CN112978923B - Mixed fluidized bed reactor and application thereof - Google Patents
Mixed fluidized bed reactor and application thereof Download PDFInfo
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- CN112978923B CN112978923B CN202110344739.4A CN202110344739A CN112978923B CN 112978923 B CN112978923 B CN 112978923B CN 202110344739 A CN202110344739 A CN 202110344739A CN 112978923 B CN112978923 B CN 112978923B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 52
- 238000011049 filling Methods 0.000 claims abstract description 13
- 231100000331 toxic Toxicity 0.000 claims abstract description 8
- 230000002588 toxic effect Effects 0.000 claims abstract description 8
- 238000012856 packing Methods 0.000 claims abstract description 6
- 239000000725 suspension Substances 0.000 claims description 6
- 239000010815 organic waste Substances 0.000 claims 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 61
- 229910052760 oxygen Inorganic materials 0.000 abstract description 61
- 239000001301 oxygen Substances 0.000 abstract description 61
- 239000002351 wastewater Substances 0.000 abstract description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 16
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 6
- 229910052799 carbon Inorganic materials 0.000 abstract description 6
- 239000012530 fluid Substances 0.000 abstract description 6
- 238000004065 wastewater treatment Methods 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 25
- 239000010802 sludge Substances 0.000 description 25
- 238000000034 method Methods 0.000 description 19
- 230000008569 process Effects 0.000 description 19
- 239000007788 liquid Substances 0.000 description 13
- 230000000694 effects Effects 0.000 description 10
- 238000002156 mixing Methods 0.000 description 10
- 239000007787 solid Substances 0.000 description 9
- 239000000945 filler Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 230000009471 action Effects 0.000 description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 5
- 244000005700 microbiome Species 0.000 description 5
- 231100000614 poison Toxicity 0.000 description 5
- 239000003440 toxic substance Substances 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 238000005273 aeration Methods 0.000 description 4
- 238000005191 phase separation Methods 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 239000006260 foam Substances 0.000 description 3
- 238000006396 nitration reaction Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 231100000419 toxicity Toxicity 0.000 description 3
- 230000001988 toxicity Effects 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 229910045601 alloy Inorganic materials 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 231100000086 high toxicity Toxicity 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000033001 locomotion Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 231100000167 toxic agent Toxicity 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
Classifications
-
- 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
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
-
- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The mixed fluidized bed reactor comprises a tank body, a filling part, a first guide plate and a second guide plate, wherein the tank body is provided with a water inlet and a water outlet, the water inlet is positioned at the bottom end of the tank body, the water outlet is positioned at the side surface of the tank body, the filling part is positioned above the water inlet, the first guide plate is positioned above the filling part, the second guide plate is positioned above the first guide plate, the lower end of the second guide plate is positioned in the tank body, and the upper end of the second guide plate is higher than the water outlet; the packing component comprises a screen and a guide cylinder, the screen and the guide cylinder are of hollow columnar structures, the guide cylinder is positioned in the screen, an annular containing cavity is formed between the screen and the guide cylinder, and a carrier is arranged in the annular containing cavity. The application of the mixed fluid bed reactor is that the mixed fluid bed reactor is used for treating toxic organic wastewater. The invention can realize coexistence of multi-stage dissolved oxygen areas in the tank body, has high carbon and nitrogen removal efficiency, and belongs to the field of environmental bioengineering wastewater treatment.
Description
Technical Field
The invention relates to the field of environmental bioengineering wastewater treatment, in particular to a mixed fluidized bed reactor and application thereof.
Background
The key point of treatment of eutrophic polluted water is to remove nitrogen and phosphorus, and at present, the most common mode of nitrogen removal is biological nitrogen removal. The traditional biological denitrification is a process that organic nitrogen and ammonia nitrogen in wastewater are finally converted into nitrogen-containing gas through ammoniation, nitration and denitrification processes under the action of microorganisms. Wherein the ammonification and nitration reactions take molecular oxygen as electron acceptor, so that the reaction only occurs when there is sufficient dissolved oxygen. The dissolved oxygen concentration in the reactor should be kept sufficient in order to meet the normal nitrification. Whereas the traditional denitrification process needs to occur in an anaerobic environment, it is generally considered that the denitrification reaction occurs only when the dissolved oxygen concentration is below 0.5 mg/L. Therefore, to realize the traditional whole biological denitrification process, the process needs to be carried out in two reactors, and the concentration of dissolved oxygen needs to be controlled.
Waste water from petrochemical industry, coal chemical industry, coal coking, gas purification, chemical product recovery and refining and the like contains high-concentration organic matters, but has low biodegradability and high toxicity. Among them, low biodegradability can limit denitrification reactions. At present, the water treatment plant widely uses the operation modes of prepositive anaerobic technology such as A/O, A2/O, A/O2 and the like, and aims to decompose organic substances which are difficult to degrade, reduce the toxicity of wastewater, crack macromolecular substances and improve the biodegradability of the wastewater so as to be used for denitrification. However, due to the presence of nitrogen-containing toxic compounds such as CN-, SCN-, the effect is often insignificant when the toxicity is reduced using a pre-anaerobic process. Anaerobic acidification and anaerobic methanogenesis processes are totally and significantly inhibited. The high toxicity inhibits the nitration reaction, and the pre-aerobic process OAO can be used to remove most of the organic and toxic substances. However, the pre-aerobic process can consume the organic carbon source for denitrification in advance, and the organic load of the subsequent biological units can be increased by discarding the pre-anaerobic treatment. Some refractory toxic substances are difficult to degrade under aerobic conditions, and can inhibit the nitrification process. In addition, the aerobic biological treatment of the wastewater generally requires that dissolved oxygen is 4-5 mg/L, in order to achieve the dissolved oxygen amount, a mode of improving aeration is often adopted in the process, a large amount of energy is additionally consumed by excessively high aeration amount, a lot of aeration power is wasted, meanwhile, a large amount of foam is generated by organic matters such as surfactants and the like contained in the wastewater under the condition of sufficient aeration, and the rapid increment of filamentous bacteria is brought by the sufficient dissolved oxygen environment. Foam and expanded sludge pass over the overflow weir groove to take away a large amount of sludge, so that the process stability is affected.
Summarizing the above, there are disadvantages to using either a pre-anaerobic or a pre-aerobic process to treat toxic organic wastewater: in the pre-anaerobic treatment, anaerobic bacteria are easily inhibited by toxic substances, the anaerobic effect is poor, and denitrification cannot be performed. In the pre-aerobic treatment, the inhibition of organic matters on nitrification is partially relieved, but excessive carbon sources are consumed, so that denitrification carbon sources in the subsequent working section are insufficient, and some refractory organic matters are difficult to degrade under the condition of complete aerobic. In summary, this results in difficulty in achieving efficient carbon and nitrogen removal at the same time, whether a pre-anaerobic or a pre-aerobic process is used.
Disclosure of Invention
Aiming at the technical problems existing in the prior art, the invention aims at: provides a mixed fluidized bed reactor capable of realizing coexistence of aerobic and anoxic environments and application thereof.
In order to achieve the above purpose, the invention adopts the following technical scheme: the mixed fluidized bed reactor based on wastewater treatment comprises a tank body, a filling part, a first guide plate and a second guide plate, wherein the tank body is provided with a water inlet and a water outlet, the water inlet is positioned at the bottom end of the tank body, the water outlet is positioned on the side surface of the tank body, the filling part is positioned above the water inlet, the first guide plate is positioned above the filling part, the second guide plate is positioned above the first guide plate, the lower end of the second guide plate is positioned in the tank body, and the upper end of the second guide plate is higher than the water outlet; the packing component comprises a screen and a guide cylinder, the screen and the guide cylinder are of hollow columnar structures, the guide cylinder is positioned in the screen, an annular containing cavity is formed between the screen and the guide cylinder, and a carrier is arranged in the annular containing cavity; the first guide plate is of a cambered surface structure with a downward concave surface, and a first guide hole is formed in the first guide plate; the second guide plate is internally provided with a guide channel which is communicated with the upper area and the lower area of the second guide plate, the side surface of the second guide plate is provided with a second guide hole, and the second guide hole is communicated with the guide channel and the outer side of the second guide plate. After the structure is adopted, the coexistence of the multistage dissolved oxygen areas, namely the coexistence of aerobic and anoxic microenvironments, can be realized in the tank body. The diameter of the screen is larger than that of the guide cylinder and is arranged outside the guide cylinder.
Preferably, the flow guide channel comprises a flow guide section, a gas collecting section and an outlet section which are sequentially connected, wherein the flow guide section and the outlet section are of cylindrical structures, the diameter of the flow guide section is larger than that of the outlet section, and the gas collecting section is of a circular truncated cone structure.
Preferably, the tank body is provided with an overflow weir, and the water outlet is arranged at the outer side of the overflow weir.
As a preference, a mixed fluidized bed reactor further comprises a hanging lug and a fixing block, wherein the hanging lug is fixedly connected with the first guide plate, the fixing block is fixedly connected with the tank body, a clamping groove is formed in the fixing block, and the hanging lug is detachably clamped into the clamping groove.
Preferably, the number of the fixing blocks is multiple, and the multiple fixing blocks are respectively located at different heights. After the structure is adopted, the hanging lugs can be hung on the fixing blocks with different heights, so that the height of the first guide plate can be adjusted to adapt to different requirements.
Preferably, the first deflector is a hemispherical plate, and the ratio of the outer diameter of the first deflector to the inner diameter of the tank is 0.6-0.9.
Preferably, the carrier is a suspension carrier. After the structure is adopted, a relatively compact space is formed in the annular containing cavity by utilizing the adsorption and film hanging of the carrier sludge, and dissolved oxygen is utilized by microorganisms in the oxygen transmission process, so that an anoxic or completely anaerobic environment in the carrier and the biological film is formed, and the anaerobic fermentation of the sludge, the cracking of macromolecular refractory organic matters and the denitrification of the organic carbon source are facilitated.
Preferably, the number of the first diversion holes is a plurality, and the plurality of the first diversion holes are arranged in an annular array.
Preferably, the mixed fluidized bed reactor further comprises an air pump and a gas distributor, wherein the gas distributor is positioned between the water inlet and the packing component, and the air pump is connected with the gas distributor through an air inlet pipeline.
The material of the screen is stainless steel or nickel-based alloy.
The bottom of the tank body is of a round corner structure. The structure can reduce the sludge accumulation phenomenon and lead the material distribution in the reactor to be more uniform.
The application of the mixed fluid bed reactor is that the mixed fluid bed reactor is used for treating toxic organic wastewater.
When the mixed fluidized bed reactor is used, air is pumped from the bottom, the gas-liquid-solid mixed flow rises from the bottom, so that the highest dissolved oxygen concentration is achieved in the area below the first guide plate except for the area filled with filler, the area is a primary dissolved oxygen area, the gas, liquid and solid are uniformly distributed and fluidized, the activated sludge is uniformly distributed in the area, but in the filler area, the activated sludge is attached to a carrier to form a biological film on the carrier, and dissolved oxygen is utilized by microorganisms in the process of transferring in the area, so that an anaerobic area is formed in the carrier or in the filler area. The areas above the first guide plate and in the second guide plate form a secondary dissolved oxygen area.
In general, the invention has the following advantages:
1. the coexistence of the multistage dissolved oxygen areas is realized in the reactor, the concentration of dissolved oxygen in the one-stage dissolved oxygen area is highest, no obvious dissolved oxygen gradient exists, the mass transfer speed in the area is highest, a large amount of organic matters are rapidly degraded in the area, and the treatment load of the subsequent area is reduced; in the anaerobic zone, a macroscopic dissolved oxygen gradient division from outside to inside is formed due to the existence of the carrier and the screen, and a microscopic dissolved oxygen gradient is formed on the carrier and the biological film, so that synchronous nitrification and denitrification reactions are facilitated, and partial aerobic refractory organic matters can be degraded in the anaerobic zone; the second-stage dissolved oxygen area is the area where the effluent finally stays, the dissolved oxygen in the area is about 0.8 of that in the first-stage dissolved oxygen area, the concentration of organic matters in the area is relatively low, and under the condition of sufficient oxygen, microorganisms in the area are in an endogenous metabolism stage, so that the COD of the effluent can be further reduced, and the sludge quantity can be reduced.
2. The high concentration of toxic organic matters needs to be rapidly degraded and detoxified under the aerobic condition, while some refractory matters need to be hydrolyzed under the anaerobic condition before being fully degraded under the aerobic condition. The reactor with coexisting multi-stage dissolved oxygen areas can adapt to the special water quality condition, thereby avoiding the operations such as reflux and the like of the multi-stage reactor and reducing the construction and operation cost.
3. The two guide plates promote the gas-liquid phase flow and mixing in the reactor to be more reasonable and uniform, and the mixing state is good in the area near the water inlet, the mixing speed is high, and the mass transfer and reaction speeds are high. The area near the water outlet is in a push flow overflow state from bottom to top, which is the part with the longest residence time in the reactor, and no back mixing phenomenon exists. The gas-liquid-solid separation is gradually carried out in the three-phase separation area formed by the second guide plate and the first guide plate, so that the separation effect is obvious, and the phenomena of floating mud and foam expansion are avoided.
4. The carrier of the invention interacts with the gas-liquid flow nearby to form a movable biological bed in the region, a film is hung on the suspended carrier, and microbial communities with longer generation period such as enriched denitrifying bacteria are immobilized. And the movement rate of the suspension carrier can be controlled by changing the filling quantity, so that the biological film on the suspension carrier can keep a relatively stable thickness. Thereby forming macroscopic dissolved oxygen gradient in the region and realizing anaerobic biological process in the reactor.
5. Compared with the traditional fluidized bed, the sludge enrichment area is more reasonable, and the defects of local sludge accumulation and sludge dead zone of the traditional fluidized bed are overcome.
6. Compared with the multistage series reactors, the invention can change the stay time of the wastewater in different dissolved oxygen areas by adjusting the position of the first guide plate according to the water quality of the effluent and the requirement of the effluent index on the premise of not changing the inflow flow, so that the reactor can adapt to various water qualities and working conditions.
Drawings
Fig. 1 is an internal structural view of a mixed fluidized bed reactor.
Fig. 2 is a perspective view of a first baffle.
FIG. 3 is a schematic view showing the internal structure of a mixed fluidized bed reactor in use.
FIG. 4 is a graph of flow velocity profile in a mixed fluidized bed reactor.
FIG. 5 is a graph showing the concentration profile of dissolved oxygen in a mixed fluidized bed reactor.
FIG. 6 is a graph of dissolved oxygen concentration versus depth in an anaerobic zone.
FIG. 7 is a graph showing the COD treatment effect.
FIG. 8 is a view showing the denitrification effect of the conventional fluidized bed reactor.
FIG. 9 is a graph showing denitrification effect of the mixed fluidized bed reactor.
Wherein 1 is a tank body, 2 is a guide cylinder, 3 is a screen, 4 is a first guide plate, 5 is a second guide plate, 6 is a second guide hole, 7 is a first guide hole, 8 is a hanging lug, 9 is a fixed block, 10 is an overflow weir, 11 is a water inlet, 12 is a water outlet, 13 is an air pump, 14 is a gas distributor, 15 is a water pump, 16 is a carrier, 17 is a water quality monitor, 18 is a guide section, 19 is a gas collecting section, 20 is a gas outlet section, A is a primary dissolved oxygen area, B is a secondary dissolved oxygen area, and C is an anaerobic area.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments.
Example 1
The mixed fluidized bed reactor based on wastewater treatment comprises a tank body, a filling part, a first guide plate and a second guide plate, wherein the tank body is provided with a water inlet and a water outlet, the water inlet is positioned at the bottom end of the tank body, the water outlet is positioned on the side surface of the tank body, the filling part is positioned above the water inlet, the first guide plate is positioned above the filling part, the second guide plate is positioned above the first guide plate, the lower end of the second guide plate is positioned in the tank body, and the upper end of the second guide plate is higher than the water outlet; the packing component comprises a screen and a guide cylinder, the screen and the guide cylinder are of hollow columnar structures, the guide cylinder is positioned in the screen, an annular containing cavity is formed between the screen and the guide cylinder, and a carrier is arranged in the annular containing cavity; the first guide plate is of a cambered surface structure with a downward concave surface, and a first guide hole is formed in the first guide plate; the second guide plate is internally provided with a guide channel which is communicated with the upper area and the lower area of the second guide plate, the side surface of the second guide plate is provided with a second guide hole, and the second guide hole is communicated with the guide channel and the outer side of the second guide plate.
The flow guide channel comprises a flow guide section, a gas collecting section and an outlet section which are sequentially connected, wherein the flow guide section and the outlet section are of cylindrical structures, the diameter of the flow guide section is larger than that of the outlet section, and the gas collecting section is of a circular truncated cone structure.
The tank body is provided with an overflow weir, and the water outlet is arranged at the outer side of the overflow weir.
The mixed fluidized bed reactor further comprises a hanging lug and a fixing block, wherein the hanging lug is fixedly connected with the first guide plate, the fixing block is fixedly connected with the tank body, a clamping groove is formed in the fixing block, and the hanging lug is detachably clamped into the clamping groove.
The quantity of fixed blocks is the multiunit, and multiunit fixed block is in different altitudes respectively.
The first guide plate is a hemispherical plate, and the ratio of the outer diameter of the first guide plate to the inner diameter of the tank body is 0.6-0.9.
The carrier is a suspension carrier. The suspension carrier is a lightweight ceramic carrier with internal air holes, is prepared from coal gangue and biological sludge, and has a particle density of 1.091 and a specific surface area of 674.4.
The number of the first diversion holes is multiple, and the first diversion holes are distributed in an annular array.
The mixed fluidized bed reactor also comprises an air pump and a gas distributor, wherein the gas distributor is positioned between the water inlet and the filler component, and the air pump is connected with the gas distributor through an air inlet pipeline.
The application of the mixed fluid bed reactor is that the mixed fluid bed reactor is used for treating toxic organic wastewater.
The screen mesh is made of stainless steel or nickel-based alloy, and is sleeved on the outer side of the guide cylinder.
The bottom of the tank body is of a hemispherical structure with the inner diameter of 120cm, and the tank body is 190cm higher than the bottom. The inner diameter of the screen is 75cm; the thickness of the annular accommodating cavity is 25cm; the inner diameter of the first guide plate is 100cm; the heights of the guide cylinder and the screen are 150cm, and the top of the guide cylinder and the bottom of the first guide plate are positioned on the same plane; the first diversion holes are annularly arranged on the first diversion plate by taking a vertical line as a central axis, and the bottom end height of each first diversion hole is 30cm higher than the bottom end of each first diversion plate; the bottom of the first diversion hole is in the same plane with the bottom of the second diversion plate, the second diversion hole is arranged on the outer side of the diversion section, the second diversion holes are uniformly distributed in two rows of rings, the second diversion holes are positioned below the liquid level, and the aperture of the second diversion hole is 5cm.
The sludge mixed liquid in the reactor sequentially passes through a water inlet, a gas distributor, a sludge upflow area, a three-phase separation area and a water outlet. The sludge rising area is positioned in the center of the filler component, and the pumped air drives the sludge to rise; the three-phase separation zone is the area above the packing element.
When the mixed fluidized bed reactor is used, air is pumped from the bottom, the gas-liquid-solid mixed flow rises from the bottom, so that the highest dissolved oxygen concentration is achieved in the area below the first guide plate except for the area filled with filler, the area is a primary dissolved oxygen area, the gas, liquid and solid are uniformly distributed and fluidized, the activated sludge is uniformly distributed in the area, but in the filler area, the activated sludge is attached to a carrier to form a biological film on the carrier, and dissolved oxygen is utilized by microorganisms in the process of transferring in the area, so that an anaerobic area is formed in the carrier or in the filler area. The areas above the first guide plate and in the second guide plate form a second-stage dissolved oxygen area, and the dissolved oxygen concentration of the second-stage dissolved oxygen area is slightly lower than that of the first-stage dissolved oxygen area.
The toxic organic wastewater enters the tank body from the water inlet through the water pump and the flowmeter, the gas-liquid-solid mixed flow rises from the bottom under the disturbance of the gas entering by the gas pump and the gas distributor, most of the gas-liquid-solid flows back to the outer cylinder area under the mixed action of the guide cylinder, the first guide plate and the water pressure, the efficient aerobic reaction is continuously carried out in the area, meanwhile, the liquid and the solid enter the carrier area through the screen, the dissolved oxygen concentration of the carrier area is gradually reduced from outside to inside, and the anaerobic area is formed. Some of the gas flows to the three-phase separation area, but flows back and falls under the action of the first guide plate, and a part of the gas entrains liquid and sludge to escape from the first guide holes, and the falling gas-liquid flow and sludge are mixed with the inlet water again to circulate the process, so that the first guide plate is designed to enable the reaction to be more sufficient, and the oxygen utilization rate is higher. The gas-liquid and sludge escaping from the first diversion holes are pushed to rise in the second-stage dissolved oxygen area, and the gas escapes at the open interface inside the second diversion plate. The rest solid and liquid enter the outer side area of the second guide plate through the second guide holes and settle down, and the area is a sludge settling area. Finally, the wastewater flows out from the water outlet through the overflow weir.
In this process, the degree of wastewater mixing is determined from the flow field. The flow velocity is the fastest in the first-stage dissolved oxygen area, the flow velocity in other areas is basically consistent, and the mixing degree in the first-stage dissolved oxygen area is high; the suspended carrier in the anaerobic zone is in a limited moving state under the drive of the ascending gas-liquid flow, and the liquid phase flow rate in the zone is stable and the mixing degree is high under the proper carrier loading capacity; in the second-stage dissolved oxygen area, the wastewater is in a circulating flow state under the disturbance of the escaping airflow, the liquid phase flow velocity in the area is relatively smaller, but the velocity field is uniformly distributed, and the mixing degree is high; in the sludge settling zone, the flow velocity in the zone is extremely low due to the action of the second guide plate, liquid escapes from the overflow port under the action of push flow, the liquid mixing degree is low, and the effluent quality is good. According to the biological theory of wastewater treatment, the longer the residence time of the wastewater, the higher the biological treatment degree and the better the water quality, and the average residence time of the wastewater in the tank body is that the size of the wastewater in the overflow weir is that the wastewater is that the sludge sedimentation area is that the secondary dissolved oxygen area is that the anaerobic area is that the primary dissolved oxygen area is. The invention not only ensures that the reactor has good mixing effect to improve the biological treatment efficiency, but also improves the waste water separation effect, so that the effluent quality is the best part in the reactor.
A water quality monitor is arranged in the sludge sedimentation zone, a temperature sensor and a pH sensor are arranged in the water quality monitor, and a dissolved oxygen microelectrode is arranged in the biological film zone.
A simplified simulation model is built based on COMSOL, the model ignores an anaerobic zone part, influences of two flow guide plates on a three-phase flow field are studied, and flow velocity distribution conditions in the tank body are obtained, as shown in figure 4. The color gradient from dark to light in fig. 4 represents the flow rate of the liquid phase from the minimum value to the maximum value.
The division of the dissolved oxygen area in the tank body is shown in fig. 5, and fig. 5 is a result obtained by performing gas phase distribution simulation on the basis of fig. 4. The color in the legend changes from dark to light, representing the dissolved oxygen concentration from 0 to the maximum. The dissolved oxygen concentration is positively correlated with the liquid phase flow field, and is uniformly distributed in a first-stage dissolved oxygen area, wherein the dissolved oxygen concentration is the largest in the area, and the average dissolved oxygen concentration is actually measured to be 4.6mg.L < -1 >. In the secondary dissolved oxygen zone, the average dissolved oxygen concentration was actually measured to be 3.3 mg.L-1. In the anaerobic zone, the dissolved oxygen concentration in this zone is always at a lower level.
As the screen is of a hollow cylinder structure, the side surface of the screen is used as a reference surface of depth, the direction of the central axis of the screen is the positive direction of depth increase, the relation between the dissolved oxygen concentration in the anaerobic zone and the depth is measured by using a dissolved oxygen microelectrode, as shown in figure 6, the dissolved oxygen concentration rapidly decreases along with the depth increase, and the dissolved oxygen concentration is as low as 0+/-s 0.02 mg.L < -1 > in the depth of the anaerobic zone.
Taking coking wastewater as an example, the treatment effect of the mixed fluidized bed reactor (a) and the conventional fluidized bed reactor (b) of the present example in stable operation was compared under the condition of 0.05kg COD/(m3.d), and the measured data are shown in Table 1 and FIGS. 7 to 9.
As can be seen from FIG. 7, after the anaerobic zone occupies a certain volume of the aerobic treatment zone, the COD treatment effect of the mixed fluidized bed reactor is still consistent with that of the traditional fluidized bed reactor, and the COD removal rate can reach 86.9%.
From fig. 8 to fig. 9, it can be seen that SCN-, ammonia nitrogen and total nitrogen can be effectively removed at the same time by the mixed fluidized bed reactor, and high-concentration toxic organic matters are degraded under aerobic or anaerobic conditions, so that the toxicity inhibition of biological denitrification is relieved, the nitrification efficiency is improved, and the ammonia nitrogen degradation efficiency is high in the same reactor. The traditional fluidized bed can degrade COD and partial toxic substances, but the toxic substances cannot be completely degraded, the nitrification reaction is inhibited, ammonia nitrogen cannot be completely degraded (the average ammonia nitrogen concentration of effluent is 30 mg.L < -1 >), the traditional fluidized bed reactor is in an aerobic environment, the denitrification process is difficult to carry out, and the total nitrogen cannot be removed (the average total nitrogen concentration of the effluent is 188 mg.L < -1 >)
TABLE 1
The above examples are preferred embodiments of the present invention, but the embodiments of the present invention are not limited to the above examples, and any other changes, modifications, substitutions, combinations, and simplifications that do not depart from the spirit and principle of the present invention should be made in the equivalent manner, and the embodiments are included in the protection scope of the present invention.
Claims (8)
1. A mixed fluidized bed reactor, characterized by: the novel water tank comprises a tank body, a filling part, a first guide plate and a second guide plate, wherein a water inlet and a water outlet are formed in the tank body, the water inlet is formed in the bottom end of the tank body, the water outlet is formed in the side face of the tank body, the filling part is arranged above the water inlet, the first guide plate is arranged above the filling part, the second guide plate is arranged above the first guide plate, the lower end of the second guide plate is arranged in the tank body, and the upper end of the second guide plate is higher than the water outlet; the packing component comprises a screen and a guide cylinder, the screen and the guide cylinder are of hollow columnar structures, the guide cylinder is positioned in the screen, an annular containing cavity is formed between the screen and the guide cylinder, and a carrier is arranged in the annular containing cavity; the first guide plate is of a cambered surface structure with a downward concave surface, and a first guide hole is formed in the first guide plate; the second guide plate is internally provided with a guide channel which is communicated with the upper area and the lower area of the second guide plate, the side surface of the second guide plate is provided with a second guide hole, and the second guide hole is communicated with the guide channel and the outer side of the second guide plate;
the flow guide channel comprises a flow guide section, a gas collecting section and an outlet section which are sequentially connected, the flow guide section and the outlet section are of cylindrical structures, the diameter of the flow guide section is larger than that of the outlet section, and the gas collecting section is of a circular truncated cone structure;
the tank body is provided with an overflow weir, and the water outlet is arranged at the outer side of the overflow weir.
2. A mixed fluidized bed reactor according to claim 1, characterized in that: still include hangers, fixed block, hangers and first guide plate fixed connection, fixed block and jar body fixed connection are equipped with the draw-in groove on the fixed block, and hangers detachably card is gone into in the draw-in groove.
3. A mixed fluidized bed reactor according to claim 2, characterized in that: the quantity of fixed blocks is the multiunit, and multiunit fixed block is in different altitudes respectively.
4. A mixed fluidized bed reactor according to claim 1, characterized in that: the first guide plate is a hemispherical plate, and the ratio of the outer diameter of the first guide plate to the inner diameter of the tank body is 0.6-0.9.
5. A mixed fluidized bed reactor according to claim 1, characterized in that: the carrier is a suspension carrier.
6. A mixed fluidized bed reactor according to claim 1, characterized in that: the number of the first diversion holes is multiple, and the first diversion holes are distributed in an annular array.
7. A mixed fluidized bed reactor according to claim 1, characterized in that: the air pump is connected with the gas distributor through an air inlet pipeline.
8. Use of a mixed fluidized bed reactor, characterized in that: a mixed fluidized bed reactor according to any one of claims 1 to 7 for use in the treatment of toxic organic waste water.
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