CN212222747U - Medium-high concentration organic wastewater split-phase treatment system for synchronous nitrogen and phosphorus removal - Google Patents
Medium-high concentration organic wastewater split-phase treatment system for synchronous nitrogen and phosphorus removal Download PDFInfo
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- CN212222747U CN212222747U CN202020667479.5U CN202020667479U CN212222747U CN 212222747 U CN212222747 U CN 212222747U CN 202020667479 U CN202020667479 U CN 202020667479U CN 212222747 U CN212222747 U CN 212222747U
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Abstract
The utility model provides a middle-high concentration organic wastewater split-phase treatment system for synchronous nitrogen and phosphorus removal, which comprises a hydrolytic acidification tank, a middle sedimentation tank, a methane production tank, a phosphorus sedimentation tank, an anoxic tank and an aerobic tank, wherein a first side flow pipeline is arranged between the middle sedimentation tank and the anoxic tank, and the supernatant of the middle sedimentation tank flows to the anoxic tank through the first side flow pipeline; a second side flow pipeline is arranged between the methane generating pool and the phosphorus sedimentation pool, and the supernatant of the methane generating pool flows to the phosphorus sedimentation pool through the second side flow pipeline; a fifth pipeline is arranged between the phosphorus sedimentation tank and the anoxic tank. The well high concentration organic waste water split-phase processing system of synchronous nitrogen and phosphorus removal improve anaerobic reactor shock resistance load capacity, shorten anaerobic reactor start time, hydrolysis acidification pond and methane production pond part go out water respectively and flow to oxygen deficiency pond and phosphorus sedimentation tank simultaneously, both can reduce the replenishment of exogenous carbon source, also can promote the excessive phosphorus of inhaling of good oxygen stage phosphorus accumulation fungus, reduce throwing of flocculating agent and throw, finally save the running cost.
Description
Technical Field
The utility model relates to the technical field of environmental engineering, and in particular to a middle and high concentration organic wastewater split-phase treatment system for synchronous nitrogen and phosphorus removal.
Background
The waste water produced in slaughtering and food processing industries belongs to medium-high concentration organic waste water, and has high COD, nitrogen and phosphorus concentration and large water quantity and water quality fluctuation. The wastewater is generally treated by a single-phase anaerobic coupled anoxic-aerobic system, wherein the single-phase anaerobic treatment stage of the system mainly removes organic pollutants in the wastewater, and the anoxic-aerobic treatment stage mainly realizes denitrification and dephosphorization and advanced treatment of the organic pollutants.
However, the single-phase anaerobic coupled anoxic-aerobic system has the following disadvantages in the use process:
1. the single-phase anaerobic treatment stage is slow in starting, long in time consumption and low in impact load resistance;
2. in the former stage, after most of organic matters are removed by single-phase anaerobic treatment, when denitrification treatment is carried out by a subsequent anoxic-aerobic process, the situation of insufficient carbon source often occurs, and in order to remove the total nitrogen in the wastewater, the carbon source needs to be additionally added;
3. to further reduce the total phosphorus in the wastewater, more flocculant needs to be added.
Aiming at medium and high concentration organic wastewater which needs nitrogen and phosphorus removal and has large water quantity and water quality fluctuation, an effective and impact-resistant synchronous decarburization and phosphorus removal device which saves the dosage of externally added medicaments and reduces the operation cost is urgently needed.
Disclosure of Invention
In order to solve at least part of the above technical problem, the utility model provides a well high concentration organic waste water phase splitting processing system of synchronous nitrogen and phosphorus removal, it includes: the system comprises a hydrolysis acidification tank, a middle sedimentation tank, a methane production tank, a phosphorus sedimentation tank, an anoxic tank, an aerobic tank, a first pipeline communicated with the hydrolysis acidification tank and the middle sedimentation tank, a second pipeline communicated with the middle sedimentation tank and the methane production tank, a third pipeline communicated with the methane production tank and the anoxic tank and a fourth pipeline communicated with the anoxic tank and the aerobic tank; a first side flow pipeline is arranged between the intermediate sedimentation tank and the anoxic tank, and supernatant in the intermediate sedimentation tank flows to the anoxic tank through the first side flow pipeline; a second side flow pipeline is arranged between the methane generating pool and the phosphorus sedimentation pool, and the supernatant of the methane generating pool flows to the phosphorus sedimentation pool through the second side flow pipeline; and a fifth pipeline is arranged between the phosphorus sedimentation tank and the anoxic tank.
In some embodiments, in the middle-high concentration organic wastewater split-phase treatment system for simultaneous nitrogen and phosphorus removal, a sludge return pipe is arranged between the hydrolysis acidification tank and the intermediate sedimentation tank, and sludge precipitated in the intermediate sedimentation tank flows back to the hydrolysis acidification tank through the sludge return pipe.
In some embodiments, in the middle-high concentration organic wastewater phase-splitting treatment system for simultaneous nitrogen and phosphorus removal, a first inoculated sludge is arranged in the hydrolytic acidification tank, the first inoculated sludge is hydrolytic acidification sludge, the water content of the first inoculated sludge is 96% -99%, and the volume of the first inoculated sludge is 1/4-1/3 of the volume of the hydrolytic acidification tank.
In some embodiments, in the system for treating high-concentration organic wastewater with simultaneous nitrogen and phosphorus removal, the reaction pH in the hydrolysis acidification tank is 4.5-5.5, and the reaction temperature is 20-25 ℃, 30-35 ℃, 50-55 ℃ or 70-75 ℃.
In some embodiments, in the middle-high concentration organic wastewater phase separation treatment system for simultaneous nitrogen and phosphorus removal, a second inoculated sludge is arranged in the methanogenesis pool, the second inoculated sludge is anaerobic sludge or anaerobic granular sludge, and the volume of the second inoculated sludge is 1/4-1/3 of the volume of the methanogenesis pool.
In some embodiments, in the middle-high concentration organic wastewater phase-splitting treatment system for synchronous nitrogen and phosphorus removal, the reaction pH in the methanogenesis pool is 7-8, and the reaction temperature is 20-25 ℃, 30-35 ℃ or 50-55 ℃.
In some embodiments, in the split-phase treatment system for medium and high concentration organic wastewater with simultaneous nitrogen and phosphorus removal, the anaerobic treatment process adopted in the methanogenesis tank is an upflow anaerobic sludge blanket, an expanded granular sludge blanket, an IC anaerobic reactor, an anaerobic baffle reactor or a sludge blanket-filter.
In some embodiments, in the middle-high concentration organic wastewater phase separation treatment system for simultaneous nitrogen and phosphorus removal, the volume of the supernatant output by the methanogenesis pool through the second side-stream pipeline is less than or equal to 30% of the total volume of the supernatant output by the methanogenesis pool.
In some embodiments, in the middle-high concentration organic wastewater phase-splitting treatment system for simultaneous nitrogen and phosphorus removal, a flocculating agent is added into the phosphorus sedimentation tank, and the flocculating agent is one or more of an inorganic flocculating agent, an organic flocculating agent and a microbial flocculating agent with a phosphorus removal effect.
In some embodiments, in the middle-high concentration organic wastewater split-phase treatment system for simultaneous nitrogen and phosphorus removal, the anoxic tank and the aerobic tank can adopt a form of a first-stage anoxic tank-aerobic tank or a form of a multi-stage anoxic tank-aerobic tank.
The embodiment of the utility model provides a well high concentration organic waste water phase splitting processing system of synchronous nitrogen and phosphorus removal at least has following one of beneficial effect:
in the middle-high concentration organic wastewater split-phase treatment system for synchronous nitrogen and phosphorus removal, parameters such as pH, temperature, volume load, inoculated sludge and the like are respectively regulated and controlled in an anaerobic stage, so that a hydrolytic acidification tank and a methane production tank are separated in the anaerobic treatment stage; after separation, part of the sewage flows to a subsequent anoxic tank after being treated by the hydrolytic acidification tank, a high-quality carbon source generated by hydrolytic acidification is used as a carbon source supplement of the anoxic tank, and part of the sewage flows to a phosphorus precipitation tank after being treated by the methanogenesis tank to carry out chemical phosphorus removal, so that the phosphorus absorption balance of anaerobic phosphorus release and aerobic excessive phosphorus absorption of phosphorus accumulating bacteria is broken, and the aerobic phosphorus absorption effect is promoted.
In the middle and high concentration organic waste water phase splitting processing system of synchronous nitrogen and phosphorus removal, through separation hydrolysis acidification pond and methane production pond, improve anaerobic reactor shock resistance load capacity, shorten anaerobic reactor start-up time, hydrolysis acidification pond and methane production pond partial outflow respectively flow to oxygen deficiency pond and phosphorus sedimentation tank simultaneously, both can reduce the replenishment of exogenous carbon source, also can promote the excessive phosphorus uptake of aerobic phase phosphorus accumulating bacteria, reduce throwing of flocculating agent, finally save the running cost.
Drawings
FIG. 1 is a schematic structural diagram of a middle-high concentration organic wastewater phase-splitting treatment system for simultaneous denitrification and dephosphorization according to one embodiment of the present invention.
Reference numerals:
1 represents a hydrolysis acidification tank, 2 represents a middle sedimentation tank, 3 represents a methane production tank, 4 represents a phosphorus sedimentation tank, 5 represents an anoxic tank, 6 represents an aerobic tank, 7 represents a first pipeline, 8 represents a second pipeline, 9 represents a third pipeline, 10 represents a fourth pipeline, l1 represents a first side stream pipeline, 12 represents a second side stream pipeline, 13 represents a fifth pipeline, 14 represents a sludge return pipeline, 15 represents a sludge tank, and 16 represents a sixth pipeline.
Detailed Description
Reference will now be made in detail to various exemplary embodiments of the invention, which should not be considered limiting of the invention, but rather should be understood to be a more detailed description of certain aspects, features and embodiments of the invention.
It is to be understood that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. Further, to the extent that numerical ranges are recited in the present disclosure, it is understood that the upper and lower limits of the range, and each intervening value therebetween, is specifically disclosed. Every smaller range between any stated value or intervening value in a stated range and any other stated or intervening value in a stated range is also encompassed within the invention. The upper and lower limits of these smaller ranges may independently be included or excluded in the range.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Although only the preferred methods and materials are described in this disclosure, any methods and materials similar or equivalent to those described herein can be used in the practice or testing of the present disclosure. All documents mentioned in this specification are incorporated by reference herein for the purpose of disclosing and describing the methods and/or materials associated with the documents. In case of conflict with any incorporated document, the present specification will control.
It will be apparent to those skilled in the art that various modifications and variations can be made in the embodiments of the present disclosure without departing from the scope or spirit of the disclosure. The specification and examples are exemplary only.
As used herein, the terms "comprising," "including," "having," "containing," and the like are open-ended terms that mean including, but not limited to.
As used herein, "and/or" includes any and all combinations of the stated items.
The present invention will be further described with reference to the following detailed description and accompanying drawings.
As shown in figure 1, the utility model provides a medium and high concentration organic wastewater phase-splitting treatment system for synchronous denitrification and dephosphorization, which comprises: the system comprises a hydrolysis acidification tank 1, a middle sedimentation tank 2, a methane production tank 3, a phosphorus sedimentation tank 4, an anoxic tank 5, an aerobic tank 6, a first pipeline 7 for communicating the hydrolysis acidification tank 1 with the middle sedimentation tank 2, a second pipeline 8 for communicating the middle sedimentation tank 2 with the methane production tank 3, a third pipeline 9 for communicating the methane production tank 3 with the anoxic tank 5 and a fourth pipeline 10 for communicating the anoxic tank 5 with the aerobic tank 6; a first side flow pipeline 11 is arranged between the intermediate sedimentation tank 2 and the anoxic tank 5, and supernatant in the intermediate sedimentation tank 2 flows to the anoxic tank 5 through the first side flow pipeline 11; a second side flow pipeline 12 is arranged between the methane generating tank 3 and the phosphorus sedimentation tank 4, and the supernatant of the methane generating tank 3 flows to the phosphorus sedimentation tank 4 through the second side flow pipeline 12; a fifth pipeline 13 is arranged between the phosphorus sedimentation tank 4 and the anoxic tank 5.
In the scheme, the medium-high concentration organic wastewater needs to be filtered by a grid to remove large-particle impurities before entering the hydrolysis acidification tank 1, and needs to be neutralized by a neutralization tank, wherein the pH value of the neutralized wastewater is 6-9.
In the middle and high concentration organic wastewater split-phase treatment system for synchronous nitrogen and phosphorus removal of the utility model, after the middle and high concentration organic wastewater is pretreated by a grid, pH and water quantity adjustment, the sewage is lifted to a hydrolysis acidification tank 1; in the hydrolysis acidification tank 1, organic matters are decomposed and converted into carbonates, volatile organic acids (VFAs) and the like by hydrolysis acidification bacteria, hydrogen-producing acetogenic bacteria and the like; the effluent of the hydrolysis acidification tank 1 flows to a middle sedimentation tank 2 through a first pipeline 7, mud-water separation is carried out in the middle sedimentation tank 2, wherein one part of sewage flows to a methanogenesis tank 3 through a second pipeline 8, the other part of sewage flows to an anoxic tank 5 through a first side flow pipeline ll, and the sludge precipitated in the middle sedimentation tank 2 flows back to the hydrolysis acidification tank 1; in the methane-producing pool 3, substrates such as organic acid and the like generated in the hydrolysis acidification pool 1 are utilized by methanobacterium to generate substances such as methane, carbon dioxide and the like, the methane-producing pool 3 is subjected to water-gas-solid three-phase separation, and the effluent I of the methane-producing pool 3Part of the wastewater flows to the anoxic tank 5 through a third pipeline 9, the other part of the wastewater flows to the phosphorus sedimentation tank 4 through a second side-stream pipeline 12, chemical phosphorus removal is completed in the phosphorus sedimentation tank 4 under the action of a flocculating agent, and the sewage after phosphorus removal flows to the anoxic tank 5 through a fifth pipeline 13; the anoxic tank 5 mainly performs denitrification, the denitrifying bacteria utilize organic matters in the sewage as carbon sources to reduce nitrate nitrogen brought by the return flow of the nitrifying liquid in the aerobic tank 6 into N2And released into the air, the concentration of organic matter continues to decrease; the effluent of the anoxic tank 5 automatically flows to the aerobic tank 6, organic matters are further degraded by microorganisms in the aerobic tank 6, ammonia nitrogen is converted into nitrate nitrogen or nitrite nitrogen, phosphorus is absorbed along with excessive phosphorus-accumulating bacteria and is reduced at a higher speed, and finally the effluent reaching the standard is discharged. In the whole reaction process, the excess sludge generated by the biochemical treatment system and the chemical sludge generated by the phosphorus sedimentation tank 4 are discharged to the sludge tank 15, and are transported and disposed after being dehydrated.
In the scheme, the system further comprises a sludge tank 15 which is used for temporarily storing the residual sludge.
In the above scheme, the system further comprises a sixth pipeline 16, and the sixth pipeline 16 is used for returning the nitrified liquid in the aerobic tank 6 to the anoxic tank 5.
In the scheme, the supernatant flowing from the middle sedimentation tank 2 to the anoxic tank 5 accounts for the liquid in the middle sedimentation tank 2 according to the proportion of the supernatant to the effluent BOD of the methanogenesis tank 35the/TN is determined that the supernatant flowing into the anoxic tank 5 should ensure the BOD of the mixed inlet water of the anoxic tank 55/TN≥4。
In the above scheme, a sludge return pipe 14 is arranged between the hydrolysis acidification tank 1 and the intermediate sedimentation tank 2, and the sludge precipitated in the intermediate sedimentation tank 2 returns to the hydrolysis acidification tank 1 through the sludge return pipe 14.
And the sludge precipitated in the intermediate sedimentation tank 2 flows back to the hydrolysis acidification tank 1, and the residual sludge is discharged to a sludge field. Wherein the sludge reflux proportion of the intermediate sedimentation tank 2 is 50-100%.
In the scheme, a first inoculation sludge is arranged in the hydrolysis acidification tank 1, the first inoculation sludge is hydrolysis acidification sludge, the water content of the first inoculation sludge is 96% -99%, and the volume of the first inoculation sludge is 1/4-1/3 of the volume of the hydrolysis acidification tank 1.
In the scheme, the first inoculation sludge is taken from a two-phase anaerobic digestion acidification tank or a single-phase anaerobic reactor.
In the scheme, the reaction pH value in the hydrolysis acidification tank 1 is 4.5-5.5, and the reaction temperature is 20-25 ℃, 30-35 ℃, 50-55 ℃ or 70-75 ℃.
In the scheme, second inoculated sludge is arranged in the methane-producing pool 3, the second inoculated sludge is anaerobic sludge or anaerobic granular sludge, and the volume of the second inoculated sludge is 1/4-1/3 of the volume of the methane-producing pool 3.
In the scheme, the excess sludge generated by the methane generating tank 3 is discharged to a sludge tank 15; the chemical sludge produced by the phosphorus precipitation tank 4 is discharged to the sludge tank 15.
In the scheme, the reaction pH value in the methane generating pool 3 is 7-8, and the reaction temperature is 20-25 ℃, 30-35 ℃ or 50-55 ℃.
In the scheme, the methane-producing tank 3 adopts an anaerobic treatment process including an upflow anaerobic sludge blanket, an expanded granular sludge blanket, an IC anaerobic reactor, an anaerobic baffle reactor or a sludge blanket-filter.
In the above scheme, the volume of the supernatant outputted from the methane generating tank 3 through the second side flow pipeline 12 is less than or equal to 30% of the total volume of the supernatant outputted from the methane generating tank 3.
In the scheme, a flocculating agent is added into the phosphorus sedimentation tank 4, and the flocculating agent is one or more of an inorganic flocculating agent, an organic flocculating agent and a microbial flocculating agent with a phosphorus removal effect.
In the scheme, the anoxic tank 5 and the aerobic tank 6 can adopt a form of a first-stage anoxic tank-aerobic tank or a form of a multi-stage anoxic tank-aerobic tank.
In the scheme, the aerobic tank can adopt any one of an activated sludge process, a contact oxidation process or a membrane bioreactor.
Examples
Example 1:
utilize the middle and high concentration organic waste water phase splitting processing system of synchronous nitrogen and phosphorus removal handle the pot bottom waste water that certain white spirit production produced, the concrete requirement is as follows:
| serial number | Index (I) | Unit of | Quality of raw water | Quality of |
| 1 | pH value | - | 4.5～5.5 | 6.0～9.0 |
| 2 | Biochemical Oxygen Demand (BOD)5) | mg/L | 13400 | ≤20 |
| 3 | Chemical Oxygen Demand (COD) | mg/L | 24600 | ≤60 |
| 4 | Ammonia nitrogen(NH4 +-N) | mg/L | 160 | ≤5 |
| 5 | Total Nitrogen (TN) | mg/L | 295 | ≤15 |
| 6 | Total phosphorus (in terms of P) | mg/L | 208 | ≤0.5 |
(1) Utilize the system to the bottom of a boiler waste water carry out the processing procedure who handles to do:
wastewater at the bottom of a boiler → a fine grid → a neutralization regulating tank → a hydrolysis acidification tank 1 → a middle sedimentation tank 2 → a methanogenesis tank 3(UASB tank) → a primary anoxic tank → a primary aerobic tank → a secondary anoxic tank → a secondary aerobic tank → a sedimentation tank → effluent is discharged outside
(2) Key pool function and operating parameters
The neutralization regulating tank is used for carrying out homogenizing and uniform quantity regulation on the wastewater at the bottom of the pot, and the pH value of the inlet water of the hydrolysis acidification tank 1 is regulated to 7.0 +/-0.2.
The hydrolysis acidification pool 1 is used for carrying out hydrolysis acidification on the water at the bottom of the boiler, the reaction temperature of the hydrolysis acidification pool 1 is 55 +/-2 ℃, the first inoculated sludge in the hydrolysis acidification pool 1 is taken from a certain municipal sludge high-temperature single-phase anaerobic reactor, the water content of the first inoculated sludge is 97%, the initial inoculation amount is 1/3 of the effective volume of the hydrolysis acidification pool 1, a water outlet reflux pump of the hydrolysis acidification pool 1 is arranged to ensure that the ascending flow velocity in the hydrolysis acidification pool 1 is 1.0m/h, after the hydrolysis acidification pool 1 is started, the MLSS of a reaction system is 6000mg/L, and the pH in the system is about 5.0.
The intermediate sedimentation tank 2 receives the effluent of the hydrolysis acidification tank 1, performs sludge-water separation, and reflows the precipitated sludge to the hydrolysis acidification tank 1 with the reflow proportion of 100%; because the effluent BOD of the methane-producing pool 35the/TN is 1850/295 is 6.27 is more than or equal to 4, so the precipitated sewage completely enters the methane generating tank 3, and the proportion of the side flow to the first-stage anoxic tank is 0 percent.
The UASB pool adopts medium-temperature anaerobic digestion, the reaction temperature is 35 +/-2 ℃, the second inoculated sludge is taken from a certain municipal sludge high-temperature single-phase anaerobic reactor, the water content of the second inoculated sludge is 97%, the initial inoculation amount is 1/4 of the effective volume of the UASB pool, the pH value in the UASB pool gradually rises along with the progress of methanogenesis reaction, and the pH value in the UASB pool is controlled to be 7-8.
After three-phase separation of the reaction product in the UASB tank, 15% of effluent flows to the phosphorus sedimentation tank 4, and 85% of effluent directly enters the first-stage anoxic tank.
And polyaluminium chloride (PAC) is added into the phosphorus sedimentation tank 4, and the adding amount is 200 mg/L.
Because the project has higher removal rate of organic matters, TN and TP, a two-stage anoxic-aerobic treatment mode is considered for effluent of the UASB tank, the proportion of nitrifying liquid in the two-stage aerobic tank flowing back to the anoxic tank is 400%, and polyaluminium chloride is respectively added into the first-stage aerobic tank and the second-stage aerobic tank for chemical phosphorus removal.
Example 2:
utilize the medium and high concentration organic waste water phase splitting processing system of synchronous nitrogen and phosphorus removal handle the comprehensive waste water that certain dairy products manufacturing enterprise produced, the concrete requirement is as follows:
| serial number | Index (I) | Unit of | Quality of raw water | Quality of |
| 1 | pH value | - | 6.0～9.0 | 6.0～9.0 |
| 2 | Biochemical Oxygen Demand (BOD)5) | mg/L | ≤3200 | ≤20 |
| 3 | Chemical Oxygen Demand (COD) | mg/L | ≤1600 | ≤60 |
| 4 | Ammonia Nitrogen (NH)4 +-N) | mg/L | ≤20 | ≤5 |
| 5 | Total Nitrogen (TN) | mg/L | ≤180 | ≤30 |
| 6 | Total phosphorus (in terms of P) | mg/L | ≤15 | ≤0.5 |
(1) System flow
Dairy product wastewater → pretreatment (grille + air flotation) → regulating tank → hydrolytic acidification tank 1 → intermediate sedimentation tank 2 → methanogenesis tank 3(ABR tank) → anoxic tank → aerobic tank 6 → discharged water
(2) Key pool function and operating parameters
The dairy product wastewater is pretreated to remove most SS and then enters an adjusting tank, and the water quantity and the water quality are homogenized in the adjusting tank.
The reaction temperature of the hydrolysis acidification tank 1 is normal temperature, and the rising flow rate is 0.8 m/h.
The intermediate sedimentation tank 2 receives the effluent of the hydrolysis acidification tank 1, performs sludge-water separation, and reflows the precipitated sludge to the hydrolysis acidification tank 1 with the reflow proportion of 100%; because the effluent BOD of the methane-producing pool 35And the concentration of the/TN is 480/150 which is 3.2 which is less than or equal to 4, and 5 percent of the precipitated sewage flows to the anoxic tank through the first side flow pipeline 11 side, and the rest 95 percent of the sewage flows to the ABR tank directly.
The reaction temperature of the ABR pool is normal temperature, 7.5 percent of effluent flows to the phosphorus sedimentation tank 4 through the second side flow pipeline 12 side, and the rest flows directly into the anoxic pool.
And polyaluminium chloride (PAC) is added into the phosphorus sedimentation tank 4, and the adding amount is 100 mg/L.
The proportion of the nitrified liquid in the aerobic tank 6 flowing back to the anoxic tank is 400 percent.
It will be apparent to those skilled in the art that various modifications and variations can be made in the embodiments of the present disclosure without departing from the scope or spirit of the disclosure. Other embodiments will be apparent to those skilled in the art from consideration of the specification. The specification and examples are exemplary only.
Claims (10)
1. The utility model provides a well high concentration organic waste water phase separation processing system of synchronous nitrogen and phosphorus removal which characterized in that, this system includes: the device comprises a hydrolysis acidification tank (1), a middle sedimentation tank (2), a methane production tank (3), a phosphorus sedimentation tank (4), an anoxic tank (5), an aerobic tank (6), a first pipeline (7) for communicating the hydrolysis acidification tank (1) with the middle sedimentation tank (2), a second pipeline (8) for communicating the middle sedimentation tank (2) with the methane production tank (3), a third pipeline (9) for communicating the methane production tank (3) with the anoxic tank (5) and a fourth pipeline (10) for communicating the anoxic tank (5) with the aerobic tank (6); wherein,
a first side flow pipeline (11) is arranged between the intermediate sedimentation tank (2) and the anoxic tank (5), and supernatant of the intermediate sedimentation tank (2) flows to the anoxic tank (5) through the first side flow pipeline (11);
a second side flow pipeline (12) is arranged between the methanogenesis pool (3) and the phosphorus sedimentation pool (4), and the supernatant of the methanogenesis pool (3) flows to the phosphorus sedimentation pool (4) through the second side flow pipeline (12);
a fifth pipeline (13) is arranged between the phosphorus sedimentation tank (4) and the anoxic tank (5).
2. The middle-high concentration organic wastewater split-phase treatment system for simultaneous nitrogen and phosphorus removal according to claim 1, wherein a sludge return pipe (14) is arranged between the hydrolysis acidification tank (1) and the intermediate sedimentation tank (2), and sludge precipitated in the intermediate sedimentation tank (2) returns to the hydrolysis acidification tank (1) through the sludge return pipe (14).
3. The middle-high concentration organic wastewater phase separation treatment system for simultaneous nitrogen and phosphorus removal according to claim 2, wherein a first inoculated sludge is arranged in the hydrolytic acidification tank (1), the first inoculated sludge is hydrolytic acidification sludge, the water content of the first inoculated sludge is 96% -99%, and the volume of the first inoculated sludge is 1/4-1/3 of the volume of the hydrolytic acidification tank (1).
4. The medium-high concentration organic wastewater phase-splitting treatment system for synchronous nitrogen and phosphorus removal of claim 3, wherein the reaction pH value in the hydrolysis acidification tank (1) is 4.5-5.5, and the reaction temperature is 20-25 ℃, 30-35 ℃, 50-55 ℃ or 70-75 ℃.
5. The medium-high concentration organic wastewater phase separation treatment system for simultaneous nitrogen and phosphorus removal according to claim 1, wherein a second inoculated sludge is arranged in the methanogenesis pool (3), the second inoculated sludge is anaerobic sludge or anaerobic granular sludge, and the volume of the second inoculated sludge is 1/4-1/3 of the volume of the methanogenesis pool (3).
6. The medium-high concentration organic wastewater phase separation treatment system for synchronous nitrogen and phosphorus removal according to claim 5, wherein the reaction pH in the methanogenesis tank (3) is 7-8, and the reaction temperature is 20-25 ℃, 30-35 ℃ or 50-55 ℃.
7. The middle-high concentration organic wastewater split-phase treatment system for synchronous nitrogen and phosphorus removal according to claim 1, wherein the methane-generating tank (3) adopts an anaerobic treatment process of an upflow anaerobic sludge bed, an expanded granular sludge bed, an IC anaerobic reactor, an anaerobic baffle reactor or a sludge bed-filter.
8. The middle-high concentration organic wastewater phase separation treatment system for simultaneous nitrogen and phosphorus removal according to claim 1, wherein the volume of the supernatant outputted from the methanogenesis pool (3) through the second side stream pipeline (12) is less than or equal to 30% of the total volume of the supernatant outputted from the methanogenesis pool (3).
9. The middle-high concentration organic wastewater split-phase treatment system for simultaneous nitrogen and phosphorus removal according to claim 1, wherein a flocculating agent is added into the phosphorus sedimentation tank (4), and the flocculating agent is one or more of an inorganic flocculating agent, an organic flocculating agent and a microbial flocculating agent with a phosphorus removal effect.
10. The split-phase treatment system for the middle and high concentration organic wastewater with simultaneous phosphorus and nitrogen removal of claim 1, wherein the anoxic tank (5) and the aerobic tank (6) can be in the form of a first-stage anoxic tank-aerobic tank or a multi-stage anoxic tank-aerobic tank.
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