A H C R -A 2 O Wastewater treatment system and wastewater treatment method

Abstract

An A H C R -A 2 O sewage treatment system, comprising: an anaerobic tank, a biological adsorption hydrolysis-clarification and redistribution tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank. A new biological adsorption hydrolysis-clarification and redistribution tank is provided. After the sewage is mixed with the external reflux sludge, pollutants are rapidly adsorbed and partially hydrolyzed, and settle to the bottom of the tank body, and the supernatant is collected in the upper part of the tank body. The supernatant outlet is respectively connected to the anoxic tank and the aerobic tank and selectively conducted, and the bottom sludge outlet is connected to the anoxic tank. In the sewage treatment method: according to the preset value of the supernatant turbidity, it is selected to flow into the aerobic tank or the anoxic tank, and the bottom sludge is introduced into the anoxic tank. The present invention can improve the nitrogen and phosphorus removal efficiency of a single activated sludge system, improve the utilization rate of the internal carbon source in sewage, reduce the consumption of the external carbon source. When the influent COD / TN≈5, the effluent TN≤10mg / L, the external carbon source does not need to be added, the tank volume is reduced by more than 10%, and it is applicable to the upgrading transformation of the high discharge standard of sewage treatment plants, realizing the functions of improving quality, increasing efficiency and reducing consumption.

Description

Technical Field

[0001] The present invention relates to the technical field of sewage treatment, and in particular to a H C R -A 2 O Sewage treatment systems and sewage treatment methods. Background Art

[0002] A 2 The O process is based on the traditional theory of nitrogen and phosphorus removal, and different functional units are set according to the characteristics of different functional bacteria. Among them, the anaerobic unit releases phosphorus through polyphosphate bacteria, the anoxic unit uses denitrifying bacteria to complete denitrification, and the aerobic unit performs nitrification and phosphate absorption. 2 The O process is widely used because it takes into account both nitrogen removal and phosphorus removal functions and has stable effects.

[0003] But A 2 The O process still has some shortcomings: (1) The contradiction between nitrogen removal and phosphorus removal. The sludge ages of denitrification and phosphorus removal microorganisms are different, and there is competition for carbon sources between polyphosphate bacteria and denitrifying bacteria; (2) When the nitrification liquid is refluxed, the reflux ratio is generally controlled at 100-300%. Too high a reflux ratio will cause residual dissolved oxygen to destroy the anoxic environment, resulting in a decrease in denitrification efficiency; (3) my country's sewage has a low C / N ratio and insufficient carbon source, which limits the denitrification capacity. In particular, it is more difficult for comprehensive sewage treatment plants that receive industrial wastewater to meet emission standards. Research on low-carbon nitrogen removal and phosphorus removal processes has always been a difficult and hot topic in process research.

[0004] In order to reduce the amount of external carbon source added, some studies have reported the primary sludge hydrolysis process, which aims to make full use of the influent carbon source. This method requires controlling the hydrolysis process to stably produce acid without producing methane, and the hydrolysis product needs to undergo an additional "mud-water" secondary separation, which has the disadvantage of SCOD and VFAs being removed from the sludge-water mixture. In addition, there are also studies that use side stream residual sludge hydrolysis to produce SCOD and VFAs to supplement the carbon source required for denitrification. However, this method has a low yield of SCOD and VFAs, and requires additional pool capacity and aeration.

[0005] The present invention aims to 2 In the O process, a biosorption hydrolysis-clarification redistribution tank (A H C R ), realize the hydrolysis function in the single sludge system, improve the utilization rate of carbon sources in sewage, reduce the consumption of external carbon sources, and greatly improve the denitrification and phosphorus removal efficiency of the single activated sludge system. At the same time, it overcomes the shortcomings of the above methods and achieves quality improvement, efficiency increase, energy saving and consumption reduction in the process of upgrading the high emission standards of sewage treatment plants. Summary of the invention

[0006] To overcome the shortcomings of the background technology, the present invention provides a H C R-A 2 O Sewage treatment systems and sewage treatment methods.

[0007] In order to achieve the above-mentioned object of the invention, the present invention adopts the following technical solutions:

[0008] A of the present invention H C R -A 2 A sewage treatment system, comprising: an anaerobic tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank, wherein the sewage to be treated enters the anaerobic tank, the anoxic tank, the aerobic tank and the secondary sedimentation tank are connected in sequence, an internal reflow is arranged between the aerobic tank and the anoxic tank, an external reflow is arranged between the secondary sedimentation tank and the anaerobic tank, the secondary sedimentation tank discharges the treated effluent and the residual sludge, and further comprises a biological adsorption hydrolysis-clarification redistribution tank, the biological adsorption hydrolysis-clarification redistribution tank comprises a tank body, an inlet pipe, a supernatant outlet and a bottom mud outlet, the inlet pipe, the supernatant outlet and the bottom mud outlet are respectively arranged on the tank body, the above-mentioned inlet pipe is connected with the outlet of the anaerobic tank, the sewage treated in the anaerobic tank enters the biological adsorption hydrolysis-clarification redistribution tank, the supernatant outlet is arranged at the upper part of the tank body, the bottom mud outlet is arranged at the lower part of the tank body, the supernatant outlet is respectively connected with the anoxic tank and the aerobic tank and selectively conducted, and the bottom mud outlet is connected with the anoxic tank.

[0009] This technical solution can also adopt the following technical measures:

[0010] When the turbidity of the supernatant drawn out from the supernatant outlet is not higher than the preset value, the supernatant outlet is connected to the aerobic tank, and the supernatant flows into the aerobic tank; when the turbidity of the supernatant drawn out from the supernatant outlet is higher than the preset value, the supernatant outlet is connected to the anoxic tank and the aerobic tank, and the supernatant is diverted to the anoxic tank and the aerobic tank.

[0011] According to the direction of sewage treatment in the pool, the interior of the anoxic pool is divided into the front section and the rear section of the anoxic pool, and the interior of the aerobic pool is divided into the front section, the middle section and the rear section of the aerobic pool; the supernatant outlet of the biological adsorption hydrolysis-clarification redistribution pool is connected to the rear section of the anoxic pool and the front section of the aerobic pool respectively, the sludge outlet is connected to the front section of the anoxic pool, and the rear section of the aerobic pool is connected to the front section of the anoxic pool.

[0012] An internal flow channel and a stirrer are arranged in the biosorption hydrolysis-clarification redistribution tank.

[0013] A of the present invention H C R -A 2 O sewage treatment method, comprising the following steps:

[0014] A. The sewage to be treated enters the anaerobic tank and is mixed with the external return liquid from the secondary sedimentation tank for anaerobic treatment;

[0015] B. The sewage treated in the anaerobic tank enters the biosorption hydrolysis-clarification redistribution tank through the water inlet pipe, where it undergoes biosorption, hydrolysis and clarification. After treatment, the upper part of the tank body gathers to form a supernatant, and the bottom of the tank body gathers to form a bottom sludge;

[0016] C. When the turbidity of the supernatant liquid drawn from the supernatant liquid outlet is not higher than the preset value, the supernatant liquid outlet is connected to the aerobic tank, the supernatant liquid flows into the aerobic tank, the sludge drawn from the biological adsorption hydrolysis-clarification redistribution tank and the internal reflux liquid drawn from the aerobic tank are mixed in the anoxic tank, and denitrification treatment is carried out; when the supernatant liquid turbidity is higher than the preset value, the supernatant liquid outlet is connected to the anoxic tank and the aerobic tank, the supernatant liquid is diverted to the anoxic tank and the aerobic tank, the sludge drawn from the biological adsorption hydrolysis-clarification redistribution tank, part of the supernatant liquid and the internal reflux liquid drawn from the aerobic tank are mixed in the anoxic tank, and denitrification treatment is carried out;

[0017] D. The sewage and sludge treated in the anoxic tank enter the aerobic tank, are mixed with the supernatant drawn from the biosorption hydrolysis-clarification redistribution tank, and are nitrified. The aerobic tank and the anoxic tank form an internal reflux;

[0018] E. The sewage and sludge treated in the aerobic tank enter the secondary sedimentation tank. An external reflux is formed between the secondary sedimentation tank and the anaerobic tank. The secondary sedimentation tank discharges the treated water and residual sludge.

[0019] The preset value of the turbidity of the supernatant discharged from the biosorption hydrolysis-clarification redistribution tank may be 40-60 NTU.

[0020] The preset value of the turbidity of the supernatant discharged from the biosorption hydrolysis-clarification redistribution tank is 50 NTU.

[0021] According to the direction of sewage treatment in the pool, the interior of the anoxic pool is divided into the front section and the rear section of the anoxic pool, and the interior of the aerobic pool is divided into the front section, the middle section and the rear section of the aerobic pool; when the turbidity of the supernatant liquid discharged from the supernatant liquid outlet of the biological adsorption hydrolysis-clarification redistribution pool is not higher than the preset value, it flows into the front section of the aerobic pool; when the turbidity of the supernatant liquid is higher than the preset value, the supernatant liquid flows into the rear section of the anoxic pool and the front section of the aerobic pool, the sludge discharge outlet is connected to the front section of the anoxic pool, and the rear section of the aerobic pool is connected to the front section of the anoxic pool to form an internal reflux.

[0022] The redox potential value ORP of the anaerobic tank is -250~-100mV, the ORP of the anoxic tank is -200~50mV, and the dissolved oxygen of the aerobic tank is 0.5-2.0mg / L; the ORP at the bottom of the biosorption hydrolysis-clarification redistribution tank is -350~-200mV; the sediment flow rate Q of the biosorption hydrolysis-clarification redistribution tank is 底泥 The sewage flow Q into the anaerobic tank 进The ratio is 0.9 to 1.2, and the supernatant flow Q 上清 The sewage flow Q into the anaerobic tank 进 The ratio is 0.80 to 1.1, and the internal reflux flow rate Q from the aerobic pool to the anoxic pool 内 The sewage flow Q into the anaerobic tank 进 The ratio is 1.6 to 2, and the external return liquid flow rate Q from the secondary sedimentation tank to the anaerobic tank 外 The sewage flow Q into the anaerobic tank 进 The ratio is 0.8~1.

[0023] A of the present invention H C R -A 2 O sewage treatment system, including: biological adsorption hydrolysis-clarification redistribution tank, anoxic tank, aerobic tank and secondary sedimentation tank. The biological adsorption hydrolysis-clarification redistribution tank includes a tank body, an inlet pipe, a supernatant outlet and a sludge outlet. The inlet pipe, the supernatant outlet and the sludge outlet are respectively arranged on the tank body. The supernatant outlet is arranged at the upper part of the tank body, and the sludge outlet is arranged at the lower part of the tank body. The sewage to be treated enters the biological adsorption hydrolysis-clarification redistribution tank through the inlet pipe. The supernatant outlet is respectively connected to the anoxic tank and the aerobic tank and selectively conducted. The sludge outlet is connected to the anoxic tank; the anoxic tank, the aerobic tank and the secondary sedimentation tank are connected in sequence. An internal reflux is arranged between the aerobic tank and the anoxic tank. An external reflux is arranged between the secondary sedimentation tank and the biological adsorption hydrolysis-clarification redistribution tank. The secondary sedimentation tank discharges the treated effluent and the residual sludge. (3) The sewage to be treated is introduced into the anaerobic tank A P In the biosorption hydrolysis-clarification redistribution tank (A H C R ) Water inlet pipe 1 and anaerobic tank A P The outlet is connected to the bottom mud outlet 4 and the anoxic section A N,P1 The supernatant outlet 2 is connected to the aerobic section O1 (it can also be connected to the anoxic section A N,P2 The aerobic section O4 and the secondary sedimentation tank S are connected in sequence, and the aerobic section O4 and the anoxic section A N,P1 Internal recirculation is established between the secondary sedimentation tank S and the anaerobic tank A P An external recirculation is established, and the secondary sedimentation tank S discharges the treated effluent and residual sludge.

[0024] Due to the adoption of the above-mentioned technical solution, the present invention has the following beneficial effects:

[0025] A of the present invention H C R -A 2 In the sewage treatment system and sewage treatment method, full consideration is given to the reasonable distribution of pollutants among the pools and the utilization of carbon sources in the sewage to improve the nitrogen and phosphorus removal effects. 2In the O process, a biological adsorption hydrolysis-clarification redistribution tank is set up. After the sewage and the external return sludge are mixed, the mud and water are separated in the clarification separation process; the concentrated sludge is sent to the anoxic tank for denitrification, and the supernatant is redistributed to the aerobic tank to complete nitrification. After the sewage from the anaerobic tank is treated in the biological adsorption hydrolysis-clarification redistribution tank, the supernatant is redistributed to the aerobic tank. At this time, there is no external water dilution in the anoxic tank, which cleverly resolves the A 2 In the O process, the sludge concentration in the anoxic tank is reduced due to dilution by the influent, which can increase the sludge concentration in the anoxic tank to 5000-8000 mg / L, greatly improving the denitrification efficiency. In addition, since the bottom of the clarification and separation zone is in an anaerobic state, microorganisms can hydrolyze some macromolecular organic matter, thereby 2 In the single activated sludge system, the anaerobic hydrolysis function is successfully coupled. In the anaerobic metabolism, microorganisms capture and transform a large amount of carbon sources in the sewage, and can achieve synchronous denitrification, denitrification and phosphorus removal in the subsequent anoxic tank. The clarification and separation process is controllable, and the mud and water separation effect is significant. The supernatant is redistributed to the aerobic tank to ensure the nitrification effect of the total Kjeldahl nitrogen in the sewage and reduce aeration energy consumption.

[0026] The present invention can greatly improve the efficiency of nitrogen removal and phosphorus removal in the single activated sludge system, increase the utilization rate of carbon sources in sewage, and reduce the consumption of external carbon sources. When the influent COD / TN is ≈ 5, the effluent TN is ≤ 10 mg / L, no external carbon source needs to be added, the tank volume is reduced by more than 10%, and there is no secondary pollution. It is suitable for the transformation of sewage treatment plants with high emission standards to achieve quality improvement, efficiency increase, energy saving and consumption reduction. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a schematic diagram of the structure of the biosorption hydrolysis-clarification redistribution tank of the present invention;

[0028] Figure 2 A of the present invention H C R -A 2 OSchematic diagram of the sewage treatment system;

[0029] Figure 3 A of the present invention H C R -A 2 O Schematic diagram of another architecture of sewage treatment system. DETAILED DESCRIPTION

[0030] The present invention can be explained in detail by the following examples, and the purpose of disclosing the present invention is to protect all technical improvements within the scope of the present invention.

[0031] like Figure 1 and Figure 2 As shown, A of the present invention H C R -A 2O Wastewater treatment system, including anaerobic tank A p 、Anoxic pool A N,P , aerobic tank O and secondary sedimentation tank S, sewage to be treated Q 进 Entering the anaerobic tank, the anoxic tank, the aerobic tank, and the secondary sedimentation tank are connected in sequence. An internal return is set between the aerobic tank and the anoxic tank, and an external return is set between the secondary sedimentation tank and the anaerobic tank. The secondary sedimentation tank will treat the effluent Q 出 and excess sludge Q 剩 Discharge, also includes biosorption hydrolysis-clarification redistribution tank A H C R , Biosorption Hydrolysis-Clarification Redistribution Tank A H C R It includes a tank body, a water inlet pipe 1, a supernatant outlet 2 and a bottom mud outlet 4. The water inlet pipe, the supernatant outlet and the bottom mud outlet are respectively arranged on the tank body. The water inlet pipe is arranged in the middle of the tank body and connected to the outlet of the anaerobic tank. The sewage treated in the anaerobic tank enters the biological adsorption hydrolysis-clarification redistribution tank. The supernatant outlet is arranged in the upper part of the tank body, and the bottom mud outlet is arranged in the lower part of the tank body. The supernatant outlet is respectively connected to the anoxic tank and the aerobic tank and selectively conducted, and the bottom mud outlet is connected to the anoxic tank. An internal flow channel and a stirrer 3 are arranged in the biological adsorption hydrolysis-clarification redistribution tank. The water flows in the internal flow channel of the tank body to increase the residence time. The stirrer is arranged in the middle of the tank body to stir the sewage.

[0032] The supernatant Q drawn out from the supernatant outlet 上清 When the turbidity is not higher than the preset value, the supernatant outlet is connected to the aerobic tank, and the supernatant Q 上清 Flows into the aerobic pool; when the turbidity of the supernatant discharged from the supernatant outlet is higher than the preset value, the supernatant outlet is connected to the anoxic pool and the aerobic pool, and the supernatant Q 上清 Divide into the anoxic pool and the aerobic pool. The preset value of turbidity can be selected between 40-60NTU depending on the situation. For example, the preset value of turbidity can be selected as 50NTU. When the turbidity of the supernatant is less than 50NTU, all the supernatant flows into the aerobic pool. When the turbidity of the supernatant is greater than 50NTU, 30% of the supernatant flow flows into the anoxic pool, and at the same time 70% of the supernatant flows into the aerobic pool. The diversion of the supernatant flow between the anoxic pool and the aerobic pool can be modified and set according to the situation.

[0033] According to the direction of sewage treatment in the pool, the anoxic pool A is divided into N,P The interior is divided into the anoxic pool anterior segment A N,P1 and the posterior segment of the anoxic pool A N,P2 , the aerobic pool O is divided into the front section of the aerobic pool O1, the middle section of the aerobic pool O2, O3 and the rear section of the aerobic pool O4; the biosorption hydrolysis-clarification redistribution pool A HC R The supernatant outlet is connected to the rear section of the anoxic tank and the front section of the aerobic tank respectively, the sediment outlet is connected to the front section of the anoxic tank, and the rear section of the aerobic tank is connected to the front section of the anoxic tank.

[0034] A of the present invention H C R -A 2 O sewage treatment method, comprising the following steps:

[0035] A. The sewage to be treated enters the anaerobic tank and mixes with the external return liquid Q from the secondary sedimentation tank. 外 Mixing and anaerobic treatment;

[0036] B. The sewage treated in the anaerobic tank enters the biosorption hydrolysis-clarification redistribution tank through the water inlet pipe, where it undergoes biosorption, hydrolysis and clarification. After treatment, the upper part of the tank body gathers to form a supernatant, and the bottom of the tank body gathers to form a bottom sludge;

[0037] C. When the turbidity of the supernatant liquid drawn from the supernatant liquid outlet is not higher than the preset value, the supernatant liquid outlet is connected to the aerobic tank, and the supernatant liquid flows into the aerobic tank. The sludge drawn from the biosorption hydrolysis-clarification redistribution tank and the internal reflux liquid Q drawn from the aerobic tank are 内 Mix in the anoxic tank and perform denitrification treatment; when the turbidity of the supernatant is higher than the preset value, the supernatant outlet is connected to the anoxic tank and the aerobic tank, the supernatant is diverted to the anoxic tank and the aerobic tank, the bottom mud led out of the biosorption hydrolysis-clarification redistribution tank, part of the supernatant and the internal reflux liquid led out of the aerobic tank are mixed in the anoxic tank and perform denitrification treatment;

[0038] D. The sewage and sludge treated in the anoxic tank enter the aerobic tank, are mixed with the supernatant drawn from the biosorption hydrolysis-clarification redistribution tank, and are nitrified. The aerobic tank and the anoxic tank form an internal reflux;

[0039] E. The sewage and sludge treated in the aerobic tank enter the secondary sedimentation tank. An external reflux is formed between the secondary sedimentation tank and the anaerobic tank. The secondary sedimentation tank discharges the treated water and residual sludge.

[0040] The preset value of the turbidity of the supernatant discharged from the biosorption hydrolysis-clarification redistribution tank may be 40-60 NTU.

[0041] The preset value of the turbidity of the supernatant discharged from the biosorption hydrolysis-clarification redistribution tank is 50 NTU.

[0042] According to the direction of sewage treatment in the pool, the interior of the anoxic pool is divided into the front section and the rear section of the anoxic pool, and the interior of the aerobic pool is divided into the front section, the middle section and the rear section of the aerobic pool; when the turbidity of the supernatant liquid discharged from the supernatant liquid outlet of the biological adsorption hydrolysis-clarification redistribution pool is not higher than the preset value, it flows into the front section of the aerobic pool; when the turbidity of the supernatant liquid is higher than the preset value, the supernatant liquid flows into the rear section of the anoxic pool and the front section of the aerobic pool, the sludge discharge outlet is connected to the front section of the anoxic pool, and the rear section of the aerobic pool is connected to the front section of the anoxic pool to form an internal reflux.

[0043] AC-A of the present invention 2 O sewage treatment process system and method, enters anaerobic tank A P The sewage flow is Q 进 , sewage in the AC-A 2 Total retention time of O treatment system HRT = 18-21 hours, external return to anaerobic tank A P , external reflux ratio 80-100%, internal reflux into the anoxic section A N,P1 , the internal reflux ratio is 160-200%. The HRT of the biosorption hydrolysis-clarification redistribution tank is 0.5-1 hour, and the enhanced hydrolysis zone (A H C R Pool bottom) ORP: -350-(-200)mV, bottom mud flow is 90-120%Q 进 , the supernatant flow rate is 80-110% Q 进 The DO of aerobic pool O is: 0.5-2.0mg / L; anaerobic pool A P ORP: -250-(-100)mV, anoxic pool A N,P ORP: -200-(50)mV; sludge concentration in biological system: 4000-5000mg / L, of which sludge concentration in anoxic tank: 5000-8000mg / L.

[0044] After biosorption hydrolysis-clarification redistribution tank (A H C R ) After that, when the turbidity of the supernatant is less than 50 NTU, all the supernatant enters the aerobic section O1, and the bottom mud enters the anoxic section A. N,P1 Front end; when the turbidity of the supernatant is greater than 50 NTU, the supernatant can be distributed proportionally into the anoxic section A N,P2 , aerobic section O1. The sludge directly enters the subsequent anoxic section.

[0045] Corresponding to AC-A based on adsorption, hydrolysis, clarification and redistribution of pollutants in sewage 2 The architecture of the sewage treatment process system and the specific sewage treatment implementation results are as follows:

[0046] Embodiment 1:

[0047] Influent TN = 28.09 mg / L, influent flow rate 580 L / h, HRT = 20 hrs, external reflow ratio 80%, internal reflow ratio 160%, sediment flow rate 110% Q 进 , the supernatant flow rate is 90% Q 进 The preset turbidity value is 50NTU, but the actual turbidity of the supernatant is 40NTU. All the supernatant enters the aerobic tank. The redox potential value ORP of the anaerobic tank is -250mV, the ORP of the anoxic tank is -200mV, and the dissolved oxygen of the aerobic tank is 1.5mg / L. The ORP of the bottom of the biosorption hydrolysis-clarification redistribution tank is -350mV, and the effluent NH4 + -N is below the detection limit (0.025mg / L), PO4 3- -P=0mg / L,TN=8.44mg / L,original A 2 The TN of the effluent after O process treatment is 14-15 mg / L; the TN of the effluent in this embodiment is significantly lower than the TN of the effluent from the original system, meeting the requirements for upgrading and transformation.

[0048] Embodiment 2:

[0049] Influent TN = 33.13 mg / L, influent flow rate 560 L / h, HRT = 21 hrs, external reflow ratio 100%, internal reflow ratio 200%, sediment flow rate 80% Q 进 , the supernatant flow rate is 120% Q 进 The preset turbidity value is 40NTU, the actual turbidity of the supernatant is 51NTU, 60% of the supernatant enters the aerobic tank, and 40% of the supernatant enters the anoxic tank. The redox potential value ORP of the anaerobic tank is -100mV, the ORP of the anoxic tank is 50mV, and the dissolved oxygen of the aerobic tank is 2.0mg / L; the ORP at the bottom of the biosorption hydrolysis-clarification redistribution tank is -200mV, and the effluent NH4 + -N is below the detection limit (0.025mg / L), PO4 3- -P=0mg / L,TN=9.85mg / L,original A 2 The TN of the effluent after O process treatment is 14-15 mg / L; the TN of the effluent in this embodiment is significantly lower than the TN of the effluent from the original system, meeting the requirements for upgrading and transformation.

[0050] Embodiment 3:

[0051] Influent TN = 34.47 mg / L, influent flow rate 650 L / h, HRT = 18 hrs, external reflow ratio 85%, internal reflow ratio 170%, sediment flow rate 95% Q 进 , the supernatant flow is 100% Q 进The preset turbidity value is 60NTU, and the actual turbidity of the supernatant is 42NTU. All the supernatant enters the aerobic tank. The redox potential value ORP of the anaerobic tank is -200mV, the ORP of the anoxic tank is -150mV, and the dissolved oxygen of the aerobic tank is 1.0mg / L; the ORP at the bottom of the biosorption hydrolysis-clarification redistribution tank is -300mV, and the effluent NH4 + -N is below the detection limit (0.025mg / L), PO4 3- -P=0mg / L,TN=8.54mg / L,original A 2 The TN of the effluent after O process treatment is 14-15 mg / L; the TN of the effluent in this embodiment is significantly lower than the TN of the effluent from the original system, meeting the requirements for upgrading and transformation.

[0052] Embodiment 4:

[0053] Influent TN = 34.37 mg / L, influent flow 610 L / h, HRT = 19 hrs, external reflow ratio 90%, internal reflow ratio 180%, sediment flow 100% Q 进 , the supernatant flow rate is 110% Q 进 The preset turbidity value is 55NTU, the actual turbidity of the supernatant is 65NTU, 30% of the supernatant enters the aerobic tank, 70% of the supernatant enters the anoxic tank, the redox potential value ORP of the anaerobic tank is -150mV, the ORP of the anoxic tank is -100mV, and the dissolved oxygen of the aerobic tank is 0.5mg / L; the ORP of the bottom of the biosorption hydrolysis-clarification redistribution tank is -250mV, and the effluent NH4 + -N is below the detection limit (0.025mg / L), PO4 3- -P=0mg / L,TN=8.95mg / L,original A 2 The TN of the effluent after O process treatment is 14-15 mg / L; the TN of the effluent in this embodiment is significantly lower than the TN of the effluent from the original system, meeting the requirements for upgrading and transformation.

[0054] Embodiment 5:

[0055] Influent TN = 30.47 mg / L, influent flow 600 L / h, HRT = 20 hrs, external reflow ratio 95%, internal reflow ratio 175%, sediment flow 90% Q 进 , the supernatant flow rate is 95% Q 进 The preset turbidity value is 60NTU, and the actual turbidity of the supernatant is 66NTU. 20% of the supernatant enters the aerobic tank, and 80% of the supernatant enters the anoxic tank. The redox potential value ORP of the anaerobic tank is -120mV, the ORP of the anoxic tank is -80mV, and the dissolved oxygen of the aerobic tank is 1.75mg / L; the ORP of the bottom of the biosorption hydrolysis-clarification redistribution tank is -230mV, and the effluent NH4 +-N is below the detection limit (0.025mg / L), PO4 3- -P=0mg / L,TN=10.34mg / L,original A 2 The TN of the effluent after process O treatment is 14-15 mg / L; although the TN of the effluent in this embodiment is higher than 10 mg / L, it is still significantly lower than the TN of the effluent from the original system, meeting the requirements for upgrading and transformation.

[0056] The present invention fully considers the reasonable distribution of pollutants among the pools and the utilization of carbon sources in the sewage to improve the nitrogen and phosphorus removal effects. 2 O process is equipped with biosorption hydrolysis-clarification redistribution (A H C R ) units and equipment. After the sewage and the external return sludge are mixed, the mud and water are separated in the clarification separation process; the concentrated sludge is sent to the anoxic tank for denitrification, and the supernatant is redistributed to the aerobic tank to complete nitrification.

[0057] Set up a biosorption hydrolysis-clarification redistribution tank (A H C R ) after the supernatant is distributed to the aerobic pool. Because the anoxic pool has no external water dilution, it can cleverly resolve the A 2 In the A process, the sludge concentration in the anoxic tank is reduced due to dilution by the influent, which can increase the sludge concentration in the anoxic tank to 5000-8000 mg / L, greatly improving the denitrification efficiency. In addition, since the bottom of the clarification and separation zone is in an anaerobic state, microorganisms can hydrolyze some macromolecular organic matter, which can be used in the A 2 In the single activated sludge process system, the anaerobic hydrolysis function is successfully coupled. In the anaerobic metabolism, microorganisms capture and transform a large amount of carbon sources in the sewage, and can achieve synchronous denitrification, denitrification and phosphorus removal in the subsequent anoxic tank. The clarification and separation process is controllable, and the mud and water separation effect is significant. The supernatant is redistributed to the aerobic tank to improve the nitrification effect of the total Kjeldahl nitrogen in the sewage and reduce the aeration energy consumption.

[0058] The AC-A method for adsorbing, hydrolyzing, clarifying and redistributing pollutants in sewage according to the present invention 2 O sewage treatment process system can greatly improve the efficiency of nitrogen and phosphorus removal in the single activated sludge system, improve the utilization rate of carbon sources in sewage, and reduce the consumption of external carbon sources. When the influent COD / TN≈5, the effluent TN≤10mg / L, no external carbon source needs to be added, the tank volume can be reduced by more than 10%, and there is no secondary pollution. It is suitable for the transformation of sewage plants with high emission standards to achieve quality improvement, efficiency increase, energy saving and consumption reduction.

[0059] like Figure 3 As shown, A of the present invention H C R -A 2 O sewage treatment system can also eliminate the original A 2The invention discloses an anaerobic tank in a sewage treatment system, and uses a biological adsorption hydrolysis-clarification redistribution tank as an anaerobic tank at the same time to realize the function of anaerobic treatment. The system comprises a biological adsorption hydrolysis-clarification redistribution tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank. The biological adsorption hydrolysis-clarification redistribution tank comprises a tank body, an inlet pipe, a supernatant outlet and a sludge outlet. The inlet pipe, the supernatant outlet and the sludge outlet are respectively arranged on the tank body. The supernatant outlet is arranged at the upper part of the tank body, and the sludge outlet is arranged at the lower part of the tank body. The sewage to be treated enters the biological adsorption hydrolysis-clarification redistribution tank through the inlet pipe. The supernatant outlet is respectively connected to the anoxic tank and the aerobic tank and selectively conducted, and the sludge outlet is connected to the anoxic tank; the anoxic tank, the aerobic tank and the secondary sedimentation tank are connected in sequence, an internal reflux is arranged between the aerobic tank and the anoxic tank, an external reflux is arranged between the secondary sedimentation tank and the biological adsorption hydrolysis-clarification redistribution tank, and the secondary sedimentation tank discharges the treated effluent and the residual sludge.

[0060] The parts of the present invention that are not described in detail are prior art. It is obvious to those skilled in the art that the present invention is not limited to the details of the above-mentioned exemplary embodiments, and the present invention can be implemented in other specific forms without departing from the spirit or basic characteristics of the present invention; therefore, no matter from which point of view, the embodiments should be regarded as exemplary and non-restrictive. The scope of the present invention is limited by the appended claims rather than the above description. Therefore, it is intended to include all changes within the meaning and scope of the equivalent elements of the claims in the present invention, and any figure marks in the claims should not be regarded as limiting the claims involved.

Claims

1. A H C R -A 2 O Wastewater treatment method, based on A H C R -A 2 O sewage treatment system, characterized in that, The system includes an anaerobic tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank. The sewage to be treated enters the anaerobic tank. The anoxic tank, the aerobic tank and the secondary sedimentation tank are connected in sequence. An internal return is set between the aerobic tank and the anoxic tank, and an external return is set between the secondary sedimentation tank and the anaerobic tank. The secondary sedimentation tank discharges the treated effluent and residual sludge. It also includes a biological adsorption hydrolysis-clarification redistribution tank A H C R The biosorption hydrolysis-clarification redistribution tank comprises a tank body, a water inlet pipe, a supernatant outlet and a bottom mud outlet. The water inlet pipe, the supernatant outlet and the bottom mud outlet are respectively arranged on the tank body. The water inlet pipe is connected with the outlet of the anaerobic tank. The sewage treated in the anaerobic tank enters the biosorption hydrolysis-clarification redistribution tank. The supernatant outlet is arranged at the upper part of the tank body, and the bottom mud outlet is arranged at the lower part of the tank body. The supernatant outlet is respectively connected with the anoxic tank and the aerobic tank and selectively conducted. The bottom mud outlet is connected with the anoxic tank. The steps include: A. The sewage to be treated enters the anaerobic tank and mixes with the external return liquid from the secondary sedimentation tank to undergo anaerobic reaction; B. The treated sewage in the anaerobic tank enters the biosorption hydrolysis-clarification redistribution tank through the water inlet pipe, where it undergoes biosorption, hydrolysis and clarification. After treatment, the upper part of the tank body gathers to form a supernatant, and the bottom of the tank body gathers to form a bottom sludge; C. According to the direction of sewage treatment in the pool, the interior of the anoxic pool is divided into the anoxic pool front section and the anoxic pool rear section, and the interior of the aerobic pool is divided into the aerobic pool front section, the aerobic pool middle section and the aerobic pool rear section; when the turbidity of the supernatant liquid derived from the supernatant liquid outlet of the biological adsorption hydrolysis-clarification redistribution pool is not higher than the preset value, it flows into the front section of the aerobic pool, and the bottom mud derived from the biological adsorption hydrolysis-clarification redistribution pool and the internal reflux liquid derived from the aerobic pool are mixed in the anoxic pool and denitrified; When the turbidity of the supernatant is higher than the preset value, the supernatant flows into the rear section of the anoxic tank and the front section of the aerobic tank, and the sludge drawn from the biosorption hydrolysis-clarification redistribution tank, part of the supernatant and the internal reflux liquid drawn from the aerobic tank are mixed in the anoxic tank and subjected to denitrification treatment; the sludge discharge port is connected to the front section of the anoxic tank, and the rear section of the aerobic tank is connected to the front section of the anoxic tank to form an internal reflux; the preset value of the turbidity of the supernatant drawn from the biosorption hydrolysis-clarification redistribution tank in the above steps is 50NTU; D. The sewage and sludge treated in the anoxic tank enter the aerobic tank, are mixed with the supernatant drawn from the biological adsorption hydrolysis-clarification redistribution tank, and are nitrified. The aerobic tank and the anoxic tank form an internal reflux; E. The sewage and sludge treated in the aerobic tank enter the secondary sedimentation tank, and an external return flow is formed between the secondary sedimentation tank and the anaerobic tank. The secondary sedimentation tank discharges the treated water and residual sludge; The redox potential value ORP of the anaerobic tank is -250~-100mV, the ORP of the anoxic tank is -200~50mV, and the dissolved oxygen of the aerobic tank is 0.5-2.0mg / L; the ORP at the bottom of the biosorption hydrolysis-clarification redistribution tank is -350~-200mV; the sediment flow rate Q of the biosorption hydrolysis-clarification redistribution tank is 底泥 The sewage flow Q into the anaerobic tank 进 The ratio is 0.9 to 1.2, and the supernatant flow Q 上清 The sewage flow Q into the anaerobic tank 进 The ratio is 0.80 to 1.1, and the internal reflux flow rate Q from the aerobic pool to the anoxic pool 内 The sewage flow Q into the anaerobic tank 进 The ratio is 1.6 to 2, and the external return liquid flow rate Q from the secondary sedimentation tank to the anaerobic tank 外 The sewage flow Q into the anaerobic tank 进 The ratio is 0.8~1.

Images