CN112979055A - UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation and application method thereof - Google Patents

UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation and application method thereof Download PDF

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CN112979055A
CN112979055A CN202011600313.2A CN202011600313A CN112979055A CN 112979055 A CN112979055 A CN 112979055A CN 202011600313 A CN202011600313 A CN 202011600313A CN 112979055 A CN112979055 A CN 112979055A
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sludge
tank
water
sedimentation tank
composite
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刘贤斌
李路
周安妮
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Wuhan Purgelon Environmental Engineering Technology Co ltd
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Wuhan Purgelon Environmental Engineering Technology Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/105—Phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
    • C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/284—Anaerobic digestion processes using anaerobic baffled reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/308—Biological phosphorus removal

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

The invention provides a UMIF synchronous nitrogen and phosphorus removal integrated tank for on-line fermentation of mixed liquor and an application method thereof. The invention has the advantages of simple total flow, simple control, compact tank type, carbon source saving, residual sludge reduction, low operation cost, high nitrogen and phosphorus removal efficiency and the like.

Description

UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation and application method thereof
Technical Field
The invention belongs to the technical field of online fermentation of main stream activated sludge mixed liquor for sewage treatment, development of an internal carbon source, denitrification, dephosphorization and denitrification and the like, and particularly relates to a UMIF (Un-mixed In-line nutrients) synchronous denitrification and dephosphorization integrated tank for online fermentation of mixed liquor and an application method thereof.
Background
At present, the sewage treatment of China completely enters a stage of removing organic pollutants and high-standard nitrogen and phosphorus removal. Wherein the nitrogen and phosphorus removal technology mainly adopts the synchronous nitrogen and phosphorus removal process of Anaerobic (Anaerobic) phosphorus release, Anoxic (Anaerobic) denitrification, aerobic (Oxic) phosphorus accumulation and aerobic nitrification of continuous flow, such as conventional A2O or modified form A2O, UCT, AOA and the like. In the biochemical reaction process of biological nitrogen and phosphorus removal, phosphorus bacteria and heterotrophic denitrifying bacteria need sufficient soluble and biodegradable organic matters (rbCOD) in sewage, particularly low-molecular-weight Volatile Fatty Acids (VFAs) as carbon sources, and the main problems commonly faced by sewage plants in China are that the C/N (carbon/nitrogen) ratio of inlet water is low, TN (total nitrogen) and TP (total phosphorus) of the inlet water are high, but the carbon sources are insufficient, so that the nitrogen and phosphorus removal effect is poor and the like. Meanwhile, as the effluent quality standards, especially TN and TP indexes, are further improved, although the effluent quality requirements can be better met by adopting a carrier activated sludge method or adopting fixed bed biofilm methods such as a biological aerated filter and the like, the carrier or biofilm method has high investment and operation cost and excessively complex management, and a series of problems in operation control restrict the application of the technologies.
In order to overcome the shortage of carbon source of sewage inlet water, the common practice in engineering design and operation over the past decade is to add organic carbon source (such as methanol, glucose, sodium acetate, acetic acid, etc.) to realize enhanced biological nitrogen and phosphorus removal; in addition, phosphorus removal can be achieved by adding chemical agents (such as PAC and FeCl)3Etc.) to achieve auxiliary chemical phosphorus removal; obviously, the mode of adding the external carbon source or the external medicament undoubtedly obviously increases the consumption of the carbon source and the medicament and the daily operation cost of the sewage plant, increases the final sludge yield, is difficult to be continuously applied in most areas of China, and is inconsistent with the concept of sustainable development and environmental protection in the world at present and green and low carbon. The key point is that sewage plants are not confronted with water inlet carbon sourceThe trouble is caused by the large amount of residual sludge generated by the sludge treatment device per se every day, and the sludge treatment and disposal requires high extra cost and is easy to cause secondary pollution. However, the excess sludge of sewage plants is a resource which can be utilized, and the prior art comprises the steps of adopting sludge to be subjected to mesophilic anaerobic digestion to generate methane for energy recovery, or using sludge compost for greening cultivation and the like. In fact, the residual activated sludge per se contains rich 'internal carbon sources', but the prior art cannot exert the potential carbon source utilization value and is abandoned and buried by white wastes as wastes.
In recent years, research and attempt on development and utilization of "internal carbon sources" of sludge have been started in the theoretical and engineering circles of sewage treatment, and some results and practical applications have been obtained, mainly the invention and application of technologies such as regeneration, adsorption-regeneration, bypass or side-stream hydrolysis and fermentation of primary sludge in a primary sedimentation tank, residual activated sludge in a secondary sedimentation tank, mixed sludge of the primary sludge and the residual activated sludge in the secondary sedimentation tank, and the like indicate the direction of development and utilization of carbon sources for a plurality of sewage plants with insufficient carbon sources for water inflow. However, on the basis of innovation of integration of carbon source development of mixed liquor of main stream activated sludge and nitrogen and phosphorus removal, the invention and practical application are novel, and the forms of a loose biochemical tank, a secondary sedimentation tank, a deep treatment water tank and the like which are separately built are still adopted, so that the sewage treatment process is long, the operation control is complex, the occupied area is large, and the manufacturing cost is relatively high.
Invention patent hydrolytic acidification + A without external carbon source2/O2The method for treating sewage (publication No. CN 110759592A, publication No. 2020.02.07, hereinafter referred to as prior art 1) comprises the steps of filling bionic aquatic weed composite filler in a pool volume of a biochemical pool containing a hydrolysis-acidification pool, wherein the total HRT is 13h, and arranging a stirring device in the whole pool. The invention has 2 defects: part of external carbon sources can be saved theoretically, but the equipment is multiple, the energy consumption is high, the composite filler is high in manufacturing cost and complex to operate, and great uncertainty exists in large-scale engineering application; 2, the common wall of the biochemical pool and the sedimentation pool in the drawing is combined into an integrated pool type, but only the rectangular sedimentation pool is used for separating mud and water, and the yielding water can be stable from the aspects of profession and experienceThe invention reaches the national first-class B standard, but is difficult to stably reach the current first-class A standard, so the invention needs further deepening and perfecting.
The invention relates to a V-shaped gas stripping reflux two-stage precipitation integrated sewage treatment tank (publication No. CN 103395947B, publication No. 2014.10.22, hereinafter referred to as prior art 2), which tightly combines conventional anaerobism, anoxia, aeration, V-shaped clarification and inclined tube precipitation into a whole for the conventional denitrification and dephosphorization of the conventional water quality in a compact treatment manner, and is difficult to adapt to the treatment scale of 1.5 ten thousand meters3The low-cost nitrogen and phosphorus removal of the sewage with the concentration/d and above and/or the low C/N ratio is carried out for two reasons: firstly, the concentration of anaerobic sludge in a conventional anaerobic tank is difficult to reach a high value, and a deep anaerobic environment is difficult to form, the capacity of generating rbCOD or VFAs in the anaerobic zone is weak, and the conversion capacity of an internal carbon source is weak; secondly, the automatic return effect of the nitrifying liquid is not satisfactory, so that the actual sludge concentration of the anoxic zone is slightly insufficient, and the low B/C (BOD) of the centralized sewage plant of the industrial park is treated5the/COD) ratio and the low C/N ratio sewage can only stably reach the national standard first grade B standard, so the integrated sewage treatment tank is not suitable for the higher requirements at present.
Aiming at the defects of the hydrolysis fermentation carbon source development and utilization and the synchronous nitrogen and phosphorus removal technology in two aspects: firstly, the application aspect of large-scale engineering is not enough, and secondly, the high standard, high requirement, low cost and sustainability aspect are not enough, so that it is very necessary to invent and design one of the following methods creatively: the UMIF synchronous denitrification and dephosphorization integrated tank has the characteristics of simple structure, stable operation, low energy consumption, low efficiency, no risk of filler blockage and replacement, easiness in operation and control and the like, ensures the low-cost denitrification and dephosphorization effect of sewage with low C/N ratio, and finally meets the standard discharge requirements.
In conclusion, the continuous innovation in the field of sewage treatment and the practical requirement of engineering can be a long-term and arduous task.
Based on the background and the defects of various known technologies, and the urgent need of low-cost nitrogen and phosphorus removal of sewage with low C/N ratio in the aspects of scale and engineering, the application of the invention is in force.
The invention aims to: provides a simple and convenient main stream active sludge mixed liquid for online hydrolytic fermentation to obtain a rapid internal carbon source and utilize the rapid internal carbon source so as to strengthen low-cost synchronous nitrogen and phosphorus removal of deep anaerobic phosphorus release and endogenous denitrification nitrogen removal and realize preliminary reduction and stable residual sludge for municipal sewage and industrial park sewage with low C/N ratio. The method specifically aims to realize the purposes of simple sewage treatment process, no need of filler, carbon source saving, aeration amount saving, low energy and drug consumption, residual sludge reduction, simple operation control, high nitrogen and phosphorus removal efficiency, good effluent quality and the like by discovering that non-rapid degradation COD in sewage inflow is converted into rbcOD or VFAs under the action of anaerobic hydrolysis acidification and simultaneously converting organic matters contained in residual activated sludge into rbcOD or VFAs through on-line hydrolysis fermentation, namely synchronously performing hydrolysis fermentation on sewage and sludge to obviously improve the nitrogen and phosphorus removal efficiency of sewage and reduce the addition of external carbon sources as far as possible.
The name of the invention is that the mixed liquid is obtained by on-line fermentation of UMIF: the citation paper 1, water supply and drainage, Vol.39 No. 12013, utilizes the side-stream activated sludge hydrolysis technology to strengthen biological nitrogen and phosphorus removal under the condition of low carbon source; the citation paper 2, Chinese Water supply and drainage, Vol.34 No. 242018, is a new breakthrough in biological phosphorus removal theory and practice, from mainstream EBPR to sidestream EBPR. As early as 1972, America scientist James Barnard later known as "father of denitrification and dephosphorization" carried out 100m denitrification experiment for sewage treatment3In the experimental research of/d scale, a UMIF (Un-mixed In-line Fermenters) process based on Dead Zone (Dead Zone) fermentation, namely a process called mixed liquor online hydrolysis fermentation In the current industry, is discovered occasionally, and cannot draw extensive attention to the theoretical world at the time and for a long time later, and extensive and deep research is not carried out, and the UMIF process cannot be popularized and applied In China. The name cited in the invention is that firstly the process principle is partially the same, secondly the convention in the industry is established, thirdly a new creation is createdThe nouns are easy to mix, but the living area fermentation is really different from the dead area fermentation, the invention belongs to great technical innovation and is successfully applied, and the existing invention or the published technology has obvious defects in the aspects of engineering, scale, low cost and the like, so the invention has great time-to-time significance and has very obvious practical application value.
Disclosure of Invention
Aiming at various problems in the prior art, the technical scheme adopted by the invention is as follows:
UMIF synchronous nitrogen and phosphorus removal integrated pool for mixed liquid on-line fermentation is characterized in that: the anaerobic composite anaerobic reactor comprises an up-flow anaerobic composite ABR area 1, an anoxic area 2 and an aerobic area 3, wherein the composite ABR area 1 is communicated with the anoxic area 2 through side wall holes of a water outlet collecting channel at the tail end of the composite ABR area; the anoxic zone 2 is communicated with the aerobic zone 3 through a partition wall hole between the tail end of the anoxic zone 2 and the aerobic zone 3; the integrated tank also comprises a V-shaped secondary sedimentation tank 4, an inclined tube sedimentation tank 5, a plurality of connecting pipelines and accessory facilities, wherein the accessory facilities comprise an external reflux sludge pump 6, an external reflux sludge pipe 16, a reuse sludge tank 9 and a reuse sludge pump 10; the tail end of the aerobic zone 3 is communicated with a partition wall hole below a V-shaped partition wall of the secondary sedimentation tank 4 between the aerobic zone 3 and the secondary sedimentation tank 4; supernatant is collected through a water collecting tank on the water surface of the secondary sedimentation tank and collected to a water collecting channel at the top of a partition wall between the secondary sedimentation tank 4 and the inclined tube sedimentation tank 5, and then the secondary sedimentation tank and the inclined tube sedimentation tank are communicated through an L-shaped hydraulic coagulation spinner; finally, the upper layer clear water is completely collected and conveyed to a water outlet of a main water collecting channel at the tail end of the water tank by a water surface water collecting tank of the inclined tube sedimentation tank 5, and is conveyed to a subsequent filter tank by a pipeline for filtering treatment, or is directly conveyed to a contact disinfection tank in a factory for disinfection and sterilization and then is discharged out of the factory; the bottom of the V-shaped secondary sedimentation tank 4 is respectively communicated with the sludge discharge tank and the inlet of the composite ABR area 1 through pipelines, the tail end of the aerobic area 3 is connected with the starting end of the anoxic area 2 through an internal reflux pipeline, and the inclined tube sedimentation tank 5 is communicated with the starting end of the anoxic area 2 through a sludge recycling pipeline.
The composite ABR area 1 comprises a three-grid or four-grid rectangular pool body which is respectively a first grid chamber 11, a second grid chamber 12, a third grid chamber 13 and a fourth grid chamber 14, wherein the first grid chamber 11 is internally provided with a muddy water inlet pipe 15 and an up-flow anaerobic water distributor 17 connected with the muddy water inlet pipe, and the composite ABR area 1 further comprises a water collecting tank 18, a baffling partition wall 19, a flow guide plate 20, a flow guide slope 21, a sediment discharge pipe 23 and a tail end water collecting channel 22; at most three downflow channels are formed between each adjacent cell through a baffling partition wall 19; during operation, the flowing direction of the activated sludge mixed liquor is sequentially a first grid chamber 11 → a second grid chamber 12 → a third grid chamber 13(→ a fourth grid chamber 14), and the first grid chamber 11 and the second grid chamber are communicated through a down-flow channel to form main grid chambers in an up-flow type flowing direction, and the mixed liquor flows out of the last grid chamber; each cell is provided with an upper water collecting tank 18 and a bottom sediment discharge pipe 23, and the sediment discharge pipe 23 is arranged at the position, which is lower than the downstream position of the center of the bottom and is parallel to the direction of the guide plate 20; the remaining cells, except the first cell 11, each have a baffle 20 and two flow directing ramps 21.
The upflow anaerobic water distributor 17 sprays water downwards and forms uniform upflow by the reflection of the bottom of the pool.
The upflow anaerobic water distributor 17 comprises a large-caliber tee joint positioned in the middle, the central tee joint of the tee joint faces upwards and is in butt joint with a water inlet pipe, the other two horizontal outlets are respectively connected with a horizontal cross joint, the other three branch outlets of the cross joint are respectively connected with a pair of downward small-caliber tee joints and a horizontal medium-caliber tee joint, two sides of the medium-caliber tee joint are horizontally connected with two downward medium-small-caliber tee joints, the water outlets of each small-caliber tee joint and the medium-small-caliber tee joints are connected with nozzles, the nozzles are all sprayed towards the bottom of the tank, and the positions of the bottom of the tank, which correspond to the nozzles, are provided with.
The water surface of each cell is provided with a plurality of parallel water collecting grooves 18, the ascending water flow is uniformly and densely collected, and the number of the water collecting grooves 18 of each cell is the same.
The baffling partition wall 19 and the tank body partition wall form a down-flow channel, and the ratio of the width of the down-flow channel to the width of the up-flow grid chamber is 1: 6-9.
The application method of the UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation is characterized by comprising the following steps:
step 1, mixing external reflux activated sludge RAS from an external reflux sludge pump 6 in a sludge discharge tank of a V-shaped secondary sedimentation tank 4 with inlet water (sewage to be treated) to form an activated sludge mixed solution, entering a first grid of an up-flow anaerobic composite ABR area 1 through a water inlet pipe 15, spraying water downwards by an up-flow anaerobic water distributor 17, reflecting by the bottom of the tank to form uniform up-flow, collecting a plurality of parallel water collecting tanks 18 on the water surface to enter a down channel of a second grid 12 of the composite ABR area, reaching the bottom of the second grid 12 through a channel between a baffle plate 20 and a flow guiding slope 21 of a baffle partition wall 19, and reflecting at the bottom of the tank to form up-flow in the second grid;
step 2, the ascending flow of the second grid 12 in the composite ABR area is collected by a water collecting tank 18 and then sequentially enters a descending channel of a third grid 13; the above-mentioned steps are repeated, and the mixed liquor is collected in the last water collecting tank 18 and then enters the end water collecting channel 22 of the composite ABR area;
step 3, enabling mixed liquid of a water collecting channel 22 at the tail end of the composite ABR zone to enter the starting end of an anoxic zone 2, enabling an internal reflux nitrifying liquid from the tail end of the aerobic zone 3 to enter the starting end of the anoxic zone 2, and enabling gas stripping reflux activated sludge RAS from a gas stripping reflux device 7 in a V-shaped secondary sedimentation tank 4, recycled sludge from a recycled sludge pump 10 of an advanced treatment inclined tube sedimentation tank 5 and a spare external carbon source to enter;
step 4, introducing mixed liquor at the tail end of the anoxic zone 2 into an aerobic zone 3 for aeration treatment, wherein mixed liquor in the anoxic zone 2 and the aerobic zone 3 is in a plug flow type, most of nitrified liquor fully nitrified at the tail end of the aerobic zone 3 returns to the beginning end of the anoxic zone 2 through a nitrified liquor internal reflux pump, and a small part of nitrified liquor enters a V-shaped secondary sedimentation tank 4 for sludge-water separation and sedimentation treatment;
step 5, sending most of the concentrated sludge at the bottom of the secondary sedimentation tank 4 serving as external return sludge RAS to a first grid chamber 11 at the starting end of the ABR zone 1 by an external return sludge pump 6, and discharging a small amount of sludge serving as residual sludge to a sludge treatment unit; the suspended concentrated sludge in the middle layer of the secondary sedimentation tank 4 continuously flows back to the starting end of the anoxic zone 2 in real time by the gas stripping reflux device 7; the supernatant of the secondary sedimentation tank 4 enters an inclined tube sedimentation tank 5 for further advanced treatment;
and 6, adding auxiliary chemical phosphorus removal and flocculation precipitation agents into the inclined tube sedimentation tank 5 according to the running condition of water quality, further removing residual pollutants to obtain high-quality effluent, and conveying a small amount of sludge generated by coagulation sedimentation in the inclined tube sedimentation tank 5 to the starting end of the anoxic zone 2 for reuse through a reuse sludge pump 10.
The composition of the UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquor online fermentation comprises the following 6 parts:
(1) an up-flow anaerobic composite ABR zone 1, (2) an anoxic zone 2, (3) an aerated aerobic zone 3, (4) a V-shaped secondary sedimentation tank 4, (5) an inclined tube sedimentation tank 5, and (6) a partition wall hole, a channel/a pipeline and an accessory facility system which are mutually connected. The main flow direction of sewage treatment is as follows in sequence: water inlet → upflow anaerobic combined ABR area 1 → anoxic area 2 → aerobic aeration area 3 → V-shaped secondary sedimentation tank 4 → inclined tube sedimentation tank 5 → water outlet.
The invention realizes the purpose by using innovative technical means and unprecedented simple and rapid processes.
Firstly, the method is a great innovation of anaerobic reactor technology, namely, a hydrolysis acidification and anaerobic composite ABR reactor pool type (hereinafter referred to as a composite ABR area) applied in the same period is utilized to replace a conventional traditional ABR pool or/and an anaerobic reaction pool. The internal equipment, the device and the structure of the composite ABR area 1 are unique and not complicated, the manufacture of the equipment in the pool, the installation of the device and the civil construction are humanized, the engineering implementation is easy, although the so-called exclusive tare or secret weapons are not provided, the conception structure is delicate enough, the hydraulic flow state is scientific and reasonable in the operation process, is very beneficial to the smooth proceeding of hydrolytic acidification and anaerobic reaction, because the structure ensures that the sludge and the sewage are mixed well, the contact between the activated sludge microorganisms and the pollutants in the sewage is sufficient but not violent, stable and uniform upward flow can be formed in each grid pool, no dead zone can occur, the positions with different depths from the first grid 11 to the last grid 14 are stable 'living zones' under different substrate concentrations, therefore, the method is a continuous and stable plug flow type treatment type, and is particularly suitable for large-scale and engineering continuous production.
Secondly, innovative technologies such as 'hydraulic elutriation' and 'self-concentration' help the sludge concentration to be increased, and the dominant bacteria are gradually enriched. In the second grid chamber 12 and the subsequent grid chambers of the composite ABR area, because of adopting a large V-shaped structure, hydraulic dead angles are completely eliminated, the bottom flow rate is obviously higher than the middle upper part, the risk of sludge deposition and decomposition and sediment siltation is greatly reduced, meanwhile, based on the principles of hydraulic elutriation and self-concentration, the invention adopts relatively high hydraulic load parameters, so that the structure can automatically make large-particle and heavy-particle anaerobic activated sludge in the lower layer, medium-particle and small-particle sludge in the middle layer and small-particle and flocculent sludge in the upper layer, and because a large number of water collecting grooves are specially arranged, the load of a water outlet weir mouth is reduced to ensure that the upflow flow state is smooth and uniform, the whole pool not only automatically carries out hydraulic classification, but also ensures that hydrolytic acidification sludge with high concentration is gathered in the reaction pool, and conventional anaerobic activated sludge can be "lost" to an anoxic area 2 (automatically forms balance) when the total sludge concentration reaches a certain high value, the anaerobic activated sludge entering the anoxic zone 2 completes the denitrification dephosphorization of the anoxic zone 2 and the subsequent aerobic phosphorus absorption process, and forms the repeated circulation of anaerobic 1 → anoxic 2 → aerobic 3 → secondary sedimentation tank 4 and external reflux sludge pump 6 → returning to the anaerobic 1, wherein part of sludge after full phosphorus absorption is discharged out of the system in the form of residual sludge to realize the final dephosphorization of the system.
Thirdly, the unprecedented simple process is utilized to realize the comprehensive goals of deep anaerobism, energy conservation, more acid production and the like. The composite ABR zone 1 has no forced stirrer, excessive mixing can not occur, 3-4 levels of anaerobic chambers are provided, the oxidation-reduction potential ORP of a large V-shaped area at the lower layer of a pool behind the second chamber 11 can be as low as-400 to-250 mV, so a deep anaerobic environment can be formed, the anaerobic sludge can fully release phosphorus, the hydrolytic acidification reaction rate can be obviously improved under the deep anaerobic environment by adding higher anaerobic sludge concentration, the concentration of rbcOD or VFAs in the effluent of the composite ABR zone 1 is increased by 18-58 mg/L compared with that of rbcOD or VFAs in the influent, wherein the VFAs mainly comprises mixed acids such as acetic acid, propionic acid and butyric acid, the mixed organic acids are more beneficial to the absorption of microorganisms such as phosphorus-accumulating bacteria denitrifying bacteria and the like than single organic acids, the synchronous denitrification of denitrification and denitrification with one-carbon two-purpose can be smoothly realized, meanwhile, reduction and stabilization of the excess sludge are realized, so that the total amount of the excess sludge finally discharged by the system is reduced.
Fourthly, the method utilizes a novel technical means of recycling a small amount of flocculation precipitation sludge, realizes a plurality of auxiliary functions of good sedimentation performance of activated sludge, higher sludge concentration, improvement of residual sludge dewatering performance and the like. The inclined tube sedimentation tank 5 for advanced treatment can not discharge precipitated sludge but can recycle the precipitated sludge to the anoxic zone 2, and the system only discharges residual sludge from the secondary sedimentation tank 4, so that the advantages are as follows: the dewatering performance of the inclined tube precipitated sludge as part of residual sludge can be improved, the settling performance of the activated sludge of the whole biochemical pool can be improved, the final residual sludge is easy to dewater, the total amount of the activated sludge of the whole biochemical pool is increased (the concentration is increased) due to easy settling, the denitrification and dephosphorization reaction is more thorough, and the final effluent quality is better.
The invention realizes the purpose of the invention more satisfactorily through the technical creativity, advancement and practicability of the four aspects and the cooperation of various guarantee means, and the working process and the principle are not complex, even are very concise and clear.
The working process and principle of the UMIF integrated pool of the invention are as follows:
the sewage enters the factory firstly passes through the conventional pretreatment procedures of a grille → a water pump lifting → a fine grille → a grit chamber and the like, then enters an up-flow type composite ABR area 1 at the starting end of the UMIF integrated tank together with the external reflux activated sludge RAS of a V-shaped secondary sedimentation tank 4 in the UMIF integrated tank through a muddy water inlet pipe 15, the activated sludge mixed liquor passes through a first chamber 11, a second chamber 12, a third chamber 13 and a fourth chamber 14 of the ABR area in sequence under higher anaerobic sludge concentration, on-line hydrolytic acidification fermentation is carried out on the way to generate rbcOD or VFAs, meanwhile, phosphorus bacteria fully release phosphorus under deep anaerobic environment (the foundation is laid for fully absorbing phosphorus under subsequent and oxygen-enriched environment to facilitate the subsequent biochemical reaction to smoothly realize the biological phosphorus removal function), then the mixed liquor enters an anoxic area 2 from a water collecting channel 22 at the tail end of the ABR area, the concentration of the rbcOD or the VFAs in the mixed liquor is obviously increased compared with that in the inlet water, in the anoxic zone 2, phosphorus bacteriaDenitrifying bacteria carry out excess phosphorus accumulation and denitrification reaction by using rbCOD or VFAs in the mixed liquor as a carbon source in an anoxic environment, and a substrate nitrifying liquid of the denitrification reaction comes from a nitrifying liquid internal reflux pump at the tail end of a subsequent aeration aerobic zone 3. After denitrification and denitrification are carried out in the anoxic zone 2, the mixed liquor enters the aeration aerobic zone 3 in a plug flow mode to carry out aerobic biochemical reaction, and organic pollutant degradation (decarbonization), ammoxidation and nitrification and further biological phosphorus and phosphorus absorption are completed under the action of activated sludge microorganisms. Nitrifying liquid of a nitrifying reaction product flows back to the starting end of the anoxic zone 2 under the pumping action of a nitrifying liquid internal reflux pump at the tail end of the aerobic zone 3, then the denitrification reaction is carried out while the flow is pushed in the anoxic zone 2, and finally nitrogen (N) is generated2) And the sewage overflows to the atmosphere, and the circulation is repeated, so that the aims of full denitrification, organic pollutant degradation and biological phosphorus removal of the sewage are fulfilled.
Then, one part of the sludge-water mixed solution enters a V-shaped secondary sedimentation tank 4 for sludge-water separation under the action of gravity, and the formed supernatant liquid overflows into an inclined tube sedimentation tank 5 for advanced treatment; the suspended concentrated sludge in the middle layer of the secondary sedimentation tank continuously flows back to the starting end of the anoxic zone 2 in real time by the gas stripping reflux device 7; the concentrated sludge at the bottom layer of the secondary sedimentation tank is sent back to the beginning end of the composite ABR zone 1 through an external reflux sludge pump 6, a small part of the concentrated sludge is conveyed to a sludge dehydration treatment system in the form of excess sludge through an excess sludge pump, the purpose of removing the biological phosphorus and phosphorus-rich sludge from the system is realized, and the treated sludge cake is transported to the outside for disposal.
The effluent of the secondary sedimentation tank 4 contains more biological fragments, COD, SS, colloidal state, fine particle state and dissolved TP, and is difficult to stably reach the first-level standard A of the highest standard in national standard of pollutant discharge Standard of municipal Sewage treatment plant (GB18918-2002), so that further advanced treatment such as coagulating sedimentation and even filtration is required. At this time, the effluent entering the secondary sedimentation tank of the inclined tube sedimentation tank 5 still needs to be added with auxiliary chemical phosphorus removal and flocculation sedimentation agents (such as PAC) according to the running condition of water quality, and further residual pollutants are removed to obtain high-quality effluent. The inclined tube sedimentation tank 5 in the UMIF integrated tank does not discharge precipitated sludge, the sludge is completely recycled to the starting end of the anoxic zone 2 through a recycled sludge pump 10, and the system only discharges residual sludge from the secondary sedimentation tank 4; the recycling of the inclined tube precipitated sludge can improve the sedimentation performance of the activated sludge, improve the dehydration performance of the final excess sludge and improve the total amount of the activated sludge of a biochemical system.
Compared with other similar process technologies such as internal carbon source development and denitrification dephosphorization denitrification, the advanced technology of the UMIF integrated tank has the advantages of higher denitrification and dephosphorization efficiency, wider adaptability of water quality and water quantity, more stable effluent reaching standards, lower power consumption and drug consumption, more economical engineering cost, less occupied land, more excellent operation cost, less sludge discharge and easier operation management, so the UMIF integrated tank is particularly suitable for 12 ten thousand meters3And the sewage with low C/N ratio below the/d scale is subjected to low-cost nitrogen and phosphorus removal.
The UMIF integrated pool has the technical originality, the technical reliability and the obvious technical advantages, and is embodied in the following three aspects:
one is the technical originality is realized in the following 4 dimensions:
1 from static state to dynamic state, from single to composite technical originality, since the concept of 'hydrolysis acidification' is firstly proposed in China and corresponding process technology is invented in the 80 th century, the hydrolysis acidification technology is always relatively 'static' (the latest national environmental protection standard of 2 parts of China, namely 'upflow anaerobic sludge bed reactor sewage treatment engineering technical specification' (HJ 2013-2012) and 'hydrolysis acidification reactor sewage treatment engineering technical specification' (HJ 2047-2015)) namely that anaerobic activated sludge is always in a relatively static state in the lower layer of a water pool and only performs hydrolysis acidification on sewage or sludge alone, while the invention performs 'dynamic' or 'turbulent state' hydrolysis acidification on sewage and external reflux activated sludge at normal temperature and relatively high upward flow rate simultaneously, anaerobic sludge with different densities and different grain diameters is fully distributed in the whole water pool (the upper layer of the prior art is almost clear water and does not contain activated sludge), and the most simple and energy-saving upflow type composite ABR pool type is adopted to carry out on-line hydrolysis acidification fermentation on the main stream mixed liquid, which belongs to the domestic original creation;
2, relatively high hydraulic load is also the embodiment of technical originality, the prior art is lower hydraulic load to avoid the anaerobic sludge from being flushed and lost, and the invention does not need to worry about the anaerobic sludge loss because the sludge can continuously flow back continuously and can reach self balance under a certain range of load. The aim of adopting relatively high hydraulic load is to avoid acid production aggregation and methanation reaction to consume a part of rbCOD or VFAs by the water power elutriation principle, so that the aim of automatically elutriating the rbCOD or VFAs generated by hydrolytic acidification to be used for subsequent reaction under the action of water power is fulfilled, meanwhile, the aim of improving the productivity or reducing the volume of a water tank is fulfilled, the sludge or silt deposition and the decomposition or blockage are avoided, a stirrer is not required to be used for preventing the sludge or silt deposition and the decomposition or blockage under low load, the aims of simplifying equipment, simplifying operation management, saving energy and operating and reducing the sewage treatment cost are fulfilled, and multiple purposes are achieved;
3 is an excellent 'self-concentration' technical originality of an upflow type hydraulics flow state, particularly, the effective water distribution of the bottom layer and the balanced and dense water collection of the water surface layer are realized, the effective volume rate is greatly improved, the total amount or the concentration of the sludge in the reaction tank is obviously increased, the excellent characteristics of the upflow type anaerobic water distributor are exerted, the large V-shaped structure of the three inclined surfaces is skillfully utilized, the rising flow velocity at different elevation cross sections is different, the hydraulic screening and grading are realized, the hydrolytic acidification anaerobic sludge can be effectively intercepted, the conventional anaerobic activated sludge is brought out by the water flow, the brought-out anaerobic activated sludge passes through the subsequent large circulation reciprocating process of the anoxic zone 2 → the aerobic zone 3 → the secondary sedimentation tank 4 and the external reflux sludge pump 6 → the composite ABR zone 1, and the composite ABR zone 1 can contain sufficient anaerobic hydrolytic acidification sludge and conventional anaerobic activated sludge, the self-concentration and external reflux sludge are continuously supplemented to the composite ABR zone 1, so that the sludge concentration can be maintained to be high enough, and the two anaerobic reaction effects can be ensured to reach satisfactory degrees.
4, combining the anaerobic composite ABR zone 1, the anoxic zone 2, the aerobic zone 3, the V-shaped secondary sedimentation tank 4 and the inclined tube sedimentation tank 5 into one in sequence to form the unique ABR/AO biochemical and biochemical two-stage sedimentationThe lake integrated pool belongs to the domestic initiative and even the international initiative, is an unprecedented innovation, and is compared with the conventional A2O (Anaerobic Anaerobic-Anoxic Anaxic-aerobic Oxic abbreviation AAO, also called A)2O) or modified form A2The processes of O, UCT, AOA and the like are obviously different, the invention dramatically highlights the deep integration of three new functions of main-stream mixed liquid on-line fermentation (internal carbon source development and utilization), denitrification dephosphorization and inclined-tube precipitated sludge full-recycling, and the obvious characteristics of the invention are obviously different from the traditional A2O or other modifications A2O, the invention simplifies and names the integral structural form of ABR/AO + two-stage sedimentation + inclined tube sedimentation sludge into a UMIF integral pool (refer to the name of the invention), so that the hydrolysis acidification and anaerobic composite ABR reactor (pool) technology is completely integrated with the AO technology, the two-stage sedimentation technology and the second-stage sedimentation sludge full-recycling technology, thereby becoming A2The upgrading and upgrading of O integration, namely the anaerobic compound ABR reaction technology becomes A2The high-grade component of the O process and the integration of the two-stage sedimentation and the full recycling of the inclined tube sedimentation sludge show the sewage treatment A2The major technological progress of the O process, which is needed by the situation, is the activated sludge process A2The O process technology has evolved to today's beauty sublimation.
At present, the UMIF integrated tank technology of the invention is successfully applied to sewage treatment projects of 2 cities or test areas in China, and other projects of sewage (including industrial park sewage treatment plants) of a plurality of cities and towns are applied and implemented.
Secondly, the technical reliability is realized in the following 3 points:
the adopted upflow principle and technical parameters are very reliable, and the upflow principle and the technical parameters are proved by anaerobic sewage treatment practices for many years and are listed in the two national standards, so that the technical reliability is sufficient;
2, the pool-type structure form and the internal equipment of the composite ABR zone 1 are very reliable, because the upflow type small-resistance anti-clogging anaerobic water distributor 17, the guide plate 20, the guide slope 21, the silt discharging pipe 23, the water collecting tank 18 and the vertical baffling partition wall 19 which are positioned at the bottom layer are made of corrosion-resistant materials, have simple and firm structure, are not provided with a driving motor and are not precise devices, and the reliability is undoubted as long as the control is carried out according to the national current quality standard;
and 3, the composite ABR area 1 in the UMIF integrated pool is very reliable in design, construction, installation and operation, has no secret and difficult details and no obscure and understandable concept, and has clear and clear construction drawing and technical reliability on plain paper. In a word, the multiple new technologies adopted by the invention only need to control the civil engineering quality and the installation engineering quality, comply with the operation regulations, are stable and reliable in operation and can be used for a long time.
Thirdly, the obvious technical advantages are embodied in the following 3 points:
1, the composite ABR area 1 adopted by the invention has good anaerobic sludge interception capability, when interception reaches saturation, redundant sludge can automatically overflow from a water collecting tank 18 at the water surface to the next cell until the tail end water collecting channel 22 of the last cell, and then enters a subsequent biochemical and physicochemical treatment and sludge backflow system to return to the composite ABR area 1, so that the problem of sludge loss is avoided;
2, in the processes of hydrolytic acidification and anaerobic reaction, mechanical stirring or air stirring is not needed to be arranged at the lower layer, and a filler is not needed to be arranged at the upper layer in a water tank; the whole pool is simple in structure, few in internal equipment, easy to build and install, simple to operate and maintain, and capable of being conveniently integrated into the whole UMIF integrated pool and the whole plant process flow, thereby being beneficial to low cost of sewage treatment engineering construction and low cost nitrogen and phosphorus removal in daily operation;
3, the technical advantages of the method can be conveniently converted into economic advantages, and the method is characterized by obvious energy-saving effect, low construction cost, less construction land, low operation cost and wide application range.
Compared with the prior related (independent dispersion, semi-integration, full integration and the like) tank types, the UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquor online fermentation has the most obvious beneficial effects of the following five points:
1. the additional carbon source is saved: by adopting the UMIF integrated tank, COD contained in sewage with low C/N ratio can be fully absorbed, stored and converted into an internal carbon source by microorganisms, the absorption, storage and conversion rate is higher than 87%, organic matters which are carried by the sewage and are not easy to rapidly degrade are maximally explored and used as a final carbon source, the carbon source discharged in the form of excess sludge is reduced, and the most obvious beneficial effect is that the external carbon source is saved, and if the UMIF integrated tank is counted by a commercially available sodium acetate trihydrate solid commodity, the external carbon source is directly saved by 60mg/L or more.
2. The dephosphorization and denitrification efficiency is improved: in the UMIF integrated tank, the designed hydraulic retention time HRT of the anoxic zone 2 is more than or equal to 3.9h, the sludge concentration (MLSS) reaches 4.5-5.5 g/L, and both the HRT and the MLSS are obviously higher than the design parameters of the biological nitrogen and phosphorus removal process anoxic tank in the table 6.6.20 of the outdoor drainage design Specification GB50014-2006(2016 edition), which is the current national standard, of 0.5-3 h and the MLSS is 2.5-4.5 g/L, obviously, the invention creatively enlarges the volume of the anoxic zone 2, simultaneously improves the sludge concentration of the system, obviously increases the number of microorganisms forming the anoxic zone 2 by the product of the volume and the MLSS number, has the most obvious beneficial effects of improving the nitrogen removal efficiency of anoxic denitrification and denitrification, and improves the TN nitrogen removal rate of low-carbon source sewage by 18 percent or more as proved by practice, the TP removal rate is directly up to 90% or more, while in general A2The biological phosphorus removal efficiency of the O method is 50-75% (see the table 6.6.20 of the above national standard).
3. The effluent stably reaches the national first-grade A standard: after the low C/N ratio urban sewage is treated by the UMIF integrated tank, the engineering practice of a certain city in Hainan province shows that the effluent quality is stable and reaches COD less than or equal to 30mg/L and NH3Indexes such as-N is less than or equal to 1.5mg/L, TN is less than or equal to 13mg/L, TP is less than or equal to 0.5mg/L and the like are obviously superior to the national standard A standard, so the UMIF integrated pool has the most obvious beneficial effects of high effluent quality and stable effluent quality.
4. And finally, obviously reducing the residual sludge: after the urban sewage with the low C/N ratio is treated by the UMIF synchronous nitrogen and phosphorus removal integrated tank, the engineering practice of the embodiment I shows that the system still stably runs up to the standard after the system hardly discharges the excess sludge in the first 3 months, the effect of online fermentation of the activated sludge mixed liquor of the integrated tank is remarkable, the excellent performance (increment of obtaining the rbcOD or VFAs of 18-58 mg/L) is obtained in the aspect of internal carbon source development and utilization, the final excess sludge production amount (partial sludge is digested by the online fermentation of the main flow) is reduced, the cost of sludge treatment is saved, and the economic benefit of a sewage treatment plant is finally improved.
5. Stable and reliable, energy-saving operation, and remarkable technical and economic benefits: the composite ABR zone 1 in the UMIF integrated pool has simple interior, convenient operation and use, and can really realize no fault, no blockage, no siltation and no maintenance, because no mechanical movable operation part and no transmission motor are arranged in the ABR zone, control valves for water inlet, mud inlet and mud discharge are all positioned outside the pool, and no filler is arranged in the pool, so that no filler is hardened and replaced, and the system is extremely stable and reliable and can be used for a long time as the civil engineering and the installation engineering quality meet the national general quality standard requirements and the sediment at the bottom of the pool is regularly removed during operation. Meanwhile, the UMIF integrated pool of the invention is also very energy-saving: the water head loss between the cells of the composite ABR area 1 is small, the total water head loss of inlet and outlet water of the composite ABR area 1 is only about 0.35-0.6 m, if the plug flow stirring energy consumption of the existing anaerobic tank technology is considered, the actual energy consumption is far beyond the energy consumption of the invention, and the invention can be smoothly connected with the water outlet of the grit chamber of the front-end pretreatment working section, does not need to be pressurized and lifted by a water pump for the second time, does not need to build a pretreatment facility with very high water level, and can be well adapted to the whole process flow and hydraulic elevation of a normal sewage treatment plant. In addition, the adopted composite ABR area 1 has no stirrer, no independent power consumption and low energy consumption, does not need to be heated and insulated to a certain higher temperature, and can be obtained by only well performing outer wall heat insulation and covering the pool surface in the northern cold area.
The advantages show that the UMIF synchronous nitrogen and phosphorus removal integrated tank for on-line fermentation of mixed liquor has a very simplified sewage and sludge operation flow, compared with various tank types of the prior various technologies including sewage treatment patent technology, the UMIF synchronous nitrogen and phosphorus removal integrated tank has the advantages that the efficiency of phosphorus and nitrogen removal is higher during actual operation from the perspective of engineering scale, the water quality is more guaranteed to reach the standard, the number of the water tanks is small, the equipment types are few, the occupied land is small, the investment cost is low, the medicine consumption is low, the sludge discharge is less, the energy consumption is low, the cost is low, the operation and management are simple and convenient, the summary shows that the construction cost and the operation cost are both obviously lower than those of sewage plants of other prior process technologies or tank types, and therefore, the UMIF synchronous nitrogen.
Drawings
FIG. 1 is a plan flow chart of a UMIF synchronous denitrification and dephosphorization integrated tank for on-line fermentation of mixed liquor according to the present invention;
FIG. 2 is a longitudinal cross-sectional view of the composite ABR region at the beginning of the UMIF integrated cell of the present invention;
FIG. 3 is a top plan view of the composite ABR region at the beginning of the UMIF integrated cell of the present invention;
FIG. 4 is a schematic main sectional view (cross section) of the UMIF integrated cell of the present invention.
Wherein: 1-a composite ABR zone, 2-an anoxic zone, 3-an aerobic zone, 4-a V-shaped secondary sedimentation tank, 5-an inclined tube sedimentation tank, 6-an external reflux sludge pump, 7-an air stripping reflux device, 8-a perforated sludge discharge pipe, 9-a recycled sludge tank, 10-a recycled sludge pump, 11-a first grid chamber, 12-a second grid chamber, 13-a third grid chamber, 14-a fourth grid chamber, 15-a water inlet pipe, 16-an external reflux sludge pipe, 17-an upflow type small-resistance anti-clogging anaerobic water distributor, 18-a water collecting tank, 19-a baffling partition wall, 20-a guide plate, 21-a diversion slope, 22-a water outlet channel for collecting water, and 23-a silt discharge pipe.
Detailed Description
The technical scheme of the invention is further described in detail by the following embodiments and the accompanying drawings:
example one
Referring to the attached drawings 1, 2, 3 and 4, the present invention will be further explained in detail by using the UMIF integrated tank of the present invention as an embodiment in combination with a sewage treatment project in a city of Hainan province. Thus, the present embodiment provides a practical solution that has been successfully implemented.
It is emphasized that the detailed description of the embodiments is provided to assist understanding of the spirit and intent of the present invention, and is not to be construed as limiting the invention. Moreover, in the following description, descriptions of well-known techniques and familiar structures (e.g., anoxic tanks, aeration tanks, secondary sedimentation tanks, inclined tube sedimentation tanks, etc.) have been omitted from the technical arts to avoid unnecessarily obscuring or obscuring the concepts of the present invention.
The scale of sewage treatment in this example was 4 km3D, in order to facilitate the maintenance of the pool or the equipment without stopping production, 2 groups of 4 seats are designed, each seat has 1 ten thousand meters3A/d scale series of UMIF integrated pools and auxiliary facilities. Every 1 ten thousand meters3The starting end of the/d integrated pool is provided with 2 5000m seats each3The hydrolytic acidification and anaerobic composite ABR reaction tank (area) of/d, 2 tanks are connected in parallel and are built with a common wall. Fig. 1 is a plan flow diagram of the UMIF integrated pool, fig. 2 is a longitudinal section of the composite ABR zone 1, fig. 3 is a plan view of an upper layer of the composite ABR zone 1, the length × width of the single composite ABR zone 1 is 22.85 × 5.15m, the single composite ABR zone is formed by connecting 4 cells in series, and the effective water depth is 6.30 m.
Specifically, a muddy water inlet pipe 15 to be treated, an external return sludge pipe 16 and a water surface water collecting tank 18 are arranged in the first cell 11, and an up-flow anaerobic water distributor 17 with a water distribution area of 20.23m is arranged at the bottom of the first cell 11216 water distribution nozzles, the water distribution area of a single nozzle is 1.26m2The water distribution area of a single water distribution port in charge of the water distribution system meets the technical specification of upflow anaerobic sludge bed reactor sewage treatment engineering (HJ 2013-2(flocculent sludge) and 0.5-2 m2(granular sludge). Be equipped with baffling partition wall 19 in the second check room 12, guide plate 20 and 2 water conservancy diversion slopes 21 in opposite directions, the water conservancy diversion board 20, the horizontal contained angle of 2 water conservancy diversion slopes 21 is 50, the guide plate 20 material is corrosion-resistant stainless steel or plastic sheeting, water conservancy diversion slope 21 does benefit to mud landing downwards for the smooth inclined plane of secondary pouring, bottom of the pool center is leaned on the downstream direction and still is equipped with silt and gets rid of pipe 23, the pool face is equipped with the water catch bowl 18 the same with first check room 11 quantity, but the elevation of this water catch bowl will be less than first check room water catch bowl elevation 100mm in order to ensure that the reaction tank rivers can flow into second check room 12 from first check room 11 smoothly. The third and fourth cells 13, 14 are identical to the second cell 12, but with a water collection sump 18And a tail end water collecting channel 22 is arranged in the fourth grid chamber 14, and the water flow of the grid chamber water collecting channel 18 is collected and enters the anoxic zone 2 from the side wall hole for subsequent biochemical treatment.
FIG. 4 shows a schematic main section (cross section) of the UMIF integrated cell of the present embodiment. As shown in fig. 1, fig. 2, fig. 3 and fig. 4, the composite ABR region 1 adopted by the innovative core of the UMIF-integrated pool of the present invention includes: the device comprises a first cell 11, a second cell 12, a third cell 13, a fourth cell 14, a water inlet pipe 15, an external return sludge pipe 16, an up-flow anaerobic water distributor 17, a water collecting tank 18, a baffling partition wall 19, a guide plate 20, a guide slope 21, a water collecting channel 22 and a sediment discharge pipe 23.
The main specification parameters of the composite ABR zone 1 in this example are as follows:
the net length of the first grid 11, the second grid 12, the third grid 13 and the fourth grid 14 along the main flow direction of the mixed liquid of sewage and activated sludge is 4.70m (no flow reduction chamber, partition wall and the like are contained), and the net width is 4.35m, so that an upflow space can be realized, and the biochemical reaction effects of the upflow hydrolytic acidification reaction and the anaerobic composite reaction which are as large as possible can be fully exerted; maximum hydraulic load of 24.5m of upflow chamber3/m2H, maximum upward flow velocity v thereofOn the upper part＝6.8mm/s；
The water inlet pipe 15 is positioned at the center line of the first cell 11 and enters the first cell 11 from the horizontal direction; the number of the water inlet pipes 15 is 1, and the specification is DN 500;
one end of the external return sludge pipe 16 is connected with the water inlet pipe 15, and the other end is connected with the external return sludge pump 6; the number of the external reflux sludge pipes 16 is 1, and the specification is DN 200;
the upflow anaerobic water distributor 17 is connected with the water inlet pipe 15, the upflow anaerobic water distributor 17 is horizontally arranged and supported and fixed by a buttress, all nozzles face downwards, and are in an emptying state after being fixed, and the heights of the nozzles are positioned on the same plane; the number of the upflow anaerobic water distributors 17 is 1, and the specification is DN500-16 nozzle type;
one end of the water collecting tank 18 is fixed on the bracket, the other end of the water collecting tank 18 is fixed in the through-wall hole, the water collecting tank 18 is in a triangular weir U-shaped groove, and the groove shape is favorable for flushing floating slag on the water surface from a triangular weir opening without gathering the floating slag on the water surface to influence the appearance; the number of the water collecting grooves 18 is 28 in total, 7 in each grid chamber, the specification is B multiplied by H which is 220 multiplied by 360mm, and the center distance between adjacent water collecting grooves is 0.62 m;
the two ends of the baffling partition wall 19 are respectively fixed on the pool walls of the second grid chamber 12, the third grid chamber 13 and the fourth grid chamber 14, the space height between the baffling partition wall 19 and the pool bottom plate is 1.00m, the distance between the baffling partition wall 19 and the pool walls is 60cm, the 60cm wide flow reduction type hydraulic channel space is still used for conventional anaerobic reaction, and is not only a water flow channel but also an anaerobic reaction space, and no waste is caused; the number of the baffle partition walls 19 is 3, and the included angle between the lower folded angle and the horizontal direction is 50 degrees;
one side of the flow guide plate 20 is fixed on a lower break angle of the flow guide partition wall 19, and the other side is in a suspended state and is provided with 6 tank bottom supporting points to prevent water flow from causing vibration and sludge deposition gravity pressure deformation; the angle between the deflector 20 and the horizontal direction is also 50 degrees; the guide plate 20 is made of UPVC plastic, the number of the guide plate is 3 blocks per cell, the specification is L multiplied by B is 4330 multiplied by 1000mm, the thickness is 10mm, and the distance between the guide plate 20 and the bottom of the pool is 400 mm;
the diversion slope 21 is a smooth slope surface formed by secondary pouring concrete and has the functions of eliminating hydraulic dead angles, forming a hydraulic channel, changing the direction of water flow and forming a downward sliding slope surface for sludge settlement; the included angle between the flow guiding slope 21 and the horizontal direction is also 50 degrees; the number of the flow guide slopes 21 is 6 per cell, and the height is about 1740-1900 mm;
the water collecting channel 22 at the tail end of the composite ABR zone 1 is suspended on the pool wall of the fourth grid chamber 14, the water collecting tank 18 of the fourth grid chamber 14 converges the sludge-water mixed liquid after the anaerobic reaction to enter the water collecting channel 22, and the sludge-water mixed liquid passes through the side wall water outlet hole to reach the anoxic zone 2 of the subsequent treatment unit for treatment;
the sediment discharge pipe 23 is in a perforated sediment discharge pipe form, hydrodynamic sediment discharge is carried out by means of the water pressure difference between the inside and the outside of the reactor, the position of the sediment discharge pipe is arranged in the downstream direction of the center of the bottom of each cell, and the pipe position is parallel to the direction of the flow guide plate 20, namely is vertical to the direction of the total water flow; the silt discharging pipe 23 is made of PE100 high-density polyethylene plastic water supply pipes, the number of the silt discharging pipes is 1 per grid chamber and 4, the specification is DN200, and a control valve is connected outside the pool.
The water depth difference of each cell of the composite ABR zone 1 is very small, and the hydraulic flow state is basically the same. During operation, except that the sediment deposition possibly exists slightly on the bottom of the second grid chamber 12 for a long time, the sediment deposition in the other 3 grid chambers is less, but in actual operation, a valve on a pipeline of the sediment discharge pipe 23 is opened for sand discharge and observation so as to determine how often the interval is opened. Besides, the composite ABR area 1 adopted by the innovative core of the UMIF integrated pool has extremely simple and convenient operation, can be usually in an unattended state, and only needs an attendant to regularly observe whether the water flow of each cell is abnormal or not, so that the composite ABR area 1 of the embodiment has high efficiency, high reliability, energy conservation and low operation cost.
The UMIF biochemical reaction part in the embodiment has an anoxic zone 2 and an aerobic zone 3 in addition to the upflow anaerobic composite ABR zone 1. The anaerobic ABR area 1 is communicated with the anoxic area 2 through a side wall hole of a water outlet collecting channel 22 at the tail end of the ABR area 1; the anoxic zone 2 is communicated with the aerobic zone 3 through a partition wall hole between the tail end of the anoxic zone 2 and the aerobic zone 3.
In this embodiment, the UMIF integrated tank further includes a V-shaped secondary sedimentation tank 4, an inclined tube sedimentation tank 5, and pipelines and auxiliary facilities connected to the system, including at least an external reflux sludge pump 6, a reuse sludge tank 9, a reuse sludge pump 10, an external reflux sludge pipe 16, and the like. The tail end of the aerobic zone 3 is communicated with a partition wall hole below a V-shaped partition wall of the secondary sedimentation tank 4 between the aerobic zone 3 and the secondary sedimentation tank 4; and supernatant is collected through a water surface water collecting tank of the secondary sedimentation tank 4 and collected to a water collecting channel at the top of a partition wall between the secondary sedimentation tank 4 and the inclined tube sedimentation tank 5, and then the secondary sedimentation tank 4 and the inclined tube sedimentation tank are communicated through an L-shaped hydraulic coagulation spinner. And finally, the upper layer clear water is completely collected and conveyed to a water outlet of a main water collecting channel at the tail end of the rectangular water tank by a water surface water collecting tank of the inclined tube sedimentation tank 5, and is conveyed to a subsequent filter tank by a pipeline for filtering treatment, or is directly conveyed to a contact disinfection tank in a factory for disinfection and sterilization and then is discharged out of the factory.
The main process technical parameters of the UMIF integrated cell of the present embodiment are as follows:
HRT of the composite ABR zone 1 is 2.36h, HRT of the anoxic zone 2 is 3.93h, HRT of the aerated aerobic zone 3 is 6.59h, and the total HRT of the UMIF biochemical reaction tank is 12.88 h. The design scale of the single anoxic zone 2 and the aerobic zone 3 is 1 ten thousand meters3D, the effective water depth is 6m, the MLSS concentration of the activated sludge is 4.5-5.5 g/L, the aerobic zone 3 adopts accurate aeration to control the operation of lower dissolved oxygen, and the mixed liquid of the UMIF biochemical reaction tank is of a plug flow type (the sludge bulking can be effectively avoided);
the design scale of the single-seat V-shaped secondary sedimentation tank 4 and the inclined tube sedimentation tank 5 is 1 ten thousand meters3D, the water surface height difference between the two is 1.00m, and the water surface height difference potential energy provides coagulation reaction power for the inclined tube sedimentation tank 5, so that the auxiliary chemical phosphorus removal agent and the advanced treatment coagulant (such as PAC) can obtain a satisfactory mixed flocculation effect; the water surface L multiplied by B of the secondary sedimentation tank 4 is 19.80m multiplied by 10.0m, and the designed surface load is 2.14m3/(m2H), the effective water depth is 4.99m (the depth of a sludge discharge hopper is not included), the secondary sedimentation tank is not provided with a sludge scraping and sucking machine, the bottom layer concentrated sludge is discharged through a large-opening sludge discharge pipe at the bottom of the hopper and an electric valve, 3 sets of horizontal surface type micro-power gas stripping reflux devices 7 are arranged, the gas stripping reflux is carried out on the middle layer suspended activated sludge separated from the sludge and the water, and the gas stripping reflux ratio is 50-100%; the water surface L multiplied by B of the inclined tube sedimentation tank 5 is 18.36m multiplied by 14.10m, and the designed surface load is 1.61m3/(m2H), the effective water depth is 4.39m (without the depth of a sludge discharge hopper), the inclined tube sedimentation tank 5 is not provided with a sludge scraping and sucking machine, the bottom layer precipitated sludge is discharged through a hopper bottom perforation sludge discharge pipe and an electric valve sludge discharge, after the sludge is fed into the recycled sludge tank, all the sludge is conveyed to the starting end of the anoxic zone 2 through a recycled sludge pipeline and is used as a condensation nucleus of activated sludge MLSS for forming granular sludge in a system, and the sedimentation performance of the activated sludge is greatly improved;
the rest parts of the UMIF integrated tank in the embodiment are all designed conventionally, the external reflux ratio of sludge of a biochemical reaction system is 100%, the internal reflux ratio of nitrifying liquid is 250%, the inclined tube precipitated sludge is completely recycled to the starting end of the anoxic tank, and the final residual sludge of the system is only discharged from the secondary sedimentation tank.
TABLE 1 actual influent and effluent quality of a wastewater treatment plant of example one
Item COD BOD5 SS NH3-N TN TP
Quality of inlet water (mg/L) 178 55 115 42.6 47.2 6.75
Effluent water quality (mg/L) ≤20 ≤5 ≤4 ≤1.0 ≤13 ≤0.5
Treatment efficiency (%) ≥88.8 ≥90.9 ≥96.5 ≥97.7 ≥72.5 ≥92.6
(Note: COD-chemical oxygen demand, BOD)5-5 daily biochemical oxygen demand, SS-suspended solids, NH3-N-ammonia nitrogen, TN-total nitrogen, TP-total phosphorus. )
The actual measurement result after the operation is stable shows that: extremely low C/N ratio of influent water, BOD5The nitrogen removal theoretical value/TN is only 1.17 (the nitrogen removal theoretical value is 2.86, the actual value is required to reach 4), the COD/TN is only 3.77, the carbon source is extremely lack of water quality, the theoretical adding amount of sodium acetate is calculated according to the existing 2-3 methods, the calculation result is 160-440 mg/L of commercial solid sodium acetate trihydrate, and the effluent can stably reach the standard under the condition that only 60-90 mg/L of sodium acetate is actually added during the debugging operation. Therefore, the UMIF integrated tank provided by the invention is used for carrying out nitrogen and phosphorus removal treatment on the low-carbon source urban sewage, and the effect of developing and utilizing the carbon source is satisfactory. Through measurement and calculation, at least 28.9mg/L of rbcOD or VFAs generated by hydrolytic acidification fermentation in the embodiment are used as direct carbon sources, important contribution is made to synchronous nitrogen and phosphorus removal, namely commercial solid sodium acetate with 72mg/L of external carbon sources is saved, particularly, the biological phosphorus removal efficiency is quite unexpected and is obviously higher than the highest value (75 percent) of national standard, please refer to a table 6.6.20 of 'outdoor drainage design standard' GB50014-2006(2016 edition), and all indexes of effluent stably reach the national first-class A standard.
The wastewater treatment plant of this example treated every m3The direct cost of the sewage, such as power consumption (including sewage entering a factory for lifting), medicine consumption, manpower, overhaul and expense, is 0.56 yuan, and the construction investment, the occupied land, the operation cost and the like of the sewage and other activated sludge are combinedCompared with the nitrogen and phosphorus removal process, the nitrogen and phosphorus removal process can be saved by about 25-30 percent, so the technical and economic benefits of the invention are very obvious. The UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation obtains good sewage treatment effect and technical economic effect.
Example two
Referring to the attached drawings 1, 2, 3 and 4, the invention will be further explained in detail by using the UMIF synchronous denitrification and dephosphorization integrated tank for mixed liquor online fermentation as an embodiment in combination with a sewage treatment project of a test area in Hainan province. Therefore, the embodiment provides a practical and feasible technical scheme which is successfully applied.
The scale of sewage treatment in this example was 8000m3D, in order to facilitate the maintenance of the water pool or equipment without stopping production, the design is divided into 2 seats each of 4000m3UMIF integrated pool and accessory facilities of/d. Fig. 1 is a plan view of the UMIF integrated pool, fig. 2 is a longitudinal sectional view of the composite ABR zone 1 but 3 cells for 1 cell in this example, fig. 3 is a plan view of the upper layer of the composite ABR zone 1 but 3 cells for 1 cell in this example, and the single-seat composite ABR zone 1 has a length × width of 15.00 × 4.58m, and is formed by connecting 3 cells in series, and has an effective water depth of 6.00 m.
Specifically, a sewage inlet pipe 15 to be treated, an external return sludge pipe 16 and a water surface water collecting tank 18 are arranged in the first cell 11, and an up-flow anaerobic water distributor 17 with a water distribution area of 17.44m is arranged at the bottom of the first cell 11216 water distribution nozzles, the water distribution area of a single nozzle is 1.09m2The water distribution area of a single water distribution port in charge of the water distribution system meets the technical specification of upflow anaerobic sludge bed reactor sewage treatment engineering (HJ 2013-2(flocculent sludge) and 0.5-2 m2(granular sludge). A baffling partition wall 19, a guide plate 20 and 2 opposite guide slopes 21 are arranged in the second grid chamber 12, the horizontal included angles of the guide plate 20 and the guide slopes 21 are both 50 degrees, the guide plate 20 is made of corrosion-resistant stainless steel or plastic plate, the guide slopes 21 are smooth slopes poured for the second time, sludge slides downwards, a sediment discharge pipe 23 is further arranged in the center of the bottom of the pool close to the downstream direction, and the surface of the pool is provided with a sand discharge pipe 23 corresponding to the downstream directionThe same number of water collection troughs 18 are provided in the first cells 11, but the height of the water collection troughs is 100mm lower than that of the water collection troughs in the first cells to ensure that the reaction tank water flow can smoothly flow from the first cells 11 to the second cells 12. The third cell 13 is the same as the second cell 12, but the elevation of the water collecting tank 18 is decreased in sequence, and a terminal water collecting channel 22 is arranged in the third cell 13, and the water flow of the cell water collecting tank 18 is collected and then conveyed to the subsequent anoxic zone 2 from the side wall hole for biochemical treatment.
Fig. 4 shows a schematic main section (cross section) of the UMIF-integrated cell of the present embodiment, but the number of the cells of the composite ABR region 1 is 1 less, 3 cells are provided, and there are only 1 row. Referring to fig. 1, 2, 3 and 4, a composite ABR zone 1 of the UMIF-integrated cell of the present invention includes: the device comprises a first cell 11, a second cell 12, a third cell 13, a water inlet pipe 15, an external return sludge pipe 16, an up-flow anaerobic water distributor 17, a water collecting tank 18, a baffling partition wall 19, a flow guide plate 20, a flow guide slope 21, a water collecting channel 22 and a sediment discharge pipe 23.
The main specification parameters of the composite ABR zone 1 in this example are as follows:
the net length of the first cell 11, the second cell 12 and the third cell 13 along the main flow direction of the mixed liquid of sewage and activated sludge is respectively 4.50m, 4.00m and 4.00m (no flow reduction chamber, partition wall and the like are contained), and the net width is 3.875m, so that the upflow space is as large as possible, and the biochemical reaction effects of the upflow hydrolytic acidification reaction and the anaerobic composite reaction are fully exerted; the highest hydraulic load of the upflow chamber is 22.94-25.81 m3/m2H, maximum upward flow velocity v thereofOn the upper part＝7.17mm/s；
The water inlet pipe 15 is positioned at the center line of the first cell 11 and enters the first cell 11 from the horizontal direction; the number of the water inlet pipes 15 is 1, and the specification is DN 450;
one end of the external return sludge pipe 16 is connected with the water inlet pipe 15, and the other end is connected with the external return sludge pump 6; the number of the external reflux sludge pipes 16 is 1, and the specification is DN 200;
the upflow anaerobic water distributor 17 is connected with the water inlet pipe 15, the upflow anaerobic water distributor 17 is horizontally arranged and supported and fixed by a buttress, all nozzles face downwards, and are in an emptying state after being fixed, and the heights of the nozzles are positioned on the same plane; the number of the upflow anaerobic water distributors 17 is 1, and the specification is DN450-16 nozzle type;
one end of the water collecting tank 18 is fixed on the bracket, the other end of the water collecting tank 18 is fixed in the through-wall hole, the water collecting tank 18 is in a triangular weir U-shaped groove, and the groove shape is favorable for flushing floating slag on the water surface from a triangular weir opening without gathering the floating slag on the water surface to influence the appearance; the number of the water collecting grooves 18 is 21 in total, 7 water collecting grooves are arranged in each grid chamber, the specification is B multiplied by H is 190 multiplied by 330mm, and the center distance between every two adjacent water collecting grooves is 0.55 m;
the two ends of the baffling partition wall 19 are respectively fixed on the pool walls of the second grid chamber 12 and the third grid chamber 13, the height of the baffling partition wall 19 and the bottom plate of the pool is 1.00m, the distance between the baffling partition wall 19 and the pool walls is 50cm, and the 50 cm-wide downflow type hydraulic channel space is still used for conventional anaerobic reaction, is not only a water flow channel, but also an anaerobic reaction space, and does not form any waste; the number of the baffle partition walls 19 is 2, and the included angle between the lower folded angle and the horizontal direction is 50 degrees;
one side of the flow guide plate 20 is fixed on a lower break angle of the flow guide partition wall 19, and the other side is in a suspended state and is provided with 5 tank bottom supporting points to prevent water flow from causing vibration and sludge deposition gravity pressure deformation; the angle between the deflector 20 and the horizontal direction is also 50 degrees; the guide plate 20 is made of UPVC plastic, the number of the guide plate is 2 blocks per cell, the specification is L multiplied by B (3860 multiplied by 1100 mm), the thickness is 10mm, and the distance between the guide plate 20 and the bottom of the pool is 350 mm;
the diversion slope 21 is a smooth slope surface formed by secondary pouring concrete and has the functions of eliminating hydraulic dead angles, forming a hydraulic channel, changing the direction of water flow and forming a downward sliding slope surface for sludge settlement; the included angle between the flow guiding slope 21 and the horizontal direction is also 50 degrees; the number of the flow guide slopes 21 is 4 per cell, and the height is about 1700-1900 mm;
the water collecting channel 22 at the tail end of the composite ABR zone 1 is suspended on the pool wall of the third grid chamber 13, the water collecting tank 18 of the third grid chamber 13 converges the sludge-water mixed liquid after the anaerobic reaction to enter the water collecting channel 22, and the sludge-water mixed liquid passes through the side wall water outlet hole to reach the anoxic zone 2 of the subsequent treatment unit for treatment;
the sediment discharge pipe 23 is in a perforated sediment discharge pipe form, hydrodynamic sediment discharge is carried out by means of the water pressure difference between the inside and the outside of the reactor, the position of the sediment discharge pipe is arranged in the downstream direction of the center of the bottom of each cell, and the pipe position is parallel to the direction of the flow guide plate 20, namely is vertical to the direction of the total water flow; the silt discharging pipe 23 is made of PE100 high-density polyethylene plastic water supply pipes, the number of the silt discharging pipes is 3, the number of the silt discharging pipes is 1 in each grid chamber, the specification is DN200, and a control valve is connected outside the pool.
The water depth difference of each cell of the composite ABR zone 1 is very small, and the hydraulic flow state is basically the same. During operation, except that the sediment deposition possibly exists slightly on the bottom of the second grid chamber 12 for a long time, the sediment deposition in the other 2 grid chambers is less, but in actual operation, a valve on a pipeline of the sediment discharge pipe 23 is opened for sand discharge and observation so as to determine how often the interval is opened. Besides, the composite ABR area 1 adopted by the innovative core of the UMIF integrated pool has extremely simple and convenient operation, can be usually in an unattended state, and only needs an attendant to regularly observe whether the water flow of each cell is abnormal or not, so that the composite ABR area 1 adopted by the invention has high efficiency, high reliability, energy conservation and lowest operation cost.
The main process technical parameters of the UMIF integrated cell of the present embodiment are as follows:
HRT of the composite ABR zone 1 is 1.8h, HRT of the anoxic zone 2 is 4.38h, HRT of the aerated aerobic zone 3 is 7.17h, and the total HRT of the UMIF biochemical reaction tank is 13.35 h. The design scale of the single anoxic zone 2 and the single aerobic zone 3 is 4000m3D, the effective water depth is 5.70m, the MLSS concentration of the activated sludge is 4.5-5.5 g/L, the aerobic zone 3 adopts accurate aeration to control the operation of lower dissolved oxygen, and the mixed liquid of the UMIF biochemical reaction tank is of a plug flow type (the sludge bulking can be effectively avoided);
the design scale of the single-seat V-shaped secondary sedimentation tank 4 and the inclined tube sedimentation tank 5 is 4000m3The water surface height difference between the two is 0.90m, and the water surface height difference potential energy provides coagulation reaction power for the inclined tube sedimentation tank 5, so that the auxiliary chemical phosphorus removal agent and the advanced treatment coagulant (such as PAC) can obtain a satisfactory mixed flocculation effect; two sinksThe water level L × B of the pool 4 is 12.25m × 7.35m, and the design surface load is 1.851m3/(m2H), the effective water depth is 4.10m (the depth of a sludge discharge hopper is not included), the secondary sedimentation tank is not provided with a sludge scraping and sucking machine, the bottom layer concentrated sludge is discharged through a large-opening sludge discharge pipe at the bottom of the hopper and an electric valve, 2 sets of horizontal surface type micro-power gas stripping reflux devices 7 are arranged, the gas stripping reflux ratio of the suspended activated sludge in the middle layer of the sludge-water separation is 50-100 percent; the water surface L multiplied by B of the inclined tube sedimentation tank 5 is 12.25m multiplied by 11.65m, and the designed surface load is 1.168m3/(m2H), the effective water depth is 3.60m (without the depth of a sludge discharge hopper), the inclined tube sedimentation tank 5 is not provided with a sludge scraping and sucking machine, the bottom layer precipitated sludge is discharged through a hopper bottom perforation sludge discharge pipe (8) and an electric valve, and after the sludge is discharged into a reuse sludge tank (9), the sludge is completely conveyed to the starting end of the anoxic zone 2 through a reuse sludge pipeline by a reuse sludge pump (10) and is used as a condensation nucleus of activated sludge MLSS for forming granular sludge for the system, and the sedimentation performance of the activated sludge is greatly improved;
the rest parts of the UMIF integrated tank in the embodiment are all designed conventionally, the external reflux ratio of sludge of a biochemical reaction system is 66%, the internal reflux ratio of nitrifying liquid is 216%, the inclined tube precipitated sludge is completely recycled to the starting end of the anoxic tank, and the final residual sludge of the system is only discharged from the secondary sedimentation tank.
TABLE 2 actual influent and effluent quality of the Sewage treatment plant of example two
Item COD BOD5 SS NH3-N TN TP
Quality of inlet water (mg/L) 163 50 96 38.9 44.8 5.99
Effluent water quality (mg/L) ≤20 ≤5 ≤4 ≤0.5 ≤11 ≤0.4
Treatment efficiency (%) ≥87.7 ≥90 ≥95.8 ≥98.7 ≥75.4 ≥93.3
The actual measurement result after the operation is stable shows that: extremely low C/N ratio of influent water, BOD5the/TN is only 1.12 (the denitrification theoretical value is 2.86, the actual value is required to reach 4), the COD/TN is only 3.64, the carbon source extremely lacks water quality, the theoretical adding amount of the sodium acetate is calculated according to the existing 2-3 methods, the calculation result is 170-450 mg/L commercial solid sodium acetate trihydrate, and the actual debugging and running period is adjustedThe effluent can stably reach the standard only by adding 70-100 mg/L of the water. Therefore, the UMIF integrated tank provided by the invention is used for carrying out nitrogen and phosphorus removal treatment on the sewage in the low-carbon source test area, and the effect of developing and utilizing the carbon source is satisfactory. Through measurement and calculation, at least 24mg/L of rbcOD or VFAs generated by hydrolytic acidification fermentation in the embodiment are used as direct carbon sources, important contribution is made to synchronous nitrogen and phosphorus removal, namely commercial solid sodium acetate with 60mg/L of external carbon sources is saved, particularly, the biological phosphorus removal efficiency is quite unexpected and obviously higher than the highest value (75%) of national standard, and various indexes of effluent stably reach the national first-class A standard.
As described above, the present invention can be preferably implemented by skillful conception, overall calculation, and detailed design.
From the two embodiments, the UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation can treat urban domestic sewage with low C/N ratio and biochemical production and living mixed wastewater in various parks, only an inclined tube sedimentation tank is arranged behind a secondary sedimentation tank, and a small amount of medicament (such as PAC and the like, which can ensure stable effluent quality) is added according to the effluent quality condition to directly reach the national first-level A standard without additionally arranging a complex treatment structure. Therefore, compared with other sewage treatment integrated tanks, the invention has the advantages of simple process, land saving, low construction cost and low operation cost.
In conclusion, the UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation has the advantages of ingenious, novel, unique, simple, quick and firm conception and strong engineering implementation, and can synchronously perform hydrolytic acidification fermentation and conventional anaerobic biochemical reaction, reduce the addition amount of an external carbon source even without adding the external carbon source, realize the synchronous operation of 'one carbon dual-purpose' of denitrification phosphorus removal and denitrification nitrogen removal and obviously reduce the final residual sludge production amount on the aspects of functions and performance. The excellent hydraulic characteristics of the composite ABR area 1 in the UMIF integration not only strengthen the mass transfer effect of biochemical reaction and greatly improve the reaction rate, but also have no mechanical and electrical equipment and extremely save energy in operation. In addition, the composite ABR area 1 and the whole UMIF integrated tank are simple in structure and strong in modularity, and are easy to combine with a subsequent biochemical treatment module for collaborative design, so that the universal applicability is realized, the civil engineering quantity of the whole sewage treatment project is reduced, the construction cost is obviously saved, and the wide market application prospect is realized. If the invention is widely applied to the construction of urban sewage treatment or centralized sewage treatment projects of industrial parks, a huge amount of construction funds in billions of yuan can be saved, considerable operation power consumption and carbon source consumption cost can be saved every year, and great contribution is made to global carbon emission reduction, so the invention has very remarkable macroscopic and microscopic economic benefits, environmental benefits and social benefits.
Finally, it should be noted that: the above description is only a preferred embodiment of the on-line mixed liquor fermentation UMIF simultaneous nitrogen and phosphorus removal integrated tank of the present invention, and is not intended to limit the present invention, and it will be obvious to those skilled in the art that modifications may be made to the technical solutions of the embodiments of the present invention, or equivalent substitutions may be made to some technical features, and any modifications, equivalent substitutions, improvements, and the like made should be included in the scope of the present invention.

Claims (7)

1. UMIF synchronous nitrogen and phosphorus removal integrated pool for mixed liquid on-line fermentation is characterized in that: the anaerobic/anoxic composite anaerobic/anoxic zone is communicated with the composite ABR zone through side wall holes of a water outlet collecting channel at the tail end of the composite ABR zone; the anoxic zone is communicated with the aerobic zone through a partition wall hole between the tail end of the anoxic zone and the aerobic zone; the integrated tank also comprises a V-shaped secondary sedimentation tank, an inclined tube sedimentation tank, a plurality of connecting pipelines and accessory facilities, wherein the accessory facilities comprise an external reflux sludge pump, an external reflux sludge pipe, a recycling sludge tank and a recycling sludge pump; the tail end of the aerobic zone is communicated with a partition wall hole below a V-shaped partition wall of the secondary sedimentation tank; supernatant is collected through a water collecting tank on the water surface of the secondary sedimentation tank and is collected to a water collecting channel at the top of a partition wall between the secondary sedimentation tank and the inclined tube sedimentation tank, and then the secondary sedimentation tank and the inclined tube sedimentation tank are communicated through an L-shaped hydraulic coagulation spinner; finally, the upper layer clear water is completely collected and conveyed to a water outlet of a main water collecting channel at the tail end of the water tank by a water surface water collecting tank of the inclined tube sedimentation tank, and is conveyed to a subsequent filter tank by a pipeline for filtering treatment, or is directly conveyed to a contact disinfection tank in a factory for disinfection and sterilization and then is discharged out of the factory; the bottom of the V-shaped secondary sedimentation tank is respectively communicated with the sludge discharge tank and the composite ABR zone inlet through pipelines, the tail end of the aerobic zone is connected with the initial end of the anoxic zone through an internal reflux pipeline, and the inclined tube sedimentation tank is communicated with the initial end of the anoxic zone through a sludge recycling pipeline.
2. The UMIF synchronous denitrification and dephosphorization integrated tank for mixed liquor online fermentation according to claim 1, wherein: the composite ABR area comprises a three-grid or four-grid rectangular tank body which is respectively a first grid chamber, a second grid chamber, a third grid chamber and a fourth grid chamber, wherein the first grid chamber is internally provided with a muddy water inlet pipe and an up-flow anaerobic water distributor connected with the muddy water inlet pipe; at most three down-flow channels are formed between each two adjacent cells through baffling partition walls; when the device runs, the flowing direction of the activated sludge mixed liquor is sequentially a first grid chamber → a second grid chamber → a third grid chamber (→ a fourth grid chamber), and the activated sludge mixed liquor is communicated through a down-flow channel to form main grid chambers in an up-flow type flowing direction, wherein the first grid chamber has water inlet and sludge inlet, and the last grid chamber has mixed liquor outlet; each cell is provided with an upper water collecting tank and a bottom sediment discharge pipe, and the sediment discharge pipe is arranged at the position which is lower than the downstream position of the center of the bottom and is parallel to the direction of the guide plate; except the first cell, each cell has a guide plate and two guide slopes.
3. The UMIF synchronous denitrification and dephosphorization integrated tank for mixed liquor online fermentation according to claim 1, wherein: the upflow anaerobic water distributor sprays water downwards and forms uniform upflow by the reflection of the bottom of the pool.
4. The UMIF synchronous denitrification and dephosphorization integrated tank for mixed liquor online fermentation according to claim 1, wherein: the upflow anaerobic water distributor comprises a large-caliber tee joint positioned in the middle, the central tee joint of the tee joint faces upwards and is in butt joint with a water inlet pipe, the other two horizontal outlets are respectively connected with a horizontal cross joint, the other three branch outlets of the cross joint are respectively connected with a pair of downward small-caliber tee joints and a horizontal medium-caliber tee joint, two sides of the medium-caliber tee joints are horizontally connected with two downward medium-caliber tee joints, the water outlets of each small-caliber tee joint and the medium-caliber tee joints are connected with nozzles, the nozzles spray towards the bottom of the tank, and the positions of the bottom of the tank corresponding to the nozzles are provided with diffusion cone caps.
5. The UMIF synchronous denitrification and dephosphorization integrated tank for mixed liquor online fermentation according to claim 1, wherein: a plurality of parallel water collecting grooves are formed in the water surface of each cell in the composite ABR area, ascending water flow is uniformly and densely collected, and the number of the water collecting grooves of each cell is the same.
6. The UMIF synchronous denitrification and dephosphorization integrated tank for mixed liquor online fermentation according to claim 1, wherein: the down-flow channel is formed between the baffling partition wall of the composite ABR area and the partition wall of the tank body, and the ratio of the width of the down-flow channel to the width of the up-flow grid chamber is 1: 6-9.
7. The application method of the UMIF synchronous denitrification and dephosphorization integrated tank for mixed liquor online fermentation according to any one of claims 1 to 6, comprising the following steps:
step 1, mixing external reflux activated sludge RAS from an external reflux sludge pump in a sludge discharge tank of a V-shaped secondary sedimentation tank with inlet water to form an activated sludge mixed solution, entering a first grid of an up-flow anaerobic composite ABR area through a water inlet pipe, spraying water by an up-flow anaerobic water distributor downwards, reflecting by the bottom of the tank to form uniform up-flow, collecting a plurality of parallel water collecting tanks on the water surface to enter a downlink channel of a second grid of the composite ABR area, reaching the bottom of the second grid through a channel between a baffling partition guide plate and a flow guide slope, and reflecting at the bottom of the tank to form up-flow in the second grid;
step 2, upward flow in a second grid of the composite ABR area is collected by a water collecting tank and then sequentially enters a downward channel of a third grid; the steps are repeated in sequence, and the mixed liquid enters a water collecting channel at the tail end of the composite ABR area after being collected by a water collecting channel at the tail end of the composite ABR area;
step 3, enabling mixed liquid of a water collecting channel at the tail end of the composite ABR zone to enter the starting end of an anoxic zone, enabling an internal reflux nitrifying liquid from the tail end of an aerobic zone to enter the starting end of the anoxic zone, and enabling gas stripping reflux activated sludge RAS from a gas stripping reflux device in the V-shaped secondary sedimentation tank, recycled sludge from a recycled sludge pump of the advanced treatment inclined tube sedimentation tank and a spare external carbon source to enter the anoxic zone;
step 4, introducing mixed liquor at the tail end of the anoxic zone into the aerobic zone for aeration treatment, wherein the mixed liquor in the anoxic zone and the aerobic zone is in a plug flow type, most of nitrified liquor fully nitrified at the tail end of the aerobic zone returns to the beginning end of the anoxic zone through a nitrified liquor internal reflux pump, and a small part of nitrified liquor enters a V-shaped secondary sedimentation tank for sludge-water separation and sedimentation treatment;
step 5, pumping most of the concentrated sludge at the bottom of the secondary sedimentation tank serving as external return sludge RAS back to the starting end of the composite ABR area by an external return sludge pump, and discharging a small amount of sludge serving as residual sludge to a sludge treatment unit; the suspended concentrated sludge in the middle layer of the secondary sedimentation tank continuously flows back to the starting end of the anoxic zone in real time by a gas stripping reflux device; the supernatant of the secondary sedimentation tank enters an inclined tube sedimentation tank for further advanced treatment;
and 6, adding auxiliary chemical phosphorus removal and flocculation precipitation agents into the inclined tube sedimentation tank according to the running condition of water quality, further removing residual pollutants to obtain high-quality effluent, and pumping a small amount of sludge generated by coagulation precipitation in the inclined tube sedimentation tank to the starting end of the anoxic zone for recycling through a recycling sludge pump.
CN202011600313.2A 2020-12-30 2020-12-30 UMIF synchronous nitrogen and phosphorus removal integrated tank for mixed liquid online fermentation and application method thereof Pending CN112979055A (en)

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