CN210635844U - Sewage is from source reinforcing nitrogen and phosphorus removal system - Google Patents
Sewage is from source reinforcing nitrogen and phosphorus removal system Download PDFInfo
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- CN210635844U CN210635844U CN201920143532.9U CN201920143532U CN210635844U CN 210635844 U CN210635844 U CN 210635844U CN 201920143532 U CN201920143532 U CN 201920143532U CN 210635844 U CN210635844 U CN 210635844U
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Abstract
The utility model relates to a water treatment field especially relates to a sewage is from source enhanced nitrogen and phosphorus removal system, a high-efficient nitrogen and phosphorus removal technology of sewage (SSCS) and application, and in particular to is fit for the sewage plant that the influent C/N ratio is lower, utilizes self carbon source and microorganism to strengthen nitrogen and phosphorus removal, the technology mainly comprises processes such as anaerobism, oxygen deficiency, good oxygen, from source enhancement, sludge activation, and wherein, it has 3 to be provided with the raw water point of intaking: an anaerobic tank, an anoxic tank II and an autonomous reinforcement tank; and 3 sludge reflux points: the anoxic tank I flows back to the anaerobic tank, the aerobic tank II flows back to the anoxic tank II, and the secondary sedimentation tank flows back to the sludge activation (regeneration) tank. The process is favorable for improving the treatment effect and reducing the treatment cost.
Description
Technical Field
The utility model relates to a water treatment field especially relates to a sewage is from Source enhanced nitrogen and phosphorus removal system, a high-efficient nitrogen and phosphorus removal technology (SSCS) of sewage (Self Source Carbon Supplement) and application, and in particular to is fit for the sewage factory that the C/N ratio is lower of intaking and utilizes Self Carbon Source and microorganism to strengthen nitrogen and phosphorus removal, improves treatment effect, reduces treatment cost's method.
Background
With the promulgation and the comprehensive implementation of the action plan for preventing and treating water pollution (ten items of water for short), the requirement of China on the quality of the effluent water of municipal sewage treatment plants is continuously improved. In addition to meeting new requirements of newly-built sewage plants, some sewage plants with the original design standard of 'pollutant discharge standard of municipal sewage plant' (GB18918-2002) first-class B or even second-class pollutant discharge standard also need to improve the treatment effect on pollutants such as organic matters, ammonia nitrogen, total phosphorus and the like in sewage, and reach the first-class A or higher pollutant discharge standard through upgrading and modification. In order to meet the requirements, a sewage treatment facility needs to be redesigned and modified, the sewage treatment capacity is improved, the effluent meets the corresponding discharge standard requirements, and for most sewage treatment plants, especially sewage plants with lower inlet water C/N, the problem that the total nitrogen reaches the standard and is discharged by improving the denitrification effect is the most difficult to solve.
The anaerobic-anoxic-aerobic process (A) is reported in the literature2O), oxidation ditch process, cyclic activated sludge process (CASS) and anaerobic-aerobic process (A/O) which are adopted by municipal sewage treatment plants in China at presentThe main body process, wherein (A)2O) and the improved process thereof have low energy consumption and operation cost, can effectively and simultaneously remove nitrogen and phosphorus, and have the application accounting ratio in the industry of more than 50 percent. Conventional at present A2The removal rate of TN by the/O process and the improved process thereof is about 60 percent, the TN cannot meet the requirements of new pollutant discharge standards, and in order to reach the first-class A standard, different upgrading measures need to be adopted according to the conditions of sewage plants. The main methods currently addressed include: adding carbon source, adding MBR, membrane treatment and other structures for strengthening and upgrading. These upgrading and reconstruction measures have relatively high requirements for land use, capital investment and operating cost. The utility model provides a at A2On the basis of the/O or the improved process thereof, on the premise of ensuring the removal effect of organic matters, total phosphorus and the like, structures do not need to be added, and an external carbon source is also not needed, so that the denitrification effect is greatly improved.
The prior art mainly comprises: a. the2the/O process is a common process for nitrogen and phosphorus removal in sewage plants. Tradition A2an/O process, wherein the A1 zone (anaerobic tank) is positioned at the foremost end of the process, the A2 zone (anoxic tank) and the O zone (aerobic tank) are arranged after the A1/A2/O zone, and A1/A2/O arrangement2The specific form of the O process is shown in FIG. 1.
Two kinds are in A2Common processes improved on the basis of the/O process are UCT (University of Cape Town) and MUCT (modified University of Cape Town) processes respectively, and the specific forms of the UCT process and the MUCT process are shown in fig. 2 and 3.
Referring to FIGS. 1, 2 and 3, it can be seen that the structure and layout of the UCT process is shown as A2The anaerobic pool is an anoxic pool, so that nitrate is prevented from entering the anaerobic pool to influence the release of phosphorus, and the reflux of the anoxic zone to the anaerobic zone is increased to supplement the sludge loss of the anaerobic zone; the MUCT divides the anoxic pond into two areas on the basis of UCT so as to solve the contradiction between low nitrate nitrogen and high reflux ratio of the reflux sludge, and the reflux mode is basically unchanged.
A2O andthe improved process has the advantages of simple main process, small occupied area, easy control of the whole process, sufficient organic matters in the sewage and proper C/N ratio, can obtain better denitrification and dephosphorization effects, and can basically meet the requirements of the pollutant discharge standard level B. However, in the reactor of the process, phosphorus accumulating bacteria, denitrifying heterotrophic bacteria and nitrifying bacteria are symbiotic in a system and are advanced forward along the treatment flow, various biochemical reactions are complicated, the competition contradiction between phosphorus removal and nitrogen removal in the system is prominent, the nitrogen and phosphorus removal effect is unstable, and particularly when the water quality and water quantity change suddenly from the outside such as rainstorm and the like, the impact resistance is insufficient, and the recovery time is too long.
Under the background of comprehensively implementing ten items of water, the discharge standard of a sewage plant is generally improved to the first grade A, wherein the key limiting index is the removal rate of total nitrogen. The discharge standard of the first grade A total nitrogen is reduced to 15mg/L from 20mg/L of the first grade B, the total nitrogen removal rate is required to reach more than 70 percent according to the total nitrogen content of about 50mg/L of inlet water of a common sewage plant, and the existing A total nitrogen removal rate is higher than 70 percent2The total nitrogen removal rate of O and the improved process thereof is 50-65%, and the total nitrogen removal rate is lower when the C/N ratio of raw water is lower, so that the requirement of the current pollutant discharge standard cannot be met.
Disclosure of Invention
The utility model provides a sewage is from source enhanced nitrogen and phosphorus removal system, a sewage is from source enhanced nitrogen and phosphorus removal's method, adopts the sewage factory biochemical treatment system that this method designed, under the condition of not additionally adding the carbon source, to BOD5The removal rate of the catalyst can reach more than 95 percent, and CODCrThe removal rate of the ammonia nitrogen can reach more than 90 percent, the removal rate of TP can reach more than 90 percent, the removal rate of ammonia nitrogen can reach more than 95 percent, meanwhile, the removal rate of TN can reach more than 85 percent at most, the annual average removal rate can reach more than 75 percent, and all chemical indexes of effluent of sewage plants can meet the requirements of first-class A of pollutant discharge standards of urban sewage treatment plants (GB 18918-2002).
The utility model firstly provides a sewage is from source reinforcing nitrogen and phosphorus removal system, include: the anaerobic tank, the anoxic tank I, the anoxic tank II, the aerobic tank I, the self-source strengthening tank, the aerobic tank II and the secondary sedimentation tank are sequentially connected; and a sludge activation (regeneration) tank;
wherein, it has 3 to set up raw water inflow point: an anaerobic tank, an anoxic tank II and an autonomous reinforcement tank;
and 3 sludge reflux points: the anoxic tank I flows back to the anaerobic tank, the aerobic tank II flows back to the anoxic tank II, the secondary sedimentation tank flows back to the sludge activation (regeneration) tank, and the sludge activation (regeneration) tank is connected with the anoxic tank I.
As an optimized technical proposal of the utility model, a flow impeller and/or an aerator are simultaneously arranged in the self-source strengthening tank, and the concentration of dissolved oxygen DO is controlled according to different process requirements. In addition, the bottoms of the sludge activation (regeneration) tank and the rest aerobic tanks are provided with lath type microporous aerators and are provided with linear flow regulating valves for accurately controlling aeration.
The utility model further provides a sewage is from source enhanced nitrogen and phosphorus removal technology adopts aforementioned system, include:
(1) the process flow mainly comprises the processes of anaerobic treatment, anoxic treatment, aerobic treatment, self-source strengthening, sludge activation and the like, wherein the flow direction of water in the process is as follows: water inlet → anaerobic tank → anoxic tank I → anoxic tank II → aerobic tank I → autonomous reinforcement tank → aerobic tank II → secondary sedimentation tank;
(2) the raw water inlet points are 3: an anaerobic tank, an anoxic tank II and an autonomous reinforcement tank;
(3) the number of sludge backflow points is 3: the anoxic tank I flows back to the anaerobic tank, the aerobic tank II flows back to the anoxic tank II, and the secondary sedimentation tank flows back to the sludge activation (regeneration) tank and then enters the anoxic tank I.
As an optimal technical scheme of the utility model, for under the condition that does not increase the pond volume, increase nitrobacteria's reserves for biological system can maintain an efficient nitrification, set up mud activation (regeneration) pond, carry out the controlled aeration to two heavy pond backward flow bed mud, and the design dwell time in mud activation (regeneration) pond is 3% -10% of total dwell time, and the design dissolved oxygen control is at 0.2-1 mg/L. The sludge activation (regeneration) pool can simultaneously keep or improve the activity of other flora in the system, so that the whole system is in a healthy state.
As an optimal technical scheme of the utility model, install impeller and aeration dish simultaneously in the pond of strengthening from the source to carry out aeration control air supply volume through the solitary air conduit who is equipped with linear flow regulating valve, be equipped with solitary raw water inlet channel. When the C/N ratio of inlet water is lower, opening a raw water inlet valve, adjusting the inlet water to account for 5% -50% of the total inlet water, and utilizing a carbon source in the raw water to make up a denitrification carbon source; when C/N is higher, a raw water inlet pipeline is closed, and the raw water can be continuously used as an anoxic pond for denitrification by reducing or closing aeration, and dissolved oxygen DO is controlled to be about 0.5-1 mg/L; or by controlling the ORP, wherein the ORP is controlled between-200 and 200 mV.
As an optimized technical proposal of the utility model, the sludge reflux ratio range of the sludge activation (regeneration) pool reflowed to the secondary sedimentation pool is controlled to be 50-100 percent, the secondary reflux ratio range of the anaerobic pool reflowed to the anoxic pool I is 50-200 percent, the secondary reflux ratio range is determined according to the primary reflux and the anaerobic retention time, the internal reflux ratio range of the aerobic pool I reflowing to the anoxic pool II is 100-300 percent, and the secondary reflux ratio range is compared with the A 20 and the derivative process thereof, a reflux pump is not required to be added; the utility model designs a sludge concentration is determined according to the water quality concentration of inlet water and the sludge concentration, the higher the sludge concentration is, the higher the inlet water concentration is, the larger the adjusted gas-water ratio is, the sludge concentration needs to be more than or equal to 3000mg/L, the aerobic aeration tank controls the gas-water ratio to reach at least 3: 1; the sludge concentration is preferably designed to be 3000-10000mg/L, preferably 5000mg/L in actual operation; the aerobic aeration tank is preferably designed to control the gas-water ratio to be between 3:1 and 8: 1.
The utility model aerates the aerobic tank I and the aerobic tank II, carries out controlled aeration in the sludge activation (regeneration) tank, controls the dissolved oxygen at 0.2-1mg/L, and has the retention time accounting for 3% -10% of the total retention time.
The utility model discloses aforementioned scheme is preferably obtained through a large amount of research experiments, has following characteristics:
(1) the original one-grid anaerobic tank of the MUCT is transformed into a sludge activation (regeneration) tank, sludge in a secondary sedimentation tank flows back to the sludge activation (regeneration) tank, the sludge age is prolonged, the quantity of nitrobacteria and other microorganisms is increased on the premise of not increasing the concentration of mixed liquid entering the secondary sedimentation tank, the system is in a stable active state, and reliable nitrification is realized.
(2) A self-source strengthening tank is arranged at the middle section of the aerobic tank, a submersible water impeller and a batten type microporous aerator are simultaneously arranged in the tank, DO is controlled to be about 0.5mg/L, and the problem that denitrification efficiency is influenced due to insufficient carbon source is solved by supplementing raw water.
(3) The process comprises the step of passing sewage A2On the basis of the/O improvement process, according to the process mode of sludge activation-anaerobic-anoxic-aerobic-self-source reinforcement-aerobic, the sludge is subjected to micro-activation by adding a sludge activation (regeneration) pool to increase the microbial number and prolong the sludge age so as to meet the purpose of longer reproduction generation of nitrobacteria; the denitrification bacteria can fully play the denitrification role by increasing the anoxic retention time and solving the problem of insufficient carbon source by adding the self-source strengthening tank, thereby achieving the purpose of strengthening the denitrification. In addition, the denitrification benefit brought by the self-source strengthening tank reduces the nitrate brought back by the secondary sedimentation tank, provides a good anaerobic environment for phosphorus accumulating bacteria, and promotes the release of phosphorus and the absorption of phosphorus at the later stage.
The utility model discloses beneficial effect for prior art includes:
(1) the process creates a new backflow thought by adding a sludge activation (regeneration) tank, concentrates the high-concentration sludge in the secondary sedimentation tank, directly controls the environment by aeration, and can increase the microbial magnitude without increasing the volume of the structure.
(2) The process utilizes the carbon source in the raw water, can reach the better water quality standard without additional carbon source, and is similar to the general A2Compared with the O and the derivative process, the operation cost is greatly reduced.
(3) The utility model can be used for all A2The O process and the derivative process transformation project thereof achieve the purpose of improving the water quality on the premise of not adding new structures.
Drawings
FIG. 1, Prior Art A2O process;
fig. 2, a prior art UCT process;
FIG. 3, a prior art MUCT process;
FIG. 4, SSCS process of the present invention;
FIG. 5 is a schematic view of a sludge activation (regeneration) tank of the present invention;
FIG. 6 is a schematic diagram of the self-source strengthening pool process of the present invention;
fig. 7, the utility model discloses TN gets rid of effect schematic diagram.
Detailed Description
The present invention will be described in further detail with reference to the following examples and drawings, but the embodiments of the present invention are not limited thereto.
Example 1
Control group 1 is the MUCT process (see FIG. 3) and group 2 is the SSCS process (see FIGS. 4, 5 and 6). The two groups of inlet water flow rates are about 3700m3The sludge reflux ratio is about 80 percent, the internal reflux ratio is about 250 percent, the secondary reflux ratio is 105 percent, the aeration rate and the water quality of the inlet water are controlled to be consistent, and the concentration of the two groups of biological tanks is about 8500 mg/L. After the operation is stable, two groups of data corresponding to each on-way point are respectively monitored:
the average concentration of the inlet TP of the two groups is 3.82mg/L, the average concentration of the anaerobic released TP of the group 1 is 6.34mg/L, and the average concentration of the anaerobic released TP of the group 2 is 8.75 mg/L; the final group 1 yielded an average TP concentration of 0.65mg/L, and group 2 0.40 mg/L.
The average concentration of TN of the inlet water of the two groups is 24.59mg/L, the removal rate of TN of the outlet water of the group 1 is 10.97mg/L and the removal rate of TN of the outlet water of the group 2 is 73.6% and is 55.4%.
Example 2
Referring to fig. 4, 5 and 6, adjusting the SSCS process of the group 1 and the group 2, wherein the water inlet source is the same, the sludge reflux ratio is controlled to be about 50%, the secondary reflux ratio is controlled to be about 100%, the internal reflux ratio is controlled to be about 200%, the sludge concentration is 6500mg/L, and the gas-water ratio is controlled to be 3: 1; the control variables are that the group 1 self-source strengthening pool does not increase raw water, and the group 2 self-source strengthening pool increases raw water. Detecting the water quality of inlet water and outlet water after stable operation:
the average concentration of the TP of the inlet water of the two groups is 10.08mg/L, and the average concentration of the TP of the outlet water of the groups 1 and 2 is 0.2 mg/L;
the average concentration of TN of the inlet water of the two groups is 25.96mg/L, the average concentration of TN of the outlet water of the group 1 is 6.58mg/L, the removal rate is 74.65%, the average concentration of TN of the outlet water of the group 2 is about 3.45mg/L, and the removal rate is 86.7%.
Example 3
Referring to fig. 4, 5 and 6, the group 1 and the group 2 both run in an SSCS process mode, the water inlet source is the same, the sludge reflux ratio is controlled to be about 50%, the secondary reflux ratio is controlled to be about 100%, the internal reflux ratio is controlled to be about 200%, the sludge concentration is 6500mg/L, and raw water with the same proportion is added into the self-source strengthening tanks of the group 1 and the group 2; control group 1 gas-water ratio is 3:1, the gas-water ratio of the group 2 is 5: 1. Detecting the water quality of inlet water and outlet water after stable operation:
the concentration of TP in the inlet water of the biochemical pool is about 10.86mg/L, and the average concentration of TP in the outlet water of the group 1 and the group 2 is 0.2 mg/L; the average TN concentration of the inlet water is about 26.30mg/L, the average TN concentration of the outlet water of the group 1 is 7.53mg/L, the removal rate is 71.4%, the average TN concentration of the outlet water of the group 2 is about 4.18mg/L, and the removal rate is 84.1%.
Example 4 technical effects example
The SSCS technology of example 2 is adopted, and the SSCS technology is shipped and used for a certain sewage treatment plant in 2018 and 4 months, wherein the average concentration of influent COD of the sewage treatment plant is 212mg/L (the minimum concentration is 326mg/L and the maximum concentration is 1615mg/L), the average concentration of influent TN is 28mg/L (the minimum concentration is 26.53mg/L and the maximum concentration is 78.74mg/L), and the concentration of influent TP is 15mg/L (the minimum concentration is 4.2mg/L and the maximum concentration is 32.14 mg/L); the average value of the C/N of the inlet water is 7.8, (the lowest value is 3.26, and the highest value is 25.88). Controlling the DO concentration of the sludge activation (regeneration) pool to be about 0.5mg/L, controlling the DO concentration of the self-source activation pool to be about 0.5mg/L, and adjusting the water inflow of the self-source strengthening pool, wherein the gas-water ratio is more than 3: 1. Under normal conditions, the effluent quality reaches TP0.2mg/L, TN6 mg/L. As shown in fig. 7: during 214 days of operation, the TN effluent concentration was <8mg/L, the days of TN removal rate of greater than 70% accounted for 95% of the total days, and the days of TN removal rate of greater than 74% accounted for 90% of the total days.
From the above implementation effects, it can be derived:
1. the process of the utility model is suitable for all applications A2O and the derivative thereof improve the process, and further enhance the denitrification and dephosphorization effect and reduce the TN concentration of the effluent. The denitrification efficiency can reach more than 70 percent, and the TN of the effluent is stabilized below 10 mg/L.
2. The true bookThe novel process is based on the self-source strengthening pool, does not need to increase the cost of a carbon source, and is compared with A2The O and the derivative process thereof save the addition of external carbon sources, save land and reduce the running power consumption compared with biological membranes and other advanced treatment processes, and are relatively economic enhanced denitrification processes.
The above embodiments are preferred embodiments of the present invention, but the embodiments of the present invention are not limited to the above embodiments, and any other changes, modifications, substitutions, combinations, and simplifications which do not depart from the spirit and principle of the present invention should be equivalent replacement modes, and all are included in the scope of the present invention.
Claims (3)
1. The utility model provides a sewage is from source enhanced nitrogen and phosphorus removal system which characterized in that includes: the system comprises an anaerobic tank, an anoxic tank I, an anoxic tank II, an aerobic tank I, an autonomous reinforcement tank, an aerobic tank II and a secondary sedimentation tank which are sequentially connected, and a sludge activation tank;
wherein, it has 3 to be provided with raw water inlet point: an anaerobic tank, an anoxic tank II and an autonomous reinforcement tank;
and 3 sludge reflux points: the anoxic tank I flows back to the anaerobic tank, the aerobic tank II flows back to the anoxic tank II, the secondary sedimentation tank flows back to the sludge activation tank, and the sludge activation tank is connected with the anoxic tank I.
2. The system of claim 1, wherein a flow impeller and an aerator are installed in the self-sourced enhanced tank.
3. The system of claim 1, wherein a flow impeller or an aerator is installed in the self-sourced enhanced tank.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109626754A (en) * | 2019-01-28 | 2019-04-16 | 深圳市水务(集团)有限公司南山水质净化厂 | A kind of wastewater efficient denitrification dephosphorization technique (SSCS) and application |
| CN112794444A (en) * | 2020-12-23 | 2021-05-14 | 联合环境技术(天津)有限公司 | A2Optimization method of reflux ratio of O biological nitrogen and phosphorus removal |
| CN113173643A (en) * | 2021-04-22 | 2021-07-27 | 浙江工业大学 | Method for efficiently and stably degrading DBP in landfill leachate based on A/A/O system |
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2019
- 2019-01-28 CN CN201920143532.9U patent/CN210635844U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109626754A (en) * | 2019-01-28 | 2019-04-16 | 深圳市水务(集团)有限公司南山水质净化厂 | A kind of wastewater efficient denitrification dephosphorization technique (SSCS) and application |
| CN112794444A (en) * | 2020-12-23 | 2021-05-14 | 联合环境技术(天津)有限公司 | A2Optimization method of reflux ratio of O biological nitrogen and phosphorus removal |
| CN112794444B (en) * | 2020-12-23 | 2022-08-23 | 联合环境技术(天津)有限公司 | A 2 Optimization method of reflux ratio of O biological nitrogen and phosphorus removal |
| CN113173643A (en) * | 2021-04-22 | 2021-07-27 | 浙江工业大学 | Method for efficiently and stably degrading DBP in landfill leachate based on A/A/O system |
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