CN110342750A - Sewage treatment device and process for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal - Google Patents

Abstract

The invention relates to a sewage treatment device and process for synchronously realizing in-situ reduction of sludge and denitrification and phosphorus removal. Adsorption assembly, aeration tank and solid-liquid separation unit, the excess sludge outlet of the sludge settling tank is also connected to the aeration tank through the sludge return pipeline, and the excess sludge outlet of the solid-liquid separation unit is also connected to the aeration tank The sludge reduction tank is connected through the second sludge return pipeline. Compared with the prior art, the process of the present invention can realize significant sludge reduction under the premise that the effluent water quality meets the GB18918‑2002 Grade A standard or even the Class IV standard of surface water.

Description

Sewage treatment equipment and process for simultaneous realization of in-situ sludge reduction and nitrogen and phosphorus removal

technical field

The invention belongs to the technical field of sewage treatment, and relates to a sewage treatment device and process for synchronously realizing in-situ reduction of sludge and denitrification and phosphorus removal.

Background technique

As the most widely used sewage treatment technology at present, the activated sludge process has treated more than 90% of urban sewage and about 50% of industrial wastewater in the world. With the increase of sewage treatment rate and increasingly stringent environmental protection regulations, the treatment and disposal of excess sludge has become the main factor that plagues the further development of activated sludge process, and its investment and operation costs account for about 25-65% of the entire sewage treatment plant. Moreover, regardless of landfill or incineration, they all encounter difficulties in site selection and public support, and there are also secondary pollution problems. Therefore, how to solve the problem of sludge outlet has become a major environmental problem that needs to be solved urgently in the process of urban development in my country, and it is also a focus of attention of the world's environmental protection industry today. Compared with treatment and disposal technology, in-situ reduction of sludge in the process of sewage treatment is the best way to solve the problem of excess sludge. Among them, setting an anaerobic side-stream reactor in the sludge return pipeline has the advantages of low operating cost and little impact on microorganisms, and is one of the in-situ reduction processes most likely to be applied in sewage treatment plants. This process is to keep a part of the sludge in an anaerobic environment for a certain period of time after passing through the side flow reactor unit, so that it can achieve a lower sludge yield without affecting the sedimentation performance of the sludge and the quality of the effluent. Sludge reduction is mainly based on four reduction mechanisms: lytic recessive growth, energy uncoupling metabolism, microbial predation and sludge attenuation.

Among various sludge reduction processes, the OSA process with a side stream reactor (SSR) on the sludge return pipeline has the advantages of simple process, low operating cost and large treatment scale, and is considered to be the most likely to be applied in practice. craft. The process has been proven to achieve sludge reduction and improve sludge settling performance without affecting the effluent quality. However, the effective reduction of SSR requires a long reaction time, and the minimum hydraulic retention time (HRT) is 6-7h. For example, in the Levico sewage treatment plant in Italy where ASSR-AO is adopted throughout the plant, the ratio of HRT between SSR and mainstream biological treatment system is 0.47. Too long HRT will limit the promotion and application of ASSR. How to accelerate sludge reduction and reduce floor space through microbial physiological and ecological regulation is the key to improving its technical competitiveness.

Studies have shown that SSR insertion does not affect or even improves sludge settling performance. However, when the sludge production does not match the reduction rate, SSR will cause insufficient solid-liquid separation capacity of the secondary settling tank, and the problem of high suspended solids (SS) in the effluent will appear. For example, in the OSA pilot experiment conducted by Coma et al. (Bioresource Technology, 2013, 129:229-235), under the conditions of side flow ratio of 10%, 50% and 100%, the concentration of SS in the effluent was 105, 118 and 128mg respectively /L. In addition to the stable compliance of SS in the effluent, the sludge reduction process also needs to consider the deterioration of the phosphorus removal effect in the effluent caused by long sludge age operation. This problem generally exists in the OSA process with many research reports.

In order to solve the above problems, an intermediate sedimentation tank can be inserted behind the SSR tank, and the effluent from the SSR tank enters the sedimentation tank for solid-liquid separation, so as to effectively buffer the floating mud problem caused by sludge accumulation. In the process of sludge reduction in SSR ponds, the hydrolysis of particulate matter and microbial lysis will release ammonia nitrogen. For domestic sewage with low carbon-to-nitrogen ratio, insufficient carbon sources will easily lead to excessive nitrogen and phosphorus in the effluent. Therefore, the development of the coupling of the sludge reduction process and the denitrification unit in the dual-sludge system is of great significance for improving the efficiency of sludge reduction and maintaining the effluent quality to meet the standard.

Contents of the invention

The object of the present invention is to provide a sewage treatment device and process for simultaneously realizing in-situ reduction of sludge and denitrification and dephosphorization in order to overcome the above-mentioned defects in the prior art. Aiming at the problems that the suspended solids in the effluent of the sludge side flow in-situ reduction system are easy to exceed the standard, and the efficiency of nitrogen and phosphorus removal in low-carbon-to-nitrogen ratio sewage is not high, a new sludge reduction process technology is provided through the coupling of physicochemical and biochemical technologies. The process of the present invention can realize significant sludge reduction on the premise that the effluent quality meets the GB18918-2002 Grade A standard or even the Class IV standard of surface water.

The purpose of the present invention can be achieved through the following technical solutions:

One of the technical proposals of the present invention is to propose a sewage treatment device that simultaneously realizes in-situ reduction of sludge and denitrification and phosphorus removal, including sludge reduction tanks, sludge sedimentation tanks, mixing Coagulation sedimentation tank, ammonia nitrogen adsorption assembly, aeration tank and solid-liquid separation unit, the remaining sludge outlet of the sludge settling tank is also connected to the aeration tank through the sludge return pipeline, and the solid-liquid separation unit The excess sludge outlet is also connected to the sludge reduction tank through the second sludge return pipeline.

Further, the sludge reduction tank used can be switched to anaerobic, anoxic and micro-aerobic operating modes according to working conditions, and can be further switched to full-mixed anaerobic reactors, upflow anaerobic reactors according to different anaerobic modes of operation Sludge bed, sludge expanded bed and other modes, and recover methane produced by sludge. Among them, fully mixed anaerobic reactor, upflow anaerobic sludge bed and sludge expanded bed are all common structures in this field, as follows:

Fully mixed anaerobic reactor: the specific structure is a closed tank and a stirring device. Wastewater can be completely mixed with anaerobic sludge and anaerobically digested to produce methane. After the sewage to be treated enters the fully mixed anaerobic reactor, all the anaerobic sludge is quickly mixed by the stirring device, and anaerobic digestion reaction occurs under the action of anaerobic microorganisms in the sludge, so that the concentration of anaerobic sludge is always kept relatively low. Low state, and finally achieve sludge reduction.

Upflow anaerobic sludge bed: The upflow anaerobic sludge bed is mainly composed of a water distribution system at the bottom, an anaerobic reaction zone at the bottom, and a gas-liquid-solid three-phase separator at the top. Sewage to be treated enters the reactor and mixes with anaerobic sludge in the lower anaerobic zone, where reactions such as anaerobic digestion and sludge reduction occur, and methane and other gases produced are discharged from the triangular area at the bottom of the herringbone baffle of the three-phase separator . The mixed sludge undergoes natural sedimentation and the action of the three-phase separator, so that the effluent, residual gas and mud are discharged from the top for the next step of biological treatment.

Sludge expanded bed: The sludge expanded bed has great similarities with the upflow anaerobic sludge bed in terms of structure and sludge morphology. However, the sludge expanded bed increases the treatment water circulation system, increases the liquid flow rate in the reactor, and expands the sludge bed in the reactor, which can ensure full contact between the sewage to be treated and the anaerobic sludge.

Further, a phosphorus removal and dosing box is also provided on the connecting pipeline between the sludge sedimentation tank and the coagulation sedimentation tank. Furthermore, the phosphorus removal agent in the phosphorus removal chemical box can choose to add calcium, aluminum or iron compounds such as lime, alum, ferric chloride, etc.

Further, the ammonia nitrogen adsorption assembly includes at least one set of ammonia nitrogen adsorption columns, and the water inlet and outlet of the ammonia nitrogen adsorption columns are respectively connected to the coagulation sedimentation tank and the aeration tank.

Furthermore, the ammonia nitrogen adsorption column includes a water inlet, a water outlet and an ammonia nitrogen adsorption material filled between them. The ammonia nitrogen adsorption materials that can be used include molecular sieves, activated carbon, ceramsite, zeolite, ion exchange resin, etc.

It is preferable to set up two or more sets of ammonia nitrogen adsorption columns, so that a single set of ammonia nitrogen adsorption columns will enter the regeneration stage after adsorption and breakthrough, and the water inlet will be switched to another set to continue operation.

Furthermore, a regeneration liquid tank connected to the water inlet of the ammonia nitrogen adsorption column through a regeneration pipeline is also provided, and a regeneration waste liquid discharge pipeline is also provided at the water outlet of the ammonia nitrogen adsorption column.

Further, the solid-liquid separation unit is a secondary settling tank, the supernatant liquid of the secondary settling tank is discharged through the outlet pipeline, and the remaining sludge at the bottom is respectively returned to connect the sewage through the sludge return pipeline 2 Mud reduction tank and aeration tank.

Further, the solid-liquid separation unit is a membrane separation module placed in the aeration tank, and a sludge outlet is processed at the bottom of the aeration tank as the excess sludge outlet of the solid-liquid separation unit, and the sludge The second return pipeline is respectively connected to the sludge outlet and the sludge reduction tank. The membrane separation module can adopt membrane separation equipment commonly used in the field that can realize sewage filtration.

The sewage to be treated enters the sludge reduction tank, and is evenly mixed with the returned residual sludge to maintain an anaerobic environment for a certain period of time. Based on the four reduction mechanisms of lytic recessive growth, energy uncoupling metabolism, microbial predation and sludge attenuation, the sludge is reduced in the sludge reduction tank. Simultaneously, denitrification and anaerobic phosphorus release reactions occur. The sewage treated by the sludge reduction tank enters the sludge sedimentation tank for mud-water separation. Part of the sludge is returned to the aerobic tank to supplement the sludge concentration in the system, and the other part of the sludge is discharged as surplus sludge. Due to reactions such as anaerobic phosphorus release in the sludge reduction tank, the separated sewage contains a relatively high concentration of total phosphorus. Sewage enters the coagulation sedimentation tank for coagulation and sedimentation treatment to remove most of the total phosphorus and suspended matter, so that the influent will not block the ammonia nitrogen adsorption component. The influent removes most of the ammonia nitrogen through ion adsorption in the ammonia nitrogen adsorption module. The low-phosphorus and low-ammonia-nitrogen effluent enters the aeration tank, which is beneficial to the joint action of aerobic microorganisms such as phosphorus-accumulating bacteria, polysaccharide bacteria, etc., to remove dissolved organic matter, and finally achieve the standard discharge of sewage treatment

The second technical solution of the present invention is to propose a sewage treatment process that simultaneously realizes in-situ reduction of sludge and denitrification and phosphorus removal, including the following steps:

(1) After the sewage to be treated is sent to the sludge reduction tank for treatment, the resulting treated sewage is discharged into the sludge sedimentation tank for a sedimentation, and the supernatant obtained is added to the phosphorus removal agent and then enters the coagulation sedimentation tank for sedimentation treatment. The remaining sludge is partly directly sent to the aeration tank in step (2);

(2) Phosphorus removal sewage obtained after coagulation and sedimentation in the coagulation sedimentation tank enters the ammonia nitrogen adsorption module, and after ammonia nitrogen adsorption treatment, it is then sent to the aeration tank for aeration treatment;

(3) The sewage treated by aeration in the aeration tank is then treated by the solid-liquid separation unit, and the resulting clear liquid is discharged as effluent, and the remaining sludge is returned to the aeration tank and the sludge reduction tank respectively.

Further, in step (1), the treatment process of the sewage to be treated in the sludge volume reduction tank is as follows: a stirring device is installed in the sludge volume reduction tank, and the sewage to be treated and the return sludge are evenly mixed, and the sludge concentration is at 4~10g SS/L, the oxygen concentration is about 0.2mg/L, and the hydraulic retention time is 4~10h. In the sludge reduction tank, after denitrification of returned sludge, anaerobic release of sludge and sludge reduction, etc., when the sewage enters the sedimentation tank, the concentration of pollutants such as ammonia nitrogen and total phosphorus may be higher than that of the sewage to be treated , while the concentration of pollutants such as chemical oxygen demand will be lower than that of the sewage to be treated.

Further, in step (1), the phosphorus removal agent is a compound of calcium, aluminum or iron, and its addition amount is 5-1500 mg/g SS, which is adjusted according to the actual situation. Too low dosage may lead to high effluent total phosphorus concentration, and too high dosage may lead to reduced sludge activity and inhibit nitrification rate to a certain extent;

In step (2), the time for ammonia nitrogen adsorption treatment is 0.2-4 hours, and it is adjusted according to the actual situation. If the adsorption time is too low, the total nitrogen in the effluent may be too high, and if it is too long, the cost will increase;

In step (3), the time for aeration treatment is 0.5-10 hours, and the aeration rate satisfies that the oxygen concentration in the water body of the aeration tank is 0.8-8 mg/L, and is adjusted according to the actual situation. Lower aeration rate may result in the concentration of effluent pollutants not reaching the standard.

Further, after the ammonia nitrogen adsorption component has been operated for a set period of time, regeneration is realized by soaking the regeneration solution through its water inlet. The salt in the regeneration solution can be selected from calcium salt, potassium salt, magnesium salt, zinc salt, iron salt, aluminum salt, and sodium salt, and its concentration is 4-90g/L, and it should be adjusted according to the actual situation. Lower concentrations may result in incomplete regeneration of the adsorption module, while higher concentrations may damage the adsorption material, reduce nitrogen removal efficiency, and increase costs.

Compared with the prior art, the present invention has the following advantages:

(1) The coupling of high-efficiency physicochemical denitrification and phosphorus removal technology with biological treatment technology greatly shortens the reaction time and reduces land occupation. Due to the setting of anoxic, anaerobic, and aerobic units in the traditional nitrogen and phosphorus removal process, a hydraulic retention time of up to 20 hours is required to achieve the first-level A standard. In the present invention, the chemical phosphorus removal and ammonia nitrogen adsorption rates can be quickly completed , The total hydraulic retention time of the reactor can be controlled below 8 hours, which greatly reduces the footprint of the process system.

(2) The combination of high-efficiency pollutant removal and sludge reduction technology can achieve a significant reduction in sludge production while the sewage is treated up to the standard, which is only 10-20% of the traditional process.

(3) The process design is flexible, which is conducive to the utilization of material resources. The sludge reduction tank can be switched to anaerobic mode operation, which can convert the organic matter in the sewage into methane for recycling while reducing the sludge volume; due to the solid-liquid pre-separation of the sludge reduction tank, the coagulation sedimentation tank can remove phosphorus The sediment with higher phosphorus content can be obtained, which is beneficial to the recovery and utilization of phosphorus resources.

Description of drawings

Figure 1 is a schematic diagram of a process for simultaneously realizing high-efficiency sludge in-situ reduction and nitrogen and phosphorus removal;

Figure 2 is a schematic diagram of another process flow for simultaneous realization of high-efficiency sludge in-situ reduction and nitrogen and phosphorus removal;

Instructions for marks in the figure:

1 is the water inlet pump; 2 is the sludge reduction tank; 3 is the sludge sedimentation tank; 4 is the coagulation sedimentation tank; 5 is the ammonia nitrogen adsorption column; 6 is the aeration tank; 7 is the secondary sedimentation tank; 8 is the outlet pump; 9 is the second sludge return pump; 10 is the first sludge discharge pump; 11 is the second sludge discharge pump; 12 is the water inlet pump of the first ammonia nitrogen adsorption column; 13 is the water inlet pump of the second ammonia nitrogen adsorption column; 14 is the first ammonia nitrogen adsorption column 15 is the outlet pump of the second ammonia nitrogen adsorption column; 16 is the regeneration liquid pump; 17 is the regeneration waste liquid discharge pump; 18 is the first sludge return pump; 19 is the phosphorus removal and dosing pump; 20 is the third Sludge return pump; 21 is a membrane separation module.

Detailed ways

The present invention will be described in detail below in conjunction with the accompanying drawings and specific embodiments. This embodiment is carried out on the premise of the technical solution of the present invention, and detailed implementation and specific operation process are given, but the protection scope of the present invention is not limited to the following embodiments.

One of the technical solutions of the present invention is to propose a sewage treatment device that simultaneously realizes in-situ sludge reduction and denitrification and phosphorus removal, including a sludge reduction tank 2 and a sludge sedimentation tank 3 arranged in sequence along the sewage treatment direction , coagulation sedimentation tank 4, ammonia nitrogen adsorption assembly, aeration tank 6 and solid-liquid separation unit, the remaining sludge outlet of described sludge sedimentation tank 3 also passes through sludge return pipeline one (the first sludge can be set above it) The return pump 18) is connected to the aeration tank 6, and the excess sludge outlet of the solid-liquid separation unit is also connected to the sludge reduction tank 2 through the sludge return pipeline 2.

In a specific embodiment of the present invention, the sludge volume reduction tank 2 used can be selected as anaerobic, anoxic and micro-aerobic operating modes according to different actual working conditions, and can be further selected when operating in anaerobic mode. Anaerobic reactor, upflow anaerobic sludge bed, sludge expanded bed and other operating modes, and recover methane produced by sludge. Among them, the fully mixed anaerobic reactor: the specific structure is a closed tank and a stirring device. Wastewater can be completely mixed with anaerobic sludge and anaerobically digested to produce methane. After the sewage to be treated enters the reactor, all anaerobic sludge is quickly mixed by the stirring device, and anaerobic digestion reaction occurs under the action of anaerobic microorganisms in the sludge, so that the concentration of anaerobic sludge is always kept relatively low, and finally Achieve sludge reduction.

Upflow anaerobic sludge bed: The upflow anaerobic sludge bed is mainly composed of a water distribution system at the bottom, an anaerobic reaction zone at the bottom, and a gas-liquid-solid three-phase separator at the top. Sewage to be treated enters the reactor and mixes with anaerobic sludge in the lower anaerobic zone, where reactions such as anaerobic digestion and sludge reduction occur, and methane and other gases produced are discharged from the triangular area at the bottom of the herringbone baffle of the three-phase separator . The mixed sludge undergoes natural sedimentation and the action of the three-phase separator, so that the effluent, residual gas and mud are discharged from the top for the next step of biological treatment.

Sludge expanded bed: The sludge expanded bed has great similarities with the upflow anaerobic sludge bed in terms of structure and sludge morphology. However, the sludge expanded bed increases the treatment water circulation system, increases the liquid flow rate in the reactor, and expands the sludge bed in the reactor, which can ensure full contact between the sewage to be treated and the anaerobic sludge.

In a specific embodiment of the present invention, a phosphorus removal dosing box is also provided on the connecting pipeline between the sludge sedimentation tank 3 and the coagulation sedimentation tank 4 . Furthermore, the phosphorus removal agent in the phosphorus removal chemical box can choose to add calcium, aluminum or iron compounds such as lime, alum, ferric chloride, etc. The dephosphorization dosing box can be connected in this connection pipeline through the pipeline with the dephosphorization dosing pump 19.

In a specific embodiment of the present invention, the ammonia nitrogen adsorption assembly includes at least one group of ammonia nitrogen adsorption columns 5, the water inlet of the ammonia nitrogen adsorption column 5 (the ammonia nitrogen adsorption column 5 water inlet pump can be set) and the water outlet (the ammonia nitrogen adsorption column 5 water inlet pump can be set) and the water outlet (can be set Ammonia nitrogen adsorption column 5 (outlet pump) is respectively connected with the coagulation sedimentation tank 4 and the aeration tank 6.

Furthermore, the ammonia nitrogen adsorption column 5 includes a water inlet, a water outlet and an ammonia nitrogen adsorption material filled between them. Available ammonia nitrogen adsorption materials include molecular sieve, activated carbon, ceramsite, zeolite, ion exchange resin and the like.

Two or more sets of ammonia nitrogen adsorption columns 5 are preferably installed, so that a single set of ammonia nitrogen adsorption columns 5 will enter the regeneration stage after adsorption and breakthrough, and the water inflow will be switched to another set to continue operation.

Furthermore, at the water inlet of the ammonia-nitrogen adsorption column 5, there is also a regeneration liquid tank connected to it through a regeneration pipeline, and at the water outlet of the ammonia-nitrogen adsorption column 5, a regeneration waste liquid discharge pipeline is additionally provided, and the regeneration waste liquid A regeneration waste liquid discharge pump may be arranged on the discharge pipeline.

In a specific embodiment of the present invention, the solid-liquid separation unit is a secondary settling tank 7, the supernatant of the secondary settling tank 7 is discharged through an outlet pipeline, and the remaining sludge at the bottom is passed through the sludge The second return pipeline returns to connect the sludge reduction tank 2 and the aeration tank 6 respectively. More specifically, the sludge return pipeline has two branches, and one of them returns to the aeration tank 6 through the third sludge return pump 20 . The other fork returns to the sludge reduction tank 2 through the second sludge return pump 9 .

In a specific embodiment of the present invention, the solid-liquid separation unit is a membrane separation module 21 placed in the aeration tank 6, and a sludge outlet is processed at the bottom of the aeration tank 6 as the solid-liquid separation unit. The excess sludge is exported, and the sludge return pipeline 2 is arranged to connect the sludge outlet and the sludge volume reduction tank 2 respectively. Membrane separation module 21 can adopt membrane separation equipment commonly used in the field that can realize sewage filtration.

The sewage to be treated enters the sludge reduction tank, and is evenly mixed with the returned residual sludge to maintain an anaerobic environment for a certain period of time. Based on the four reduction mechanisms of lytic recessive growth, energy uncoupling metabolism, microbial predation and sludge attenuation, the sludge is reduced in the sludge reduction tank. Simultaneously, denitrification and anaerobic phosphorus release reactions occur. The sewage treated by the sludge reduction tank enters the sludge sedimentation tank for mud-water separation. Part of the sludge is returned to the aerobic tank to supplement the sludge concentration in the system, and the other part of the sludge is discharged as surplus sludge. Due to reactions such as anaerobic phosphorus release in the sludge reduction tank, the separated sewage contains a relatively high concentration of total phosphorus. Sewage enters the coagulation sedimentation tank for coagulation and sedimentation treatment to remove most of the total phosphorus and suspended matter, so that the influent will not block the ammonia nitrogen adsorption component. The influent removes most of the ammonia nitrogen through ion adsorption in the ammonia nitrogen adsorption module. The low-phosphorus and low-ammonia-nitrogen effluent enters the aeration tank, and through the joint action of aerobic microorganisms such as phosphorus-accumulating bacterioglycan bacteria, dissolved organic matter is removed, and the discharge of sewage treatment is finally achieved.

The second technical solution of the present invention is to propose a sewage treatment process that simultaneously realizes in-situ reduction of sludge and denitrification and phosphorus removal, including the following steps:

(1) After the sewage to be treated is sent to the sludge reduction tank 2 for treatment, the treated sewage is discharged into the sludge sedimentation tank 3 for a sedimentation, and the obtained supernatant is added to the phosphorus removal agent and then enters the coagulation sedimentation tank 4 Sedimentation treatment, the surplus sludge of gained then partly directly sends in the aeration tank 6 in the step (2);

(2) Phosphorus removal sewage obtained after coagulation and sedimentation in the coagulation sedimentation tank 4 enters the ammonia nitrogen adsorption module, and after ammonia nitrogen adsorption treatment, it is then sent to the aeration tank 6 for aeration treatment;

(3) The sewage after aeration treatment in the aeration tank 6 is then treated by the solid-liquid separation unit, and the resulting clear liquid is discharged as effluent, and the remaining sludge is returned to the aeration tank 6 and the sludge reduction tank 2 respectively.

In a specific embodiment of the present invention, in step (1), the treatment process of the sewage to be treated in the sludge reduction tank 2 is specifically: an agitator is set in the sludge reduction tank, and the sewage to be treated and the backflow The sludge is mixed evenly, the sludge concentration is 4-10g SS/L, the oxygen concentration is about 0.2mg/L, and the hydraulic retention time is 4-10h. In the sludge reduction tank, after denitrification of returned sludge, anaerobic release of sludge and sludge reduction, etc., when the sewage enters the sedimentation tank, the concentration of pollutants such as ammonia nitrogen and total phosphorus may be higher than that of the sewage to be treated , while the concentration of pollutants such as chemical oxygen demand will be lower than that of the sewage to be treated.

In a specific embodiment of the present invention, in step (1), the phosphorus removal agent is a compound of calcium, aluminum or iron, and its addition amount is 5-1500 mg/g SS.

In a specific embodiment of the present invention, in step (2), the time of ammonia nitrogen adsorption treatment is (0.2～4h, and is adjusted according to the actual situation.

In a specific embodiment of the present invention, in step (3), the time of aeration treatment is 0.5-10h, and the aeration rate satisfies the oxygen concentration in the aeration tank 6 water body is 0.8-8mg/L, and according to the actual situation Make adjustments.

In a specific embodiment of the present invention, after the ammonia nitrogen adsorption component has been operated for a set period of time, it is soaked in a regeneration solution through its water inlet to achieve regeneration.

Each of the above implementation modes can be implemented individually, or can be implemented in any combination of two or more.

The above implementation manner will be further described below in combination with specific examples.

Example 1:

As shown in Fig. 1, a kind of sewage treatment process of this embodiment simultaneously realizes high-efficiency sludge in-situ reduction and denitrification and dephosphorization, enters the sludge reduction tank 2 (anaerobic) mode,), after reacting with the second sludge return pump 9 to return 100% of the remaining sludge for 6.7 hours, after entering the sludge settling tank 3 to settle the sludge for 3 hours, the supernatant is added with ferric chloride by the phosphorus removal dosing pump 19 After phosphorus removal, enter the coagulation sedimentation tank 4 for sedimentation, and the sludge discharge period of the coagulation sedimentation tank 4 is 3 hours. Phosphorus removal sewage is pumped into the ammonia nitrogen adsorption column 4 through the first ammonia nitrogen adsorption column inlet pump 12 and the second ammonia nitrogen adsorption column inlet pump 13, and is adsorbed ammonia nitrogen for 15 minutes, and passes through the first ammonia nitrogen adsorption column outlet pump 14 from the ammonia nitrogen adsorption column 4 And the second ammonia nitrogen adsorption column outlet pump 15 after water outlet, enter aeration tank 6 biological treatment 6h, aeration tank 6 receives first sludge return pump 18 from the 100% sludge of sludge settling tank 3, and add in advance The activated sludge is subjected to biological treatment, enters the secondary settling tank 7 and settles for 1 hour, and the effluent is discharged through the effluent pump 8 .

The sludge undergoes anaerobic reaction and sludge reduction in the sludge reduction tank 2, and most of the ammonia nitrogen sewage is removed by the ammonia nitrogen adsorption column 5, and the remaining low ammonia nitrogen wastewater enters the aeration tank 6 to undergo nitrification and other organic matter removal, 100% The sludge in the influent flow returns to the sludge reduction tank 1. After the ammonia nitrogen adsorption column 5 runs for 24 hours and is saturated, the regeneration liquid is pumped into the regeneration liquid tank through the regeneration liquid pump 16 for regeneration for 4 hours, and the regeneration waste liquid discharge pump 17 pumps out the regeneration waste liquid. After a certain number of regenerations, the regeneration solution can be decalcified, and the treated regeneration solution can be reused.

Run continuously for 100 days according to the above process. The average concentrations of dissolved COD, ammonia nitrogen, total nitrogen and total phosphorus in the influent water were 280.5, 60.2, 75.1 and 15.4 mg/L. After being treated by the above process proposed by the present invention, the pH of the reactor is 6.5-7.5, and the average concentrations of COD, ammonia nitrogen, total nitrogen and total phosphorus in the effluent are 15.2, 0.5, 3.4 and 0.3 mg/L respectively. Sludge production decreased by 75% compared with the same period last year.

The ammonia nitrogen adsorption column in this embodiment uses a zeolite column.

Example 2

The high-ammonia-nitrogen waste water of a sewage plant that intercepts coarse floating and suspended solids through the grid enters the sludge reduction tank 2 with a HRT of 6 hours through the inlet pump 1, and fully mixes and contacts with the return sludge. Then enter the sludge sedimentation tank 3 with HRT of 2h for mud-water separation. After separating the supernatant and removing phosphorus, it enters the ammonia nitrogen adsorption column 4 with a HRT of 0.5h to remove most of the ammonia nitrogen. When a single ammonia nitrogen adsorption column 4 runs continuously for 12 hours and penetrates, it enters the regeneration stage, and the water inflow is switched to another adsorption column to continue run. When the ammonia nitrogen adsorption column 4 is regenerated, the regeneration liquid pump 16 pumps the regeneration liquid into the ammonia nitrogen adsorption column to desorb and regenerate the adsorption material, and convert the desorbed ammonia nitrogen into nitrogen gas. The concentration of the composite regeneration solution is 40g/L, and the regeneration soaking time is 4h. Then enter the aeration tank 5 with HRT of 6.5h. At this time, the ammonia nitrogen in the influent is low, and the nitrate nitrogen is denitrified in the sludge reduction tank 2 using the carbon source in the influent. Since most of the ammonia nitrogen is adsorbed in the ammonia nitrogen adsorption column 4, the carbon source in the system can be fully utilized by the phosphorus accumulating bacteria, so that the total phosphorus in the effluent reaches the standard. Finally, the effluent is discharged through the membrane module.

After 6 months of continuous operation of this model, the average concentrations of dissolved COD, ammonia nitrogen, total nitrogen and total phosphorus in the influent water are 180.5, 100.2, 150.3 and 10.0 mg/L. After being treated by the above process proposed by the present invention, the pH of the reactor is 6.5-7.5, and the average concentrations of COD, ammonia nitrogen, total nitrogen and total phosphorus in the effluent are 10.1, 5.0, 7.0 and 0.8 mg/L respectively. Sludge production decreased by 70% compared with the same period last year.

Comparative example 1

Compared with Example 1, most of them are the same, except that the ammonia nitrogen adsorption component is removed in this example. At this time, after the ammonia nitrogen adsorption assembly in Figure 1 is removed, the water enters the sludge volume reduction tank 2 (anaerobic mode) through the grid inlet pump 1, and returns 100% of the inlet water flow rate with the second sludge return pump 9 After reacting for 6.7 hours, the remaining sludge enters the sludge sedimentation tank 3 and settles the sludge for 3 hours. The supernatant enters the coagulation sedimentation tank 4 for precipitation after being dephosphorized by the dephosphorization dosing pump 19 and ferric chloride. The sludge discharge cycle of pool 4 is 3 hours. Phosphorus removal sewage enters the aeration tank 6 for biological treatment for 6 hours, and the aeration tank 6 receives 100% sludge from the sludge settling tank 3 from the first sludge return pump 18, performs biological treatment with the activated sludge added in advance, and enters the second The settling tank 7 settles for 1 hour, and the effluent is discharged through the effluent pump 8.

The sludge undergoes anaerobic reaction and sludge reduction in the sludge reduction tank 2. In the sludge reduction tank, sludge reduction such as sludge lysis will release a large amount of ammonia nitrogen and dissolved organic matter, and then the sewage enters the aeration Nitrification reaction and other organic matters are removed in the pool 6, and the sludge with 100% inflow flow is returned to the sludge reduction pool 1. Since a large amount of nitrate will be produced during the nitrification process, the utilization of carbon by microorganisms in the denitrification process is prior to biological phosphorus removal, resulting in the failure of total phosphorus in the effluent to meet the standard treatment.

Run continuously for 100 days according to the above process. The average concentrations of dissolved COD, ammonia nitrogen, total nitrogen and total phosphorus in the influent water were 260.4, 40.5, 60.3 and 20.1 mg/L. After the above-mentioned process treatment, the pH of the reactor is 6.5-7.5, and the average concentrations of COD, ammonia nitrogen, total nitrogen and total phosphorus in the effluent are 19.6, 8.5, 14.6 and 0.7 mg/L respectively. Sludge production decreased by 25% compared with the same period last year.

The above descriptions of the embodiments are for those of ordinary skill in the art to understand and use the invention. It is obvious that those skilled in the art can easily make various modifications to these embodiments, and apply the general principles described here to other embodiments without creative effort. Therefore, the present invention is not limited to the above-mentioned embodiments. Improvements and modifications made by those skilled in the art according to the disclosure of the present invention without departing from the scope of the present invention should fall within the protection scope of the present invention.

Claims (10)

1. a kind of synchronous sewage-treatment plant for realizing sludge in-situ decrement and denitrogenation dephosphorizing, which is characterized in that including along sewage Mud decrement pond, mudpan, coagulative precipitation tank, ammonia nitrogen absorption component, aeration tank and the solid-liquid that processing direction is sequentially arranged The excess sludge outlet of separative unit, the mudpan also connects the aeration tank by sludge reflux pipeline one, described The excess sludge outlet of solid-liquid separation unit also connects the mud decrement pond by sludge reflux pipeline two.

2. a kind of synchronous sewage-treatment plant for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 1, It is characterized in that, is additionally provided with dephosphorization dosing tank on the connecting line between mudpan and coagulative precipitation tank.

3. a kind of synchronous sewage-treatment plant for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 1, It is characterized in that, the ammonia nitrogen absorption component includes at least one set of ammonia nitrogen absorption column, the water inlet of the ammonia nitrogen absorption column and water outlet Mouth is separately connected the coagulative precipitation tank and aeration tank.

4. a kind of synchronous sewage-treatment plant for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 3, It is characterized in that, the regeneration liquid case connecting with it by regeneration pipeline is additionally provided in the water inlet of ammonia nitrogen absorption column, inhaled in ammonia nitrogen The water outlet of attached column also separately sets a regeneration liquid waste discharge line.

5. a kind of synchronous sewage-treatment plant for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 1, It is characterized in that, the solid-liquid separation unit is secondary settling tank, and the supernatant liquor of the secondary settling tank is discharged by outlet pipeline, bottom Excess sludge then passes through the sludge reflux pipeline two and returns to the connection mud decrement pond and aeration tank respectively.

6. a kind of synchronous sewage-treatment plant for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 1, It is characterized in that, the solid-liquid separation unit is the membrane separation assemblies being placed in aeration tank, is machined with sludge in aeration bottom of pond portion and goes out Mouth is exported as the excess sludge of the solid-liquid separation unit, and the sludge reflux pipeline two is arranged and is separately connected the sludge Outlet and mud decrement pond.

7. a kind of synchronous sewage treatment process for realizing sludge in-situ decrement and denitrogenation dephosphorizing, which is characterized in that including following step It is rapid:

(1) treatment sewage is admitted in mud decrement pond after processing, and sewage, which is discharged into mudpan, after gained processing carries out Primary sedimentation, gained supernatant liquor enter coagulative precipitation tank precipitation process, gained excess sludge then part after Dephosphorization reagent is added It is sent directly into the aeration tank in step (2)；

(2) dephosphorization sewage resulting after coagulating sedimentation enters back into ammonia nitrogen absorption component in coagulative precipitation tank, through ammonia nitrogen absorption After processing, it is then sent into Air Exposure in aeration tank；

(3) sewage in aeration tank after Air Exposure is handled through solid-liquid separation unit again, and gained clear liquid is as water outlet discharge, institute It obtains excess sludge and is then back to aeration tank and mud decrement pond respectively.

8. a kind of synchronous sewage treatment process for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 7, It is characterized in that, in step (1), treatment process of the treatment sewage in mud decrement pond specifically: set in mud decrement pond Mixing plant is set, treatment sewage is uniformly mixed with the excess sludge of reflux, and guarantees the concentration of sludge in 4~10g SS/ L, hydraulic detention time 4-10h.

9. a kind of synchronous sewage treatment process for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 7, It is characterized in that, in step (1), the Dephosphorization reagent is the compound of calcium, aluminium or iron, and additive amount is 5~1500mg/g SS；

In step (2), the time of ammonia nitrogen absorption processing is 0.2~4h；

In step (3), time of Air Exposure is 0.5~10h, aeration quantity meet oxygen concentration in the water body of aeration tank be 0.8~ 8mg/L。

10. a kind of synchronous sewage treatment process for realizing sludge in-situ decrement and denitrogenation dephosphorizing according to claim 7, It is characterized in that, after ammonia nitrogen absorption assembly operating setting time, after being passed through regenerated liquid immersion treatment from its water inlet, realizes regeneration.