical pool temperature control device (2.12), a PN biochemical pool heating device (2.13), a PN biochemical pool pH and DO real-time monitoring device (2.14), a PN biochemical pool mechanical stirrer (2.15), a PN biochemical pool aeration device (2.16), a PN biochemical pool gas flow meter (2.17) and a PN biochemical pool microporous aeration disc (2.18); the primary sedimentation tank also comprises a primary biochemical treatment residual sludge discharge pipeline (3.4); the PNA biochemical pool (5) further comprises a PNA biochemical pool cell II (5.2), a PNA biochemical pool cell III (5.3), a PNA biochemical pool cell IV (5.4), a PNA biochemical pool cell V (5.5), a PNA biochemical pool cell VI (5.6), a PNA biochemical pool cell VII (5.7), a PNA biochemical pool cell VIII (5.8), a PNA biochemical pool cell nine (5.9), a PNA biochemical pool temperature control device (5.16), a PNA biochemical pool heating device (5.17), a PNA biochemical pool pH and DO real-time monitoring device (5.18), a PNA biochemical pool mechanical stirrer (5.19), a PNA biochemical pool aeration device (5.20), a PNA pool gas flow meter (5.21), a PNA biochemical pool microporous aeration disc (5.22), a biomembrane carrier (5.23) and a biomembrane carrier fixing frame (5.24); the DE biochemical pool (8) further comprises a pH and DO real-time monitoring device (8.3) of the DE biochemical pool, a mechanical stirrer (8.4) of the DE biochemical pool, an aeration device (8.5) of the DE biochemical pool, a gas flowmeter (8.6) of the DE biochemical pool and a microporous aeration disc (8.7) of the DE biochemical pool; the three-stage sedimentation tank (9) also comprises a three-stage biochemical treatment residual sludge discharge pipeline (9.2). The specific location is shown in fig. 1.
The method for treating the landfill leachate at the late stage by using the device is carried out according to the following processes:
(1) Starting the PN biochemical pool (2):
the water temperature of the PN biochemical pool (2) is 30 +/-1 ℃; the sludge concentration is that MLSS is 4500 + -500 mg/L, the sludge reflux ratio is 300%; dissolved oxygen from PN biochemical pool cell five (2.5) to PN biochemical pool cell nine (2.9) is 3.0-7.0 mg/L; the inlet water of the PN biochemical pool (2) is leachate raw water, the total inorganic nitrogen concentration is 2000.0 +/-200.0 mg/L, and NH 4 + The concentration of-N is 1980.0 +/-200.0 mg/L, and the COD is 3370.0 +/-200.0 mg/L; the pH value from PN biochemical pool cell I (2.1) to PN biochemical pool cell IV (2.4) is 7.6-7.8, PN biochemical pool cell V (2.5) to PN biochemical pool cell VI (2.9)The pH of (A) is 7.2-7.8; the FA concentration from the PN biochemical pool cell I (2.1) to the PN biochemical pool cell IV (2.4) is 25.0-40.0 mg N/L, and the FA concentration from the PN biochemical pool cell V (2.5) to the PN biochemical pool cell nine (2.9) is 5.2-28.1 mg N/L; the FNA concentration of PN biochemical cell I (2.1) to PN biochemical cell IV (2.4) is lower than 0.07mg N/L, and the FNA concentration of PN biochemical cell V (2.5) to PN biochemical cell VI (2.9) is lower than 0.22mg N/L; the operation is carried out according to the conditions, so that the nitrite accumulation rate of the effluent of the PN biochemical pool (2) is more than 90.0 percent, and NH is added 4 + -N removal greater than 60%; (2) constructing a shortcut nitrification coupled anaerobic ammonia oxidation PNA system:
inoculating a biomembrane carrier (5.23) with the relative abundance of anammox bacteria of more than 10.0 percent into the PNA biochemical pool (5), and fixing the biomembrane carrier (5.23) on a biomembrane carrier fixing frame (5.24), wherein the filling ratio is 20.0 +/-2.0 percent; inoculating the residual sludge after the primary biochemical treatment into a PNA biochemical pool (5) to ensure that the concentration of floc sludge is 2000-2500 mg/L and the sludge reflux ratio is 200 percent; the water temperature of the PNA biochemical pool (5) is 30 +/-1 ℃; the dissolved oxygen concentration of the PNA biochemical pool cell III (5.3), the PNA biochemical pool cell VI (5.6) and the PNA biochemical pool cell nine (5.9) is 0.1-0.2 mg/L; the secondary regulating tank (4) is internally provided with raw water of percolate and effluent of primary biochemical treatment 1:1 at a flow ratio of 1 3 Increasing the volume of/d to 0.25kg N/m 3 D; PNA biochemical pool cell I, II, IV, V, VII, VIII (5.1, 5.2,5.4,5.5,5.7, 5.8) pH 7.6-7.9, FA concentration 7.8-14.6 mg N/L, FNA concentration less than 0.01mg N/L; PNA biochemical pool cell three, six, nine (5.3, 5.6, 5.9) pH 6.9-7.2, FA concentration 0-1.0 mg N/L, FNA concentration less than 0.005mg N/L; the operation is carried out according to the conditions, so that the total inorganic nitrogen concentration in the effluent of the PNA biochemical pool (5) is lower than 60.0mg/L, and NH is generated 4 + -N concentration lower than 10.0mg/L, COD lower than 2200mg/L;
(3) PN biochemical pool (2), PNA biochemical pool (5) and DE biochemical pool (8) are connected in series for operation:
sodium acetate solution with the mass fraction of 15 percent enters the reactor through an external carbon source feeding pump (7.1) and an external carbon source feeding pipeline (7.2)The wastewater enters a third-stage regulating tank (7) and is mixed with the effluent of the second-stage biochemical treatment according to the flow ratio of 1 3 - The concentration of-N is 20.0-50.0 mg/L; the sludge concentration of the DE biochemical pool (8) is 4000 +/-500 mg/L, and the sludge reflux ratio is 100 percent; dissolved oxygen in an aerobic zone (8.9) of the DE biochemical tank is 2.0-3.0 mg/L, and the pH value is 7.0-7.5; the pH value of an anoxic zone (8.8) of the DE biochemical pool is 7.5-8.0; the operation is carried out according to the conditions, so that the total inorganic nitrogen of the effluent of the three-stage biochemical treatment is lower than 15.0mg/L and NH 4 + -N concentration lower than 1.5mg/L;
(4) Starting effluent backflow:
the effluent of the three-stage biochemical treatment enters a first-stage regulating reservoir (1) through an effluent reflux pump (9.5) and an effluent reflux pipeline (9.6), and the raw water of the leachate is 1:1, mixing in a flow ratio;
(5) Adjusting the operation parameters of the PN biochemical pool (2):
the water temperature of the PN biochemical pool (2) is 30 +/-1 ℃; the sludge concentration is that MLSS is 4500 + -500 mg/L, the sludge reflux ratio is reduced from 300% to 200%; the inlet water of the PN biochemical pool (2) is a mixed solution (1.2) of raw leachate and outlet water 1 of three-stage biochemical treatment, the total inorganic nitrogen concentration is 1000.0 +/-100.0 mg/L, and NH is generated by the reaction of the raw leachate and the outlet water 1 4 + The concentration of N is 990.0 +/-100.0 mg/L, and the COD is 2700.0 +/-200.0 mg/L; the pH value from the PN biochemical cell I (2.1) to the PN biochemical cell IV (2.4) is 7.7-8.0, the FA concentration is 16.1-30.8 mg N/L, and the FNA concentration is lower than 0.02mg N/L; the pH value from PN biochemical cell five (2.5) to PN biochemical cell nine (2.9) is 7.0-7.5, the FA concentration is 0.8-8.7 mg N/L, the FNA concentration is 0.03-0.17 mg N/L, and the dissolved oxygen is 3.0-7.0 mg/L.
The novel device and the method for treating the late landfill leachate by the continuous flow single-stage A/O process have the following characteristics and advantages:
(1) The anoxic in-situ FA treatment and the aerobic in-situ FNA treatment effectively inhibit and elutriate NOB in the PN biochemical pool, and ensure stable short-cut nitrification effect.
(2) The strategy of mixing the effluent subjected to the three-stage biochemical treatment with the raw leachate effectively relieves the inhibition of FA and FNA in the PN biochemical pool on AOB and denitrifying bacteria.
(3) The PNA biochemical pool staged water inlet strategy effectively relieves the inhibition of FA on the AnAOB, and also improves the utilization efficiency of inlet organic matters.
(4) The PNA biochemical pool is used for fixing a biological membrane and coexisting with floc sludge, so that the effective retention of the AnAOB is promoted, and the influence of adverse environmental factors of the unit on the AnAOB is relieved.
(5) The PN biochemical pool, the PNA biochemical pool and the DE biochemical pool are arranged in a grading way, so that the anoxic zone of the PNA biochemical pool is ensured to have sufficient nitrite substrate, and the deep removal of nitrate generated in the PNA process is realized.
Drawings
FIG. 1 is a schematic structural diagram of a device for treating late landfill leachate by a three-stage plug-flow PN-PNA-DE process.
Wherein, 1, a first-stage adjusting tank; 2-PN biochemical pool; 3-a first-stage sedimentation tank; 4-a secondary regulating tank; 5-PNA biochemical pool; 6-a secondary sedimentation tank; 7-a third-stage adjusting tank; 8-DE biochemical pool; 9-a third-level sedimentation tank; 1.1-leachate; 2.1-PN biochemical pool cell I; 2.2-PN biochemical pool cell II; 2.3-PN biochemical pool cell III; 2.4-PN biochemical pool cell four; 2.5-PN biochemistry pool cell five; 2.6-PN biochemical pool cell six; 2.7-PN biochemical pool cell seven; 2.8-eight PN biochemical pool cells; 2.9-PN biochemical pool cell nine; 2.10-PN biochemical pool water inlet pump; 2.11-inlet pipeline of PN biochemical pool; 2.12-temperature control device of PN biochemical pool; 2.13-PN biochemical pool heating device; 2.14-PN biochemical pool pH and DO real-time monitoring device; 2.15-PN biochemical pool mechanical agitator; 2.16-PN biochemical pool aeration device; 2.17-PN biochemical pool gas flowmeter; 2.18-PN biochemical pool microporous aeration disc; 2.19-PN biochemical pool water outlet pipeline; 3.1-a water outlet pipeline for primary biochemical treatment; 3.2-first-stage sludge reflux pump; 3.3-first-stage sludge return line; 3.4-a first-stage biochemical treatment excess sludge discharge pipeline; 4.1-a water inlet pump of a secondary regulating tank; 4.2-water inlet pipeline of the secondary regulating tank; 4.3-first-stage biochemical treatment water outlet pump; 5.1-PNA biochemical pool cell I; 5.2-PNA biochemical pool cell II; 5.3-PNA biochemical pool cell III; 5.4-PNA Biochemical pool cell four; 5.5-PNA biochemical pool cell five; 5.6-PNA biochemical pool cell six; 5.7 PNA biochemical pool cell seven; 5.8-PNA biochemical pool cell eight; 5.9 PNA Biochemical pool cell nine; 5.10-PNA biochemical pool water inlet pump I; 5.11-inlet pipe I of PNA biochemical pool; 5.12-PNA biochemical pool inlet pump II; 5.13-inlet pipe of PNA biochemical pool two; 5.14-PNA biochemical pool intake pump III; 5.15-inlet pipeline III of PNA biochemical pool; 5.16-PNA biochemical pool temperature control device; 5.17 — PNA biochemical pool heating device; 5.18 — PNA biochemical pool pH and DO real-time monitoring device; 5.19-PNA biochemical pool mechanical stirrer; 5.20-PNA biochemical pool aeration apparatus; 5.21-PNA biochemical pool gas flowmeter; 5.22-PNA biochemical pool microporous aeration disc; 5.23-biofilm carrier; 5.24-biofilm carrier fixing frame; 5.25-water outlet pipeline of PNA biochemical pool; 6.1-a secondary biochemical treatment water outlet pipeline; 6.2-second level sludge reflux pump; 6.3-secondary sludge return line; 7.1-external carbon source feeding pump; 7.2-external carbon source feeding pipeline; 8.1-DE biochemical pool water inlet pump; 8.2-DE biochemical pool water inlet pipeline; 8.3-a real-time monitoring device for pH and DO of the DE biochemical pool; 8.4-DE biochemical pool mechanical agitator; 8.5-DE aeration device of biochemical pool; 8.6-DE biochemical pool gas flowmeter; 8.7-DE biochemical pool microporous aeration disc; 8.8-anoxic zone of DE biochemical pool; 8.9-aerobic zone of DE biochemical pool; 8.10-DE biochemical pool water outlet pipeline; 9.1-a water outlet pipeline for three-stage biochemical treatment; 9.2-a three-stage biochemical treatment excess sludge discharge pipeline; 9.3-three-stage sludge reflux pump; 9.4-three-stage sludge return line; 9.5-effluent reflux pump; 9.6-water outlet return pipeline.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
As shown in FIG. 1, the device for treating the late landfill leachate by the three-stage plug-flow PN-PNA-DE process comprises: a primary regulating tank (1); a PN biochemical pool (2); a primary sedimentation tank (3); a secondary regulating tank (4); a PNA biochemical pool (5); a secondary sedimentation tank (6); a third-stage regulating tank (7); a DE biochemical pool (8); a third-stage sedimentation tank (9);
wherein, a PN biochemical pool water inlet pump (2.10) continuously pumps the raw leachate and the mixed liquor (1.2) of the three-stage biochemical treatment effluent 1 from the primary regulating pool (1) through a PN biochemical pool water inlet pipeline (2.11) into a PN biochemical pool cell I (2.1) to be mixed with activated sludge, and flows out of the PN biochemical pool cell II (2.9) to enter a PN biochemical pool water outlet pipeline (2.19) and a primary sedimentation pool (3); after precipitation, supernatant enters a secondary regulating tank (4) through a primary biochemical treatment water outlet pump (4.3) and a primary biochemical treatment water outlet pipeline (3.1), and sludge in the primary sedimentation tank (3) flows back to a PN biochemical pool grid chamber I (2.1) through a primary sludge return pump (3.2) and a primary sludge return pipeline (3.3); leachate raw water is pumped into a secondary regulating reservoir (4) through a secondary regulating reservoir water inlet pump (4.1) and a secondary regulating reservoir water inlet pipeline (4.2) to be mixed with effluent of primary biochemical treatment; mixed liquid in the secondary regulating tank (4) respectively enters a PNA biochemical tank cell I (5.1), a PNA biochemical tank cell IV (5.4) and a PNA biochemical tank cell VII (5.7) of the PNA biochemical tank (5) through a PNA biochemical tank water inlet pump I (5.10) and a PNA biochemical tank water inlet pipeline I (5.11), a PNA biochemical tank water inlet pump II (5.12) and a PNA biochemical tank water inlet pipeline II (5.13), the PNA biochemical tank water inlet pump III (5.14) and the PNA biochemical tank water inlet pipeline III (5.15); the sludge-water mixed liquid of the PNA biochemical tank (5) enters a secondary sedimentation tank (6) through a PNA biochemical tank water outlet pipeline (5.25); after precipitation, supernatant in the secondary sedimentation tank (6) enters a tertiary regulating tank (7) through a secondary biochemical treatment water outlet pipeline (6.1); sludge at the bottom of the secondary sedimentation tank (6) flows back to a PNA biochemical tank cell I (5.1) through a secondary sludge return pump (6.2) and a secondary sludge return pipeline (6.3); sodium acetate solution enters a third-stage regulating tank (7) through an external carbon source feeding pump (7.1) and an external carbon source feeding pipeline (7.2) to be mixed with effluent of the second-stage biochemical treatment; the mixed liquid in the third-stage regulating tank (7) enters the front end of an anoxic zone (8.8) of the DE biochemical tank through a DE biochemical tank water inlet pump (8.1) and a DE biochemical tank water inlet pipeline (8.2), and water is discharged from the tail end of an aerobic zone (8.9) of the DE biochemical tank and enters a third-stage sedimentation tank (9) through a DE biochemical tank water outlet pipeline (8.10); after precipitation, 50% of the supernatant enters a water outlet pipeline (9.1) for three-stage biochemical treatment, and 50% of the supernatant enters a first-stage regulating tank (1) through a water outlet reflux pump (9.5) and a water outlet reflux pipeline (9.6); the sludge in the third-stage sedimentation tank (9) flows back to an anoxic zone (8.8) of the DE biochemical tank through a third-stage sludge return pump (9.3) and a third-stage sludge return pipeline (9.4);
in addition, the primary regulating tank (1) also comprises a percolate raw water pipeline (1.1); the PN biochemical pool (2) further comprises a PN biochemical pool cell II (2.2), a PN biochemical pool cell III (2.3), a PN biochemical pool cell IV (2.4), a PN biochemical pool cell V (2.5), a PN biochemical pool cell VI (2.6), a PN biochemical pool cell seven (2.7), a PN biochemical pool cell eight (2.8), a PN biochemical pool temperature control device (2.12), a PN biochemical pool heating device (2.13), a PN biochemical pool pH and DO real-time monitoring device (2.14), a PN biochemical pool mechanical stirrer (2.15), a PN biochemical pool aeration device (2.16), a PN biochemical pool gas flow meter (2.17) and a PN biochemical pool microporous aeration disc (2.18); the primary sedimentation tank also comprises a primary biochemical treatment residual sludge discharge pipeline (3.4); the PNA biochemical pool (5) further comprises a PNA biochemical pool cell II (5.2), a PNA biochemical pool cell III (5.3), a PNA biochemical pool cell IV (5.4), a PNA biochemical pool cell V (5.5), a PNA biochemical pool cell VI (5.6), a PNA biochemical pool cell VII (5.7), a PNA biochemical pool cell VIII (5.8), a PNA biochemical pool cell nine (5.9), a PNA biochemical pool temperature control device (5.16), a PNA biochemical pool heating device (5.17), a PNA biochemical pool pH and DO real-time monitoring device (5.18), a PNA biochemical pool mechanical stirrer (5.19), a PNA biochemical pool aeration device (5.20), a PNA pool gas flow meter (5.21), a PNA biochemical pool microporous aeration disc (5.22), a biomembrane carrier (5.23) and a biomembrane carrier fixing frame (5.24); the DE biochemical tank (8) further comprises a pH and DO real-time monitoring device (8.3) of the DE biochemical tank, a mechanical stirrer (8.4) of the DE biochemical tank, an aeration device (8.5) of the DE biochemical tank, a gas flowmeter (8.6) of the DE biochemical tank and a microporous aeration disc (8.7) of the DE biochemical tank; the three-stage sedimentation tank (9) also comprises a three-stage biochemical treatment residual sludge discharge pipeline (9.2).
The method for treating the landfill leachate at the late stage by using the device is carried out according to the following processes:
(1) Starting the PN biochemical pool (2):
the water temperature of the PN biochemical pool (2) is 30 +/-1 ℃; the sludge concentration is that MLSS is 4500 + -500 mg/L, the sludge reflux ratio is 300%; dissolved oxygen from PN biochemical pool cell five (2.5) to PN biochemical pool cell nine (2.9) is 3.0-7.0 mg/L; the inlet water of the PN biochemical pool (2) is leachate raw water, the total inorganic nitrogen concentration is 2000.0 +/-200.0 mg/L, and NH 4 + The concentration of-N is 1980.0 +/-200.0 mg/L, and the COD is 3370.0 +/-200.0 mg/L; the pH value from PN biochemical pool cell I (2.1) to PN biochemical pool cell IV (2.4) is 7.6-7.8, and the pH value from PN biochemical pool cell V (2.5) to PN biochemical pool cell V (2.9) is 7.2-7.8; the FA concentration from the first (2.1) of the PN biochemical cell to the fourth (2.4) of the PN biochemical cell is 25.0 to 40.0mg NThe FA concentration from the fifth (2.5) of the PN biochemical cell chamber to the ninth (2.9) of the PN biochemical cell chamber is 5.2 to 28.1mg N/L; the FNA concentration of PN biochemical cell I (2.1) to PN biochemical cell IV (2.4) is lower than 0.07mg N/L, and the FNA concentration of PN biochemical cell V (2.5) to PN biochemical cell VI (2.9) is lower than 0.22mg N/L; the operation is carried out according to the conditions, so that the nitrite accumulation rate of the effluent of the PN biochemical pool (2) is more than 90.0 percent, and NH is added 4 + -N removal greater than 60%; (2) constructing a shortcut nitrification coupling anaerobic ammonia oxidation PNA system:
a biomembrane carrier (5.23) with the relative abundance of anaerobic ammonium oxidation bacteria of more than 10.0 percent is inoculated in the PNA biochemical pool (5), and the biomembrane carrier (5.23) is fixed on a biomembrane carrier fixing frame (5.24), and the filling ratio is 20.0 +/-2.0 percent; inoculating the residual sludge after the primary biochemical treatment into a PNA biochemical pool (5) to ensure that the concentration of floc sludge is 2000-2500 mg/L and the sludge reflux ratio is 200 percent; the water temperature of the PNA biochemical pool (5) is 30 +/-1 ℃; the dissolved oxygen concentration of the PNA biochemical pool cell III (5.3), the PNA biochemical pool cell VI (5.6) and the PNA biochemical pool cell nine (5.9) is 0.1-0.2 mg/L; raw leachate water and primary biochemical treatment effluent 1 are arranged in the secondary regulating tank (4): 1, the mixed solution is continuously pumped into a first PNA biochemical pool cell (5.1), a fourth PNA biochemical pool cell (5.4) and a seventh PNA biochemical pool cell (5.7) in sections according to the flow ratio of 1 3 Increasing the volume of/d to 0.25kg N/m 3 The step water inlet strategy aims to relieve the inhibition of FA on the AnAOB and improve the utilization efficiency of organic matters in inlet water; PNA biochemical pool cell I, II, IV, V, VII, VIII (5.1, 5.2,5.4,5.5,5.7, 5.8) pH 7.6-7.9, FA concentration 7.8-14.6 mg N/L, FNA concentration less than 0.01mg N/L; PNA biochemical pool cell three, six, nine (5.3, 5.6, 5.9) pH 6.9-7.2, FA concentration 0-1.0 mg N/L, FNA concentration less than 0.005mg N/L; the operation is carried out according to the conditions, so that the total inorganic nitrogen concentration in the effluent of the PNA biochemical pool (5) is lower than 60.0mg/L, and NH is generated 4 + -N concentration lower than 10.0mg/L, COD lower than 2200mg/L; (3) PN biochemical pool (2), PNA biochemical pool (5) and DE biochemical pool (8) are connected in series for operation:
sodium acetate solution with the mass fraction of 15 percent enters a third-stage regulating tank (7) and a second-stage biochemical treatment tank through an external carbon source feeding pump (7.1) and an external carbon source feeding pipeline (7.2)The treated effluent is mixed according to the flow ratio of 1 3 - The concentration of-N is 20.0-50.0 mg/L; the sludge concentration of the DE biochemical pool (8) is 4000 +/-500 mg/L, and the sludge reflux ratio is 100 percent; dissolved oxygen in an aerobic zone (8.9) of the DE biochemical tank is 2.0-3.0 mg/L, and the pH value is 7.0-7.5; the pH value of an anoxic zone (8.8) of the DE biochemical pool is 7.5-8.0; the operation is carried out according to the conditions, so that the total inorganic nitrogen of the effluent of the three-stage biochemical treatment is lower than 15.0mg/L and NH 4 + -N concentration lower than 1.5mg/L;
(4) Starting system effluent backflow:
the effluent of the three-stage biochemical treatment enters a first-stage regulating reservoir (1) through an effluent reflux pump (9.5) and an effluent reflux pipeline (9.6), and the raw water of the leachate is 1:1 flow ratio is mixed and is used as the inlet water of the PN biochemical pool (2);
(5) Adjusting the operation parameters of the PN biochemical pool (2):
the inlet water of the PN biochemical pool (2) is a mixed solution (1.2) of raw leachate and outlet water 1 of three-stage biochemical treatment, the total inorganic nitrogen concentration is 1000.0 +/-100.0 mg/L, and NH is generated by the reaction of the raw leachate and the outlet water 1 4 + The concentration of N is 990.0 +/-100.0 mg/L, and the COD is 2700.0 +/-200.0 mg/L, so that the inhibition of FA on AOB and denitrifying bacteria is reduced; because the ammonia nitrogen concentration of the inlet water of the PN biochemical pool (2) is reduced and the FA concentration of the unit is also reduced, the sludge reflux ratio is reduced from 300 percent to 200 percent so as to save energy consumption; the pH value from the first cell (2.1) of the PN biochemical cell to the fourth cell (2.4) of the PN biochemical cell is 7.7 to 8.0, the FA concentration is 16.1 to 30.8mg N/L, and the FNA concentration is lower than 0.02mg N/L; the pH value from the fifth (2.5) cell chamber of the PN biochemical pool to the ninth (2.9) cell chamber of the PN biochemical pool is 7.0 to 7.5, the FA concentration is 0.8 to 8.7mg N/L, the FNA concentration is 0.03 to 0.17mg N/L, and the dissolved oxygen is 3.0 to 7.0mg/L; the operation is carried out according to the conditions, so that the ammonia nitrogen oxidation rate is more than 90%, and the nitrite accumulation rate is more than 90.0%.
The experimental results show that: when the three-stage plug-flow PN-PNA-DE process is adopted to treat the late landfill leachate, the total inorganic nitrogen concentration of the influent water is 2000.0 +/-200.0 mg/L, and NH is generated 4 + Total inorganic nitrogen and NH when the-N concentration is 1980.0 +/-200.0 mg/L and the COD is 3370.0 +/-200.0 mg/L 4 + The removal rates of-N and COD can respectively reach 99.0%, 99.9% and 50.0%.
The device and method for treating late landfill leachate by using the three-stage plug-flow PN-PNA-DE process provided by the present invention are introduced in detail, and the principle and the embodiment of the present invention are explained by applying specific examples, which are only used for assisting in understanding the method and the core idea of the present invention. Variations in the detailed description which follow will be apparent to those skilled in the art upon practicing the methods and concepts of the invention. Accordingly, the subject matter of this specification should not be construed as limiting the invention.
Claims (1)
1. The method for treating the late landfill leachate by the three-stage plug-flow PN-PNA-DE process is characterized by comprising the following steps of: the device used in the method comprises a primary regulating tank (1); a PN biochemical pool (2); a primary sedimentation tank (3); a secondary regulating tank (4); a PNA biochemical pool (5); a secondary sedimentation tank (6); a third-stage regulating tank (7); a DE biochemical pool (8); a third-stage sedimentation tank (9);
wherein, a PN biochemical pool water inlet pump (2.10) continuously pumps leachate raw water and mixed solution (1.2) of three-level biochemical treatment effluent 1 from a first-level regulating pool (1) through a PN biochemical pool water inlet pipeline (2.11) into a PN biochemical pool cell I (2.1) to be mixed with activated sludge, and the mixed solution flows out of a PN biochemical pool cell II (2.9) and enters a PN biochemical pool water outlet pipeline (2.19) and a first-level sedimentation pool (3); after precipitation, supernatant enters a secondary regulating tank (4) through a primary biochemical treatment water outlet pump (4.3) and a primary biochemical treatment water outlet pipeline (3.1), and sludge in the primary sedimentation tank (3) flows back to a PN biochemical pool grid chamber I (2.1) through a primary sludge return pump (3.2) and a primary sludge return pipeline (3.3); raw leachate is pumped into a secondary regulating reservoir (4) through a secondary regulating reservoir water inlet pump (4.1) and a secondary regulating reservoir water inlet pipeline (4.2) to be mixed with effluent of primary biochemical treatment; mixed liquid in the secondary regulating tank (4) respectively enters a PNA biochemical pool cell first (5.1), a PNA biochemical pool cell fourth (5.4) and a PNA biochemical pool cell seventh (5.7) of the PNA biochemical pool (5) through a PNA biochemical pool water inlet pump I (5.10) and a PNA biochemical pool water inlet pipeline I (5.11), a PNA biochemical pool water inlet pump II (5.12) and a PNA biochemical pool water inlet pipeline II (5.13), a PNA biochemical pool water inlet pump III (5.14) and a PNA biochemical pool water inlet pipeline III (5.15); the sludge-water mixed liquid of the PNA biochemical tank (5) enters a secondary sedimentation tank (6) through a PNA biochemical tank water outlet pipeline (5.25); after precipitation, supernatant in the secondary sedimentation tank (6) enters a tertiary regulating tank (7) through a secondary biochemical treatment water outlet pipeline (6.1); sludge at the bottom of the secondary sedimentation tank (6) flows back to a PNA biochemical tank cell I (5.1) through a secondary sludge return pump (6.2) and a secondary sludge return pipeline (6.3); sodium acetate solution enters a third-stage regulating tank (7) through an external carbon source feeding pump (7.1) and an external carbon source feeding pipeline (7.2) to be mixed with effluent of the second-stage biochemical treatment; the mixed liquid in the third-stage regulating tank (7) enters the front end of an anoxic zone (8.8) of the DE biochemical tank through a DE biochemical tank water inlet pump (8.1) and a DE biochemical tank water inlet pipeline (8.2), and water is discharged from the tail end of an aerobic zone (8.9) of the DE biochemical tank and enters a third-stage sedimentation tank (9) through a DE biochemical tank water outlet pipeline (8.10); after precipitation, 50% of the supernatant enters a water outlet pipeline (9.1) of the three-stage biochemical treatment, and 50% of the supernatant enters a first-stage regulating tank (1) through a water outlet reflux pump (9.5) and a water outlet reflux pipeline (9.6); the sludge in the third-stage sedimentation tank (9) flows back to an anoxic zone (8.8) of the DE biochemical tank through a third-stage sludge return pump (9.3) and a third-stage sludge return pipeline (9.4);
in addition, the primary regulating tank (1) also comprises a percolate raw water pipeline (1.1); the PN biochemical pool (2) further comprises a PN biochemical pool cell II (2.2), a PN biochemical pool cell III (2.3), a PN biochemical pool cell IV (2.4), a PN biochemical pool cell V (2.5), a PN biochemical pool cell VI (2.6), a PN biochemical pool cell seven (2.7), a PN biochemical pool cell eight (2.8), a PN biochemical pool temperature control device (2.12), a PN biochemical pool heating device (2.13), a PN biochemical pool pH and DO real-time monitoring device (2.14), a PN biochemical pool mechanical stirrer (2.15), a PN biochemical pool aeration device (2.16), a PN biochemical pool gas flow meter (2.17) and a PN biochemical pool microporous aeration disc (2.18); the primary sedimentation tank also comprises a primary biochemical treatment residual sludge discharge pipeline (3.4); the PNA biochemical pool (5) further comprises a PNA biochemical pool cell II (5.2), a PNA biochemical pool cell III (5.3), a PNA biochemical pool cell IV (5.4), a PNA biochemical pool cell V (5.5), a PNA biochemical pool cell VI (5.6), a PNA biochemical pool cell VII (5.7), a PNA biochemical pool cell VIII (5.8), a PNA biochemical pool cell nine (5.9), a PNA biochemical pool temperature control device (5.16), a PNA biochemical pool heating device (5.17), a PNA biochemical pool pH and DO real-time monitoring device (5.18), a PNA biochemical pool mechanical stirrer (5.19), a PNA biochemical pool aeration device (5.20), a biochemical PNA pool gas flow meter (5.21), a PNA biochemical pool microporous aeration disc (5.22), a biological membrane carrier (5.23) and a biological membrane carrier fixing frame (5.24); the DE biochemical tank (8) further comprises a pH and DO real-time monitoring device (8.3) of the DE biochemical tank, a mechanical stirrer (8.4) of the DE biochemical tank, an aeration device (8.5) of the DE biochemical tank, a gas flowmeter (8.6) of the DE biochemical tank and a microporous aeration disc (8.7) of the DE biochemical tank; the third-stage sedimentation tank (9) also comprises a third-stage biochemical treatment residual sludge discharge pipeline (9.2);
the method comprises the following steps:
(1) Starting the PN biochemical pool (2):
the water temperature of the PN biochemical pool (2) is 30 +/-1 ℃; the sludge concentration is that MLSS is 4500 + -500 mg/L, the sludge reflux ratio is 300%; dissolved oxygen from PN biochemical pool cell five (2.5) to PN biochemical pool cell nine (2.9) is 3.0-7.0 mg/L; the inlet water of the PN biochemical pool (2) is percolate raw water, the total inorganic nitrogen concentration is 2000.0 +/-200.0 mg/L, and NH 4 + The concentration of N is 1980.0 +/-200.0 mg/L, and the COD is 3370.0 +/-200.0 mg/L; the pH value from PN biochemical pool cell I (2.1) to PN biochemical pool cell IV (2.4) is 7.6-7.8, and the pH value from PN biochemical pool cell V (2.5) to PN biochemical pool cell V (2.9) is 7.2-7.8; the FA concentration from the first PN biochemical pool cell (2.1) to the fourth PN biochemical pool cell (2.4) is 25.0-40.0 mg N/L, and the FA concentration from the fifth PN biochemical pool cell (2.5) to the ninth PN biochemical pool cell (2.9) is 5.2-28.1 mg N/L; FNA concentration from PN biochemical pool cell I (2.1) to PN biochemical pool cell IV (2.4) is lower than 0.07mg N/L, and FNA concentration from PN biochemical pool cell V (2.5) to PN biochemical pool cell VI (2.9) is lower than 0.22mg N/L; the operation is carried out according to the conditions, so that the nitrite accumulation rate of the effluent of the PN biochemical pool (2) is more than 90.0 percent, and NH is added 4 + -N removal greater than 60%;
(2) Constructing a shortcut nitrification coupled anaerobic ammonia oxidation PNA system:
a biomembrane carrier (5.23) with the relative abundance of anaerobic ammonium oxidation bacteria of more than 10.0 percent is inoculated in the PNA biochemical pool (5), and the biomembrane carrier (5.23) is fixed on a biomembrane carrier fixing frame (5.24), and the filling ratio is 20.0 +/-2.0 percent; inoculating the excess sludge of the first-stage biochemical treatment into a PNA biochemical tank (5) to ensure that the concentration of floc sludge is 2000-2500 mg/L and the reflux ratio of the sludge is 200 percent; the water temperature of the PNA biochemical pool (5) is 30 +/-1 ℃; PNA Biochemical pool cell III (5.3), PNA BiochemicalThe dissolved oxygen concentration of the cell six (5.6) and the PNA biochemical cell nine (5.9) is 0.1-0.2 mg/L; the secondary regulating tank (4) is internally provided with raw water of percolate and effluent of primary biochemical treatment 1:1 at a flow ratio of 1 3 Increasing the value of/d to 0.25kg N/m 3 D; PNA biochemical pool cell I, II, IV, V, VII, VIII (5.1, 5.2,5.4,5.5,5.7, 5.8) pH 7.6-7.9, FA concentration 7.8-14.6 mg N/L, FNA concentration less than 0.01mg N/L; PNA biochemical pool cell three, six, nine (5.3, 5.6, 5.9) pH 6.9-7.2, FA concentration 0-1.0 mg N/L, FNA concentration less than 0.005mg N/L; the operation is carried out according to the conditions, so that the total inorganic nitrogen concentration in the effluent of the PNA biochemical pool (5) is lower than 60.0mg/L, and NH is generated 4 + -N concentration lower than 10.0mg/L, COD lower than 2200mg/L;
(3) PN biochemical pool (2), PNA biochemical pool (5) and DE biochemical pool (8) are connected in series for operation:
sodium acetate solution with mass fraction of 15 percent enters a third-stage regulating tank (7) through an external carbon source feeding pump (7.1) and an external carbon source feeding pipeline (7.2) to be mixed with effluent of secondary biochemical treatment according to the flow ratio of 1 3 - The concentration of N is 20.0-50.0 mg/L; the sludge concentration of the DE biochemical pool (8) is 4000 +/-500 mg/L, and the sludge reflux ratio is 100 percent; the dissolved oxygen of the aerobic zone (8.9) of the DE biochemical tank is 2.0-3.0 mg/L, and the pH value is 7.0-7.5; the pH value of an anoxic zone (8.8) of the DE biochemical pool is 7.5-8.0; the operation is carried out according to the conditions, so that the total inorganic nitrogen of the effluent of the three-stage biochemical treatment is lower than 15.0mg/L and NH 4 + -N concentration lower than 1.5mg/L;
(4) Starting effluent backflow:
the effluent of the three-stage biochemical treatment enters a first-stage regulating reservoir (1) through an effluent reflux pump (9.5) and an effluent reflux pipeline (9.6), and the raw water of the leachate is 1:1, mixing in a flow ratio;
(5) Adjusting the operating parameters of the PN biochemical pool (2):
the water temperature of the PN biochemical pool (2) is 30 +/-1 ℃; the sludge concentration is that MLSS is 4500 + -500 mg/L, the sludge reflux ratio is reduced from 300% to 200%; PN biochemical pool (2) inletThe water is a mixed solution (1.2) of raw leachate and effluent of three-stage biochemical treatment 1, the total inorganic nitrogen concentration is 1000.0 +/-100.0 mg/L, and NH is generated 4 + The concentration of N is 990.0 +/-100.0 mg/L, and the COD is 2700.0 +/-200.0 mg/L; the pH value from the PN biochemical cell I (2.1) to the PN biochemical cell IV (2.4) is 7.7-8.0, the FA concentration is 16.1-30.8 mg N/L, and the FNA concentration is lower than 0.02mg N/L; the pH value from PN biochemical cell five (2.5) to PN biochemical cell nine (2.9) is 7.0-7.5, the FA concentration is 0.8-8.7 mg N/L, the FNA concentration is 0.03-0.17 mg N/L, and the dissolved oxygen is 3.0-7.0 mg/L.
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