CN201068420Y - Gas-liquid mixing increasing biological fluidized bed reactor - Google Patents

Gas-liquid mixing increasing biological fluidized bed reactor Download PDF

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Publication number
CN201068420Y
CN201068420Y CNU2007201109454U CN200720110945U CN201068420Y CN 201068420 Y CN201068420 Y CN 201068420Y CN U2007201109454 U CNU2007201109454 U CN U2007201109454U CN 200720110945 U CN200720110945 U CN 200720110945U CN 201068420 Y CN201068420 Y CN 201068420Y
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reactor
water
water inlet
fluidized bed
liquid
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梁志伟
陈英旭
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Zhejiang University ZJU
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Zhejiang University ZJU
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    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage

Abstract

The utility model discloses a gas-liquid mixing promotion biological fluidized bed reactor which is provided with a reactor main body; the reactor main body is provided with a water distributing device, a biological packing layer, a reaction chamber partition board, a reverse flow baffle plate, a biological carrier, and a trapezoidal back flow opening; an intermediate water inlet opening, a sampling opening, a setting zone water inlet tube, and a setting zone return tube are arranged on the side wall of the reactor main body; wherein, the setting zone water inlet tube and the setting zone return tube are respectively connected with a sedimentation tube, an air exhaust opening is arranged at the top part of the reactor main body, and the water outlet opening at the upper end of the sedimentation tube is respectively connected with a return water tank, a return water pump, a return water valve, a return water flow meter and a trapezoidal back flow opening, the air exhaust opening is respectively connected with an air collector, a second air pump and a trapezoidal back flow opening, a micropore aerating ring is respectively connected with a gas rotameter, an air inlet valve, and a first air pump, and a water distributing device at the top part is respectively connected with a water inlet flow meter at the top part, a water inlet water valve at the top, a water inlet pump, and a water inlet tank. The utility model can be suitable for the high efficient biological treatment to high ammonia-nitrogen wastewater, can realize high efficient nitrogen removal, and simultaneously save energy.

Description

A kind of biological fluidized bed reactor for raising mixed gas and liquid
Technical field
The utility model relates to a kind of biological fluidized bed reactor for raising mixed gas and liquid, is applicable to high-performance bio processing high-ammonia-nitrogen sewage, can realize efficient denitrification, simultaneously save energy.
Background technology
Twentieth century beginning of the seventies, the aggravation of energy dilemma and becoming increasingly conspicuous of global environment problem in the world wide, and interdisciplinary mutual intersection has promoted people's deepening continuously to biologic treating technique research.Breakthrough progress has appearred in the theory of the biological treatment of waste water and utilisation technology.From the angle of microorganism growth pattern reactor, the wastewater biological reactor is divided into two kinds of base types: first kind is the apposition growth reactor.With the growth of microbial film form, its shortcoming is filler costliness, relatively low, the easy obstruction (to the filter tank) of processing load, power consumption big (to expanded bed, fluidized-bed) to the microorganism of this class reactor on the solid support thing.Second kind is the suspension growth reactor.This reactor needs to stir (or otherwise) so that microorganism (as granule sludge) is in suspended state all the time.Owing to do not need filler, simple in structure, obvious processing effect, this type of reactor is considered to the most rising wastewater treatment equipment.
Take a broad view of the domestic and foreign literature data, at present common aerobic reaction device mainly is divided into three kinds of activated sludge process, biomembrance process and membrane bioreactors.Wherein activated sludge process is commonly used mainly contains UNITANK activated sludge process, oxidation ditch activated sludge process, circulating type active sludge method (Cyclic Activated Sludge Technology, abbreviation CAST), absorption degradation activated sludge process (Adsorption Bio-degradation, abbreviation AB), LINPOR technology, PACT Powdered Activated Carbon activated sludge process (Powder activated carbonTechnology, abbreviation PACT), spray circulation bioreaction technology (Jet Loop Reactor is called for short JLR) etc.What biomembrance process was commonly used has three kinds, mainly comprise the compound bio membrane technique, representing technology is gas stripping type recirculation reactor, sequencing batch activated sludge biomembrance process (Sequencing Batch Biofilm Reactor, be called for short SBBR), the BAF recent development mainly contains BIOFOR technology (Rio-Fil-Tration OxygenatedReactor, be called for short BIOFOR), BIOSTYR technology etc., the MBBR of developing in recent years in the fluidized-bed process (Moving Bed Biofilm Reactor is called for short MBBR) etc.Active sludge and biological membrane biological treatment system are the most widely used two kinds of treatment technologies of current sewage treatment area, but still exist some urgent problems, the transfer efficiency of oxygen is very important one, and the main technology that adopts mainly is enhanced aeration activated sludge processes such as jet-flow aeration, retained aeration, pressurized aeration, micro-pore aeration.Wherein retained aeration is a kind of aeration process of efficient, less energy-consumption, traditional aeration process is free aeration, the bubble that rises is not subjected to the constraint on border, make the bubble of mixed solution very big, inefficiency, retained aeration utilizes the effect of contraction of pipeline to upstream, allows air-flow seldom form stronger disturbance in current, improves aeration efficient greatly.
Common third generation anaerobic reactor has following three kinds at present: anaerobic expanded granular sludge bed (ExpandedGranular Sludge Bed; be called for short EGSB); up-flow anaerobic sludge blanket-filtering layer reactor (UpfowAnaerobic Bed-Filter; be called for short UBF); internal-circulation anaerobic reactor (Internal Circulation; be called for short IC) etc. fully used granular sludge; fluidization; feedback control (backflow); ripe biology and engineerings such as larger ratio of height to diameter design; simultaneously since as every performance of the polymeric granule sludge of microorganism along with the operational condition of reactor with handle factor such as load and make corresponding adjustment; overcome the apposition growth reactor to a certain extent owing to shortcomings such as the easy obstruction of using filler to cause and power consumption are bigger; and the suspension growth reactor relies on the very high liquid upflow velocity and the large number of biological gas that produces to make granule sludge be in good suspended state all the time, filler in granule sludge wherein and the apposition growth reactor; solid support thing or carrier role are similar.But since the conditional request height of anerobe growth, the technology controlling and process difficulty, and some pollutents of can not independently degrading etc. have limited the development of anaerobic technique.
According to different wastewater properties, the structure of reactor is different, mainly can be divided into open and closed two kinds.Open characteristics are that the top of reactor is not sealed, not the biogas of collecting precipitation district liquid level release.This reactor mainly is the organic waste water that is used for handling lower concentration, and the waste water of middle lower concentration is after reaction zone is handled, and the organic concentration in the water outlet is lower, so the biogas amount that produces in the settling region is less, does not generally need to reclaim.The structure of reactor of this form is fairly simple, is easy to construction and installation and maintenance.Enclosed characteristics are that the top of reactor seals.The open difference of the structure of triphase separator does not need special collection chamber, but forms a big collection chamber between liquid level and pond face, can collect the biogas of reaction zone and settling region simultaneously.The reactor of this form is applicable to handles high concentrated organic wastewater or the higher organic waste water of sulfur-bearing hydrochlorate.Because when handling high concentrated organic wastewater, the settling region still has more biogas to overflow, and must reclaim.The shape of reactor has rectangle, square and circular, and circular reactor has the more stable characteristics of structure, but the triphase separator of building circular reactor than rectangle and square reactor complexity many.
Nitrogen is very important pollution factor in the water body, and along with the raising of industrial expansion and living standards of the people, the nitrogen content in municipal effluent, industrial sewage and the percolate sharply rises.The environmental quality that State Environmental Protection Administration announces shows, though the pollution situation in the important water system of China and lake takes a turn for the better to some extent in recent years, situation is still very severe.Many in addition trade effluents, as leather-making waste water, food processing wastewater, coke-oven waste water, synthetic ammonia waste water also have livestock breeding wastewater etc. all to contain a large amount of nitrate pollution things, just directly discharge through effective denitrogenation processing.Mankind's activity causes that simultaneously the nitrate pollution thing enters soil and ground water regime, and surface water and underground water produce severe contamination, have made natural purification mechanism be damaged.Therefore, the denitrogenation processing of waste water has become one of the focus of environmentalist research and difficult point.
The removal of nitrogen in water body is one of main environmental problem of Chinese scholars concern always.Improvement for nitrate pollution, common both at home and abroad have biological process and a physico-chemical processes, the engineering that physico-chemical process adopts has air stripping method, selectivity ion exchange method, break point chlorination, the magnesium ammonium phosphate precipitator method etc., but because the cost of physico-chemical process is higher, and cause secondary pollution easily, so its popularization is restricted.The biological denitrificaion method has characteristics such as economy, effective, easy to operate, non-secondary pollution, is acknowledged as the method with development prospect.
Traditional biological denitrification process slower development, mainly be to be subjected to that some factor restricts: the denitrification reaction time of (1) denitrification microorganism is oversize; (2) ammonia nitrogen will pass through two separate processes of nitrification and denitrification respectively, causes the operation process complexity; (3) nitric efficiency is not high always; (4) owing to organic carbon content in the waste water is low, in denitrification process, can cause the carbon source deficiency, influence the stability of microorganism.For overcoming the above problems, closely during the last ten years, many countries have strengthened the research to biological denitrificaion, and have all obtained important breakthrough theoretical and technical.With short distance nitration-denitrification process, anaerobic ammonia oxidation process and bioelectrochemistry denitrogenation is the priority appearance of large quantities of new bio denitride technologies of sign, not only remedied traditional nitrated-defective of denitrification process, improved denitrogenation of waste water efficient, reduce the denitrogenation of waste water cost, also filled up the blank that high concentration nitrogen-containing waste water does not have direct denitride technology.In the governance process of China's nitrate pollution, use for reference and use these scientific and technological achievements, have important practical significance undoubtedly.
Novel in recent years short distance nitration denitrification process mainly contains SHARON technology, ANAMMOX technology, CANON technology, OLAND technology etc.The key that realizes short-cut nitrification and denitrification is NH 4 +Oxidation is controlled at NO 2 -Stage.Up to the present, it is actually rare nitration reaction effectively to be controlled at the report in nitrosification stage in actual motion technology.This mainly is because influence NO 2 -So controlling factor (as temperature, pH, free ammonia FA, sludge retention time SRT and dissolved oxygen DO, substrate concn, the objectionable impurities etc.) more complicated of accumulation is will be with NH 4 +Oxidation successfully be controlled at nitrite stage not a duck soup, in the application of actual engineering, have a lot of problems.
N for a long time 2O, NO and NO 2All be considered to the by product of biological denitrificaion and to microorganism toxic or restraining effect, do not give due attention to its active effect in wastewater biological denitrificaion.Studies show that these intermediate products, especially NO and NO recently 2, extremely important even essential to the biological nitrogen conversion, NO and NO 2Recovery and ammonia oxidation speed to the nitrifier ammoxidation activity have strengthening effect, NO 2Can be used as electron acceptor(EA) oxidation ammonia etc.N 2O and NO xThe unusual exploitation that act as wastewater biological denitrificaion new technology, novel process that shows in biological denitrificaion provides new direction, has proposed some based on N 2O and NO xThe imagination of the wastewater biological denitrificaion of effect, microorganism is to NO xDemand be in 10 -6Level, for oxygen, NO xAeration process can be saved most of energy consumption, and NO xAbility with strengthened anaerobic ammoxidation and aerobic ammonia oxidation has the major application prospect.
Along with the discharge of wastewater that is rich in vitriol and nitrate in a large number, adopt anaerobic technique to handle in the water of back and still contain a large amount of sulfide and nitrate, difficulty of governance is bigger.The bio-oxidation sulfur removal technology that grew up in recent years adopts colorless sulfur bacteria or photosynthetic sulfur bacteria to remove sulfide more, but low because of load, and the elemental sulfur brill invests cell surface to be difficult to problem such as separation and to limit its practical engineering application.The most frequently used method of biological denitrificaion is A/O or A2/O2 technology, technology and operation relative complex, and often need additionally add organism such as methyl alcohol so that carry out heterotrophic denitrification, this can roll up the engineering operation cost undoubtedly.In the time of research recently denitrification and desulfurization process mainly be nitrate and sulfide by biological utilisation, generate nitrogen and vitriol or elemental sulfur at last.Research is arranged with the electron donor of pyrite, keep stable p H value and finally be converted into vitriol and ferrous hydroxide as denitrogenation.Discover to also have a large amount of aromatic compounds, ammonia ammonia and sulfide in the oil refinery effluent, handle back discovery COD, ammonia nitrogen and sulfide and remove in a large number, find insoluble elemental sulfur in the water simultaneously, prove that denitrification and desulfurization can also be removed organic carbon simultaneously.
Summary of the invention
The purpose of this utility model provides a kind of biological fluidized bed reactor for raising mixed gas and liquid.
Biological fluidized bed reactor for raising mixed gas and liquid has reactor body, reactor body is provided with the top water distributor from top to bottom successively, aerobic reactor zone, the hypoxia response district, the sludge settling district, trapezoidal refluxing opening, wherein aerobic reactor zone comprises the biologic packing material layer, the micro-pore aeration ring, the hypoxia response district comprises the reaction chamber dividing plate, reverse-flow baffle, bio-carrier, the reaction chamber dividing plate is two parallel wash plates, the dividing plate both sides are connected with the reactor body wall, the dividing plate lower end is connected with reverse-flow baffle, water-in in the middle of on the reactor body sidewall, being provided with, thief hole, the settling region water inlet pipe, the settling region return line, the settling region water inlet pipe is connected with sediment tube with the settling region return line, the reactor body top is provided with venting port, sediment tube upper end water outlet and reflux tank, the backflow water pump, the backflow water valve, recirculation water flow meter, trapezoidal refluxing opening is connected, venting port and air collector, second air pump, trapezoidal refluxing opening is connected, micro-pore aeration ring and gas rotameter, intake valve, first air pump is connected, top water distributor and top flooding velocity meter, top water inlet water valve, intake pump, inlet chest is connected, middle water-in and middle flooding velocity meter, middle water inlet water valve, intake pump, inlet chest is connected.
Described reactor body is a right cylinder, cylinder diameter is 200~300mm, cylinder height 800~1000mm, top vent 26 diameters 20~30mm, be connected with the air collector 28 of 10~20L, through second air pump 29, be connected to the trapezoidal refluxing opening 13 of reactor bottom at last, the biologic packing material layer has two fixedly filter screens respectively in two ends up and down, the centre is the honeycombed biologic packing material, the thickness of honeycombed biologic packing material is 200~300mm, the aperture is 3~6mm, the micro-pore aeration ring directly through 100~150mm, pipe is through 15~25mm, the pipe upper surface is uniform-distribution with micropore, the aperture is 1~3mm, space 6~10mm between each aperture, reaction chamber dividing plate length is 400~600mm, two plates are 100~150mm at interval, two two reverse-flow baffles that reaction chamber baffle plate lower end connects respectively, downward and reverse-flow baffle is 120 °~150 ° angles, long 20~the 25mm of bus, distance 30~50mm between sediment tube and the reactor body, sediment tube diameter 50~100mm, height 400~600mm, settling region water inlet pipe diameter is 32~50mm, downwards and 30 °~60 ° of main reaction wall angles, and pipe range 35~43mm, the diameter of precipitation return line is 32~50mm, make progress and 30 °~60 ° of main reaction wall angles, pipe range 42~71mm, the reverse-flow baffle bottom is taper sludge settling district, the sludge settling district has trapezoidal refluxing opening, be connected with the mud stopping valve, on reactor wall, also be provided with six thief holes, above two thief holes, the 80~120mm of being separated by, below four thief holes, the 100~150mm of being separated by, thief hole bottom is positioned at the main reaction region bottom.
The utility model is guidance with the design theory of biological denitrification reactor, consider from the microbial film of wastewater treatment and the operability and the working cost angle of fluidization practical application, ammonia nitrogen removal frank with raising waste water is a target, through great mass of data inquiry and actual observation experiment, sum up on existing reactor and the insufficient basis of denitrification process, the design focal point of this biological fluidized bed reactor for raising mixed gas and liquid has been considered Several Factors.(1) will be in the SHRON technology with NH 4 +Oxidation successfully be controlled at nitrite stage not a duck soup, in the application of actual engineering, there are a lot of problems, organic carbon content is low in the waste water simultaneously, in denitrification process, can cause the carbon source deficiency, also need to add carbon source, the design utilizes the two ends water inlet to finish the reaction of nitrosification denitrification denitrogenation simultaneously in a reaction unit, has avoided increasing in denitrification process the requirement of carbon source and strict control pH value.(2) the design considers that can produce certain oxides of nitrogen gas in denitrification process enters air, in the time of denitrogenation atmosphere has been caused secondary pollution, by the nearest oxynitride that studies have shown that denitrification effect there is certain promoter action, the design adopts the cyclic aeration mode first, because the oxynitride activity is very high to be easy to as electron acceptor(EA), the oxynitride that produces in the denitrification process is removed again fast again, can be improved the efficient of denitrogenation simultaneously.(3) because nitrifier is adapted at growing under the different conditions with denitrifying bacterium, nitrifier and denitrifying bacteria mixed growth in the nitration denitrification reactor in the time of general have influenced mutual activity.Therefore, this fluidized bed reactor designs nitrifier is apposition growth on the aerobic zone filler of upper end, and denitrifying bacteria is suspension growth in the anoxybiotic fluidized-bed, thereby does not influence activity separately, has satisfied the nitrosification denitrification process simultaneously, has improved nitric efficiency.(4) general reactor needs higher reflux ratio just can make granule sludge be in fluidized state, has improved the reactor apparatus requirement, has increased the consumption of the energy simultaneously.The design utilizes upper end gas lift and lower end liquid return simultaneously as the power of mud fluidized cleverly, saving to a certain degree the energy.(5) settling region insufficient height height in the general reactor, the solid-liquid mixed solution was fallen short of in the settling region residence time, cause sedimentation effect not good, be unfavorable for Solid-Liquid Separation, the design's independence settling region increases the settling region height greatly, virtual height is 400~600mm, can reach the good solid-liquid effect that is separated, and effectively prevents biological loss.(6) generally adopt square or rectangular reactor can effectively avoid the short flow phenomenon of liquid, but dead angle, local reaction district appear in rectangular reactor easily, causes the flow shape instability.Therefore, the design adopts circular reactor can avoid reacting the dead angle, and main reaction region is divided into three compartments simultaneously, and mud is in the fluidized circulation state, has avoided short flow phenomenon simultaneously.(7) from the materialization angle, can remove efficiently simultaneously by transfer transport between the nitrogen sulphur, this reactor design has been considered the technology that nitrogen sulphur is removed simultaneously simultaneously, aerobic stage ammonia nitrogen and vitriol reaction, ammonia nitrogen is converted into nitrate simultaneously, and the anoxic stage is carried out the removal of denitrification and sulfide.
The oxides of nitrogen gas that the utility model utilization produces is discharged at the venting port on reactor top at the bottom inner circulating aerating, is connected with air collector in turn, the portion gas discharging, and residual gas circulates through the bottom that air pump is connected to reactor at last.Mud circulates in reactor, upwards flow in anoxic main reaction region intermediate reaction chamber, reaction chamber through both sides flows downward, upwards do annular by the intermediate reaction chamber again and circulate, mud round-robin power is to be provided by the gas of bottom backflow and the negative pressure of liquid and the generation of main reaction region top gas distribution in the reactor.Reverse-flow baffle helps phegma, gas and granule sludge to cocycle, and uniform distribution can effectively prevent the phenomenon of the short stream in reactor of water into again, and whole reactor is right cylinder, does not have the reaction dead-time problem.
Description of drawings
Fig. 1 is the biological fluidized bed reactor for raising mixed gas and liquid structural representation;
Fig. 2 is the biological fluidized bed reactor for raising mixed gas and liquid schematic top plan view;
Among the figure: reactor body 1, reaction chamber dividing plate 2, reverse-flow baffle 3, micro-pore aeration ring 4, biologic packing material layer 5, top water distributor 6, water outlet 7, sediment tube 8, settling region water inlet pipe 9, settling region return line 10, bio-carrier 11, sludge settling district 12, trapezoidal refluxing opening 13, reflux tank 14, backflow water pump 15, backflow water valve 16, recirculation water flow meter 17, intake pump 18, inlet chest 19, first air pump 20, top water inlet water valve 21, large flooding velocity meter 22, intake valve 23, gas meter 24, thief hole 25, venting port 26, middle water-in 27, air collector 28, second air pump 29, middle water inlet water valve 30, middle water inlet water valve 31, aerobic reactor zone 32, hypoxia response district 33, mud stopping valve 34.
Embodiment
As shown in Figure 1, biological fluidized bed reactor for raising mixed gas and liquid has reactor body 1, reactor body 1 is provided with top water distributor 6 from top to bottom successively, aerobic reactor zone 32, hypoxia response district 33, sludge settling district 12, trapezoidal refluxing opening 13, wherein aerobic reactor zone 32 comprises biologic packing material layer 5, micro-pore aeration ring 4, hypoxia response district 33 comprises reaction chamber dividing plate 2, reverse-flow baffle 3, bio-carrier 11, reaction chamber dividing plate 2 is two parallel wash plates, the dividing plate both sides are connected with the reactor body wall, the dividing plate lower end is connected with reverse-flow baffle 3, water-in 27 in the middle of on reactor body 1 sidewall, being provided with, thief hole 25, settling region water inlet pipe 9, settling region return line 10, settling region water inlet pipe 9 is connected with sediment tube 8 with settling region return line 10, reactor body 1 top is provided with venting port 26, sediment tube 8 upper end water outlets 7 and reflux tank 14, backflow water pump 15, backflow water valve 16, recirculation water flow meter 17, trapezoidal refluxing opening 13 is connected, venting port 26 and air collector 28, second air pump 29, trapezoidal refluxing opening 13 is connected, micro-pore aeration ring 4 and gas rotameter 24, intake valve 23, first air pump 20 is connected, top water distributor 6 and top flooding velocity meter 22, top water inlet water valve 21, intake pump 18, inlet chest 19 is connected, middle water-in 27 and middle flooding velocity meter 31, middle water inlet water valve 30, intake pump 18, inlet chest 19 is connected.
Described reactor body 1 is a right cylinder, and cylinder diameter is 200~300mm, cylinder height 800~1000mm, top vent 26 diameters 20~30mm, be connected with the air collector 28 of 10~20L,, be connected to the trapezoidal refluxing opening 13 of reactor bottom at last through second air pump 29.The biologic packing material layer has two fixedly filter screens respectively in two ends about in the of 5, the centre is the honeycombed biologic packing material, the thickness of honeycombed biologic packing material is 200~300mm, the aperture is 3~6mm, micro-pore aeration ring 4 directly through 100~150mm, pipe is through 15~25mm, the pipe upper surface is uniform-distribution with micropore, the aperture is 1~3mm, space 6~10mm between each aperture, reaction chamber dividing plate 2 length are 400~600mm, two plates are 100~150mm at interval, two two reverse-flow baffles 3 that reaction chamber baffle plate lower end connects respectively, downward and reverse-flow baffle 3 is 120 °~150 ° angles, long 20~the 25mm of bus, distance 30~50mm between sediment tube 8 and the reactor body 1, sediment tube diameter 50~100mm, height 400~600mm, water inlet pipe 9 diameters in settling region are 32~50mm, downwards and 30 °~60 ° of main reaction wall angles, pipe range 35~43mm, the diameter of precipitation return line 10 is 32~50mm, upwards with 30 °~60 ° of main reaction wall angles, pipe range 42~71mm, the reverse-flow baffle bottom is taper sludge settling district 12, and sludge settling district 12 has trapezoidal refluxing opening 13, is connected with mud stopping valve 34, on reactor wall, also be provided with six thief holes 25, above two thief holes, the 80~120mm of being separated by, below four thief holes, the 100~150mm of being separated by, thief hole bottom is positioned at the main reaction region bottom.
Biological fluidized bed reactor for raising mixed gas and liquid structurally constitutes by 5 parts, i.e. inlet and outlet system, main reaction system, return-flow system, aerating system, sludge drainage system; Comprise upper end water inlet and middle water inlet, sediment tube upper end water outlet for inlet and outlet system.Return-flow system comprises liquid return and gas backstreaming.Waste water enters reactor top and centre from inlet chest respectively through intake pump, amount of inlet water according to a certain percentage, nitration reaction is carried out in top water inlet in the aerobic zone filler, because aeration rate has certain restriction, nitrosation reaction takes place mainly.The aeration ring adopts the micro-pore aeration intensifying technology below biologic packing material.Middle water inlet left side reaction chamber in reactor flows downward earlier, upwards flow with reflux gas liquid at reactor bottom, two reaction chambers about under biologic packing material, flowing to respectively, waste water and granule sludge enter sediment tube at reactor right side reaction chamber, granule sludge comes back in the reactor through precipitation, flow out from the outlet of sediment tube upper end through sedimentary waste water, part discharging, remaining inflow reflux tank, entering reactor through the backflow water pump from reactor bottom refluxes, the portion gas that produces from reactor head also passes through air collector successively simultaneously, air pump, and enter reactor bottom with phegma and reflux, the portion gas discharging.
The conversion process of denitrogenation and nitrifier and denitrifying bacteria each side characteristic by analysis, consider to overcome the severe condition in the denitrification process emphatically, improve nitric efficiency, the denitrifier poor growth notes reducing the problem of loss, by improvement to the biological denitrification reactor operation process, according to the characteristics of denitrifier advantage in conjunction with microbial film and active sludge, adopt the two ends water intake mode, middle aeration, settling region independently, produce designs such as gas circulation reaction, the characteristic that reactor is embodied can reach better denitrification effect in denitrogenation of waste water is handled, for the selection of later Microbial denitrogenation reactor provides new thinking.
Specify as follows:
1) packing into of granule sludge and biologic packing material: before disposing of sewage, open reactor upper end air outlet capping 6, to pack in the reactor by the granule sludge of every physical behavior after measured again, in reactor, be full of water and flow to keep stable after, the estimation granule sludge of sening as an envoy to is in the flow rate of water flow scope of fluidized state according to the granule sludge concentration range; Open aerating apparatus 4 and reflux pump 15 then, regulate the reflux pump flow velocity to being slightly larger than the minimum value that can make the mud fluidized state; With biologic packing material pack into the upper end aerobic zone, build the upper end air outlet capping; The sponge that the absorption nitrifier is arranged in the filler to guarantee at the reactor initial operating stage stable nitrifier concentration being arranged, makes the operation that reactor can be stable.
2) water inlet system: water inlet system is provided with inlet chest, size is 400mm * 300mm * 500mm, water inlet pipe adopts 10~30mmPVC pipe, the upper end water distributor is aperture 2~5mm four manifold assemblies formula water distributors, be beneficial to water distribution uniformity, middle water inlet is directly injected by 10~30mm water-in, and upper end and middle water inlet are carried out according to certain ratio.
3) micro-pore aeration: aerator comprises pneumatic pump, air delivery pipe and micropore aeration pipe, micropore aeration pipe is the annular level and is in the biologic packing material lower end, advantage is to be difficult for by sludge blockage solarization air cap, conserve space, to provide negative pressure for the granule sludge fluidisation simultaneously, because micropore aeration pipe is in the reactor mid-way, so can there be two zones of anoxic, aerobic lower end, upper end.
4) settling system: sediment tube links to each other with main reaction region on the reactor right side, right side main reaction region water (flow) direction is downward, so waste water enters sediment tube from the upper end Link Port, precipitating sludge is from the lower end Link Port main reaction region that fails to be convened for lack of a quorum, because the sediment tube height reaches 400~600mm, the upper end is a water port, is connected with water tank, part water refluxes through trapezoidal refluxing opening from reactor bottom through water pump, part discharging.
5) backflow of waste water: waste water is discharged through the water outlet of sediment tube upper end, the part water outlet is directly discharged through valve, remaining water outlet flows in the reflux tank, the reflux tank size is 400mm * 300mm * 500mm, enter reactor bottom through the backflow water pump again, enter trapezoidal refluxing opening simultaneously with reflux gas and reflux.The size of the backflow water yield will be according to the decision of different factor, and granule sludge reaches fluidized state and determines minimum flow velocity, and various form nitrogen concentrations of water outlet and COD concentration can not reach standard will increase reflux ratio.
6) backflow of generation gas: the reactor head capping is opened three venting port, wherein a purpose is the gas that produces for the ease of collecting, utilize the gas that produces to carry out cyclic aeration simultaneously, another purpose is exactly for pressure that can conditioned reaction device internal gas, is convenient to the normal operation of controlling reactor.Expellant gas enters a safety flack through vapor pipe earlier, the gas pressure intensity that can reflect reactor top, be connected with a bigger air collector again, its effect is in order to regulate and control gas, can carry out cyclic aeration according to a certain percentage, discharge behind the remaining gas process alkali formula tourie, round-robin gas enters into return line through gas rotameter, needle-valve, enters the trapezoidal refluxing opening of reactor bottom with backflow waste water and refluxes.
7) water sample monitoring: after waiting reactor to move a section, by sampling unit 25 top-down samplings successively, and taking-up water water sample, different shape nitrogen concentration and COD value to each thief hole water sample detect, whether analyze aeration intensity, granule sludge concentration, reflux ratio suitable, nitrogen concentration and COD concentration value as the water outlet water sample are undesirable, then consider the dosage that whether continues to increase aeration intensity, granule sludge, reflux ratio etc., till detecting various nitrogen concentrations of water outlet and COD concentration value and meeting the requirements according to different phenomenon.After reactor moved longer for some time, reply water outlet water sample carried out continuous detecting.
8) discharge of mud: after reactor operation for some time along with a large amount of breedings of microorganism, sludge concentration may increase, improved the power requirement of fluidized state, to regularly carry out the discharging of excess sludge, at first open air outlet, reactor upper end, open the stopping valve of mud vent pipe then, utilize action of gravity that mud in the sludge bucket is discharged, the eliminating amount will be decided according to the sludge concentration that reality is surveyed.

Claims (8)

1. biological fluidized bed reactor for raising mixed gas and liquid, it is characterized in that having reactor body (1), reactor body (1) is provided with top water distributor (6) from top to bottom successively, aerobic reactor zone (32), hypoxia response district (33), sludge settling district (12), trapezoidal refluxing opening (13), wherein aerobic reactor zone (32) comprises biologic packing material layer (5), micro-pore aeration ring (4), hypoxia response district (33) comprises reaction chamber dividing plate (2), reverse-flow baffle (3), bio-carrier (11), reaction chamber dividing plate (2) is two parallel wash plates, the dividing plate both sides are connected with the reactor body wall, the dividing plate lower end is connected with reverse-flow baffle (3), water-in (27) in the middle of on reactor body (1) sidewall, being provided with, thief hole (25), settling region water inlet pipe (9), settling region return line (10), settling region water inlet pipe (9) is connected with sediment tube (8) with settling region return line (10), reactor body (1) top is provided with venting port (26), sediment tube (8) upper end water outlet (7) and reflux tank (14), backflow water pump (15), backflow water valve (16), recirculation water flow meter (17), trapezoidal refluxing opening (13) is connected, venting port (26) and air collector (28), second air pump (29), trapezoidal refluxing opening (13) is connected, micro-pore aeration ring (4) and gas rotameter (24), intake valve (23), first air pump (20) is connected, top water distributor (6) and top flooding velocity meter (22), top water inlet water valve (21), intake pump (18), inlet chest (19) is connected, middle water-in (27) and middle flooding velocity meter (31), middle water inlet water valve (30), intake pump (18), inlet chest (19) is connected.
2. a kind of biological fluidized bed reactor for raising mixed gas and liquid according to claim 1 is characterized in that described reactor body (1) is a right cylinder, and cylinder diameter is 200~300mm, cylinder height 800~1000mm.
3. a kind of biological fluidized bed reactor for raising mixed gas and liquid according to claim 1, it is characterized in that described reactor body (1) top vent (26), venting port (26) diameter 20~30mm, be connected with the air collector (28) of 10~20L, through second air pump (29), be connected to the trapezoidal refluxing opening (13) of reactor bottom at last.
4. a kind of biological fluidized bed reactor for raising mixed gas and liquid according to claim 1, it is characterized in that described biologic packing material layer (5) has two fixedly filter screens respectively in two ends up and down, the centre is the honeycombed biologic packing material, and the thickness of honeycombed biologic packing material is 200~300mm, and the aperture is 3~6mm.
5. a kind of biological fluidized bed reactor for raising mixed gas and liquid according to claim 1, it is characterized in that described micro-pore aeration ring (4) directly through 100~150mm, pipe is through 15~25mm, the pipe upper surface is uniform-distribution with micropore, the aperture is 1~3mm, space 6~10mm between each aperture.
6. a kind of biological fluidized bed reactor for raising mixed gas and liquid according to claim 1, it is characterized in that described reaction chamber dividing plate (2) length is 400~600mm, two plates are 100~150mm at interval, two two reverse-flow baffles (3) that reaction chamber baffle plate lower end connects respectively, downward and reverse-flow baffle (3) is 120 °~150 ° angles, the long 20~25mm of bus.
7. a kind of biological fluidized bed reactor for raising mixed gas and liquid according to claim 1, it is characterized in that distance 30~50mm between described sediment tube (8) and the reactor body (1), sediment tube diameter 50~100mm, height 400~600mm, settling region water inlet pipe (9) diameter is 32~50mm, downwards and 30 °~60 ° of main reaction wall angles, pipe range 35~43mm, the diameter of precipitation return line (10) is 32~50mm, upwards with 30 °~60 ° of main reaction wall angles, pipe range 42~71mm.
8. a kind of biological fluidized bed reactor for raising mixed gas and liquid according to claim 1, it is characterized in that described reverse-flow baffle bottom is taper sludge settling district (12), sludge settling district (12) has trapezoidal refluxing opening (13), be connected with mud stopping valve (34), on reactor wall, also be provided with six thief holes (25), above two thief holes, the 80~120mm of being separated by, below four thief holes, the 100~150mm of being separated by, thief hole bottom is positioned at the main reaction region bottom.
CNU2007201109454U 2007-06-22 2007-06-22 Gas-liquid mixing increasing biological fluidized bed reactor Expired - Lifetime CN201068420Y (en)

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101857306A (en) * 2009-04-07 2010-10-13 上海达源环境科技工程有限公司 Aerobic sedimentation pond for sewage treatment
CN101857334B (en) * 2009-04-07 2013-07-17 上海达源环境科技工程有限公司 Sewage treatment device and sewage treatment process thereof
CN103214102A (en) * 2012-01-18 2013-07-24 株式会社日立工业设备技术 Wastewater treatment equipment
CN105585119A (en) * 2014-10-22 2016-05-18 中国石化工程建设有限公司 A nitrification-denitrification two-phase expanded-bed reactor and a sewage treating process
CN107892437A (en) * 2017-11-28 2018-04-10 华夏碧水环保科技有限公司 A kind of MBBR reaction systems of strengthened denitrification function

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101857306A (en) * 2009-04-07 2010-10-13 上海达源环境科技工程有限公司 Aerobic sedimentation pond for sewage treatment
CN101857334B (en) * 2009-04-07 2013-07-17 上海达源环境科技工程有限公司 Sewage treatment device and sewage treatment process thereof
CN103214102A (en) * 2012-01-18 2013-07-24 株式会社日立工业设备技术 Wastewater treatment equipment
CN103214102B (en) * 2012-01-18 2016-03-09 株式会社日立制作所 Sewage treatment equipment
CN105585119A (en) * 2014-10-22 2016-05-18 中国石化工程建设有限公司 A nitrification-denitrification two-phase expanded-bed reactor and a sewage treating process
CN107892437A (en) * 2017-11-28 2018-04-10 华夏碧水环保科技有限公司 A kind of MBBR reaction systems of strengthened denitrification function
CN107892437B (en) * 2017-11-28 2020-09-15 华夏碧水环保科技有限公司 MBBR reaction system with enhanced denitrification function

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