CN114180723B - Enhanced aeration aerobic biological fluidized bed sewage treatment process and device - Google Patents
Enhanced aeration aerobic biological fluidized bed sewage treatment process and device Download PDFInfo
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Abstract
The invention provides a sewage treatment process and a sewage treatment device of an aerobic biological fluidized bed for strengthening aeration, wherein sewage is treated by an anoxic biological reactor and then is introduced into the bottom of the aerobic biological fluidized bed, a micro-bubble aerator, a first inner cylinder, a second aerator and a second inner cylinder are sequentially arranged in the aerobic biological fluidized bed from bottom to top, the micro-bubble aerator and the second aerator respectively generate micro-bubbles and macro-bubbles, the sewage flows upwards in the first inner cylinder under the action of the micro-bubbles, and the rise of the bubbles and the aggregation and removal of the micro-bubbles are accelerated under the action of the macro-bubbles when reaching the second inner cylinder; a part of sewage reaching the top of the fluidized bed flows back to the bottom along the gap to form circulating flow; a part of the waste water is returned to the anoxic bioreactor; the sewage quantity and the exhaust quantity of the reflux anoxic bioreactor are controlled in a linkage way through a liquid level meter. The invention not only can improve the sewage treatment effect of the system and save a great amount of energy consumption and occupied area, but also can flexibly treat the sewage quantity and reduce manual regulation.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to an aerobic biological fluidized bed sewage treatment process and device for strengthening aeration.
Background
Along with the development of urban scale and continuous improvement of industrialization degree in China, a large amount of industrial sewage and domestic sewage which are difficult to treat are generated, the sewage treatment plant faces serious challenges, and particularly, the field of industrial sewage treatment has large sewage discharge, complex water quality, high toxicity and higher nitrogen, ammonia and COD. The current common sewage biological treatment processes comprise an activated sludge method, a suspended filler biomembrane method, a biological filter and the like. The sewage which can be treated by the activated sludge method requires low sludge concentration, cannot treat high-load sewage, and has the advantages of easy expansion of the sludge, large occupied area, large requirement for large-scale precipitation equipment and large residual sludge quantity. The suspended filler biomembrane process is to add a certain amount of filler with density close to that of water into the reactor, provide habitat for the growth of microorganisms, and improve biomass and biological species in the reactor, thereby improving the treatment efficiency of the reactor. The suspended filler biomembrane process has the characteristics of high treatment efficiency, simple operation and the like. But treated with only suspended fillers, the effluent contains higher concentrations of particulate matter and suspended matter, resulting in higher turbidity. In the traditional sand filtration treatment process, because the density of sand stone and other fillers is high, the relative filling rate is low, and the effective utilization rate of the reactor is correspondingly reduced; meanwhile, blockage is easy to cause in the process of process operation, which is unfavorable for the process operation.
The aerobic biological fluidized bed reactor has large height-diameter ratio, small occupied area, high sewage treatment efficiency, strong impact resistance, short residence time and wide application prospect, and is in a high-speed internal circulation state. However, the single aerobic biological fluidized bed process is difficult to degrade macromolecular organic matters, especially industrial sewage is difficult to discharge after reaching standards, and industrial sewage is usually required to be treated by connecting an anoxic sewage treatment process with an aerobic biological fluidized bed in series.
Meanwhile, the aeration stage has the problems of uneven aeration and overhigh aeration energy consumption. The energy consumption, oxygenation capacity, oxygen utilization rate and sludge suspension degree of the aeration equipment are main parameters of aeration performance. At present, in the process of treating sewage by an aerobic biological method, the size of bubbles generated by aeration is large, the rising speed of the bubbles in the sewage is high, the residence time is short, the aeration quantity is required to be increased to maintain the dissolved oxygen content of the sewage, so that the energy consumption of aeration equipment is high, the oxygenation capacity and the oxygen utilization rate are low, sludge precipitation is caused when the aeration quantity is reduced, the sewage treatment rate is reduced, and the like.
CN20081013608. X discloses a combined type aerobic biological fluidized bed sewage treatment device, which comprises a plurality of aerobic biological fluidized beds connected in parallel, wherein the fluidized beds adopt standardized boxes and can be assembled at will to build different treatment systems, thereby being beneficial to reducing cost and simplifying installation; the fluidized bed comprises a uniform orifice plate and a bubble cap water distribution plate positioned above the uniform orifice plate, a space is reserved between the uniform orifice plate and the bubble cap water distribution plate, and solid fine particles serving as a biological film carrier are arranged on the bubble cap water distribution plate. The treatment device only comprises an aerobic biochemical treatment device, has large occupied area and multiple interfaces, is an independent aerobic biological fluidized bed process, is difficult to degrade macromolecular organic matters, particularly treats industrial sewage, and is difficult to discharge after reaching standards.
Disclosure of Invention
In order to solve the defects in the prior art, the invention provides an aerobic biological fluidized bed sewage treatment process and device for strengthening aeration, which adopt the combination of micro-bubbles and macro-bubbles to strengthen aeration, improve the sewage treatment efficiency and save a large amount of energy consumption and occupied area.
In order to achieve the above purpose, the invention adopts the following technical scheme:
an enhanced aeration aerobic biological fluidized bed sewage treatment process adopts an anoxic biological reactor and an aerobic biological fluidized bed to treat sewage, the sewage is treated by the anoxic biological reactor and then is introduced into the bottom of the aerobic biological fluidized bed, a micro-bubble aerator, a first inner cylinder, a second aerator and a second inner cylinder are sequentially arranged in the aerobic biological fluidized bed from bottom to top, an air source is respectively aerated by the micro-bubble aerator and the second aerator to respectively generate micro-bubbles and macro-bubbles, the sewage introduced into the fluidized bed flows upwards in the first inner cylinder under the action of the micro-bubbles and enhances the reaction, the reaction is further enhanced under the action of the macro-bubbles in the second inner cylinder, and the rising of the bubbles and the coalescence of the micro-bubbles are accelerated;
part of sewage reaching the top of the aerobic biological fluidized bed flows back to the bottom along a gap outside the first inner cylinder and the second inner cylinder and circulates into the first inner cylinder to form circulating flow; a part of sewage flows back to the anoxic bioreactor; the waste gas generated by the reaction is discharged from the top;
the top of the aerobic biological fluidized bed is provided with a liquid level meter, the sewage quantity and the waste gas discharge quantity of the reflux anoxic bioreactor are controlled in a linkage way, the pressure of the top of the aerobic biological fluidized bed is regulated and controlled, and the normal water outlet is ensured;
and the sewage treated by the aerobic biological fluidized bed is discharged from the top of the aerobic biological fluidized bed.
The invention is further arranged that the gas-liquid phase feeding volume ratio of the micro-bubble aerator is (0.3-1): 1, a step of; the average diameter of the micro-bubbles is 50-150 mu m, the rising speed of the micro-bubbles is 0.005-0.009m/s, the oxygen power efficiency is 4-5 kg/(kW.h), the average diameter of the macro-bubbles is 2-20mm, and the hydraulic retention time of the aerobic biological fluidized bed is 4-8 hours.
The invention is further arranged that a reflux valve and an exhaust valve for regulating and controlling the sewage quantity and the exhaust gas discharge quantity of the reflux anoxic bioreactor are arranged at the top of the aerobic biological fluidized bed, the water inlet rate at the bottom of the aerobic biological fluidized bed is kept constant, when the liquid level is too high, the reflux valve is increased, the reflux quantity of the reflux anoxic reaction is increased, the exhaust valve is closed, the pressure is increased, the annular gap liquid circulation rate is improved, and the water outlet is ensured; when the liquid level is too low, the reflux valve is reduced, the reflux quantity of the reflux anoxic reaction is reduced, the exhaust valve is opened, the internal pressure of the fluidized bed is reduced, and the circulation rate of the annular space liquid of the inner cylinder and the outer cylinder is reduced.
The invention is further arranged that the volume ratio of the annular space sewage reflux quantity to the sewage reflux quantity flowing back to the anoxic bioreactor is (2-4): 1; the pressure range of the top of the aerobic biological fluidized bed is 0.2-0.35MPa; the oxygen content in the sewage of the reflux anoxic bioreactor at the top of the aerobic biological fluidized bed is 0.2-0.5mg/L.
The invention is further arranged that the sludge concentration in the aerobic biological fluidized bed is 3-5g/L, and the COD and NH in the aerobic biological fluidized bed 3 -the ratio of N to total P is (100-150): (4-6): 1, the volume load of the aerobic biological fluidized bed is 2-6 kgCOD/(m) 3 ·d)。
The invention is further arranged that a part of sludge after solid-liquid separation of sewage discharged by the aerobic biological fluidized bed is sent back to the anoxic bioreactor, and the rest is sent to a sludge treatment system for treatment; or a part of the sludge is sent back to the anoxic bioreactor, a part of the sludge is sent back to the aerobic biological fluidized bed, and the rest of the sludge is sent to a sludge treatment system for treatment; the sludge reflux ratio of the aerobic biological fluidized bed is (0-0.6): 1.
the invention also provides an aerobic biological fluidized bed sewage treatment device for strengthening aeration, which comprises an anoxic biological reactor and an aerobic biological fluidized bed, wherein the aerobic biological fluidized bed comprises an outer cylinder, a first inner cylinder and a second inner cylinder are arranged in the outer cylinder from bottom to top, a micro-bubble aerator is arranged at the lower end of the first inner cylinder, and a second aerator is arranged between the second inner cylinder and the first inner cylinder and is used for generating a large number of micro-bubbles and macro-bubbles respectively;
the bottom of the outer cylinder is provided with a first gas phase inlet and a sewage inlet which are respectively communicated with the gas-liquid phase inlet of the micro-bubble aerator, the sewage inlet is communicated with the anoxic bioreactor, and the side wall of the outer cylinder is provided with a second gas phase inlet which is communicated with the second aerator;
the top of the outer cylinder is provided with a reflux outlet, an exhaust gas outlet and a drainage outlet which are respectively used for refluxing part of sewage at the top of the outer cylinder to the anoxic bioreactor, and discharging the exhaust gas at the top and the treated sewage;
the top of the outer cylinder is provided with a liquid level meter which is used for controlling a reflux valve and an exhaust valve which are respectively connected with the reflux outlet and the exhaust outlet in a linkage way.
The invention further provides that the sewage treatment device further comprises an exhaust gas treatment system, a mud-water separator and a sludge treatment system, wherein the exhaust gas treatment system is used for collecting and treating the exhaust gas generated by the anoxic bioreactor and the aerobic biological fluidized bed; the mud-water separator is connected with the drainage outlet and is used for solid-liquid separating the sewage treated by the aerobic biological fluidized bed; the sludge treatment system is connected with a sludge outlet of the sludge-water separator, and the sludge outlet is connected with the anoxic bioreactor and the aerobic biological fluidized bed.
The invention is further arranged that the lower end of the first inner cylinder comprises a plurality of micro-bubble aerators which are uniformly distributed around the axis along the circumference and are obliquely arranged along the tangential direction, the oblique directions are consistent, and the oblique angle alpha of the micro-bubble aerators is 10 degrees to 40 degrees.
The invention is further arranged that the micro-bubble aerator generates a large number of micro-bubbles through liquid phase rotational flow shearing, the side wall of the micro-bubble aerator is provided with a liquid phase tangential inlet, the bottom end of the micro-bubble aerator is provided with a gas phase axial inlet, a mixing cavity which is communicated with the liquid phase tangential inlet and the gas phase axial inlet is arranged in the micro-bubble aerator, an air inlet throat is arranged between the gas phase axial inlet and the mixing cavity, the upper end of the mixing cavity is provided with a throat outlet, and the throat outlet is connected with a spiral shearing blade.
The invention is further arranged that the height-to-diameter ratio of the mixing cavity is (2-4): 1, a step of; the ratio of the diameter of the air inlet throat to the diameter of the mixing chamber is (0.05-0.3): 1, a step of; the helix angle beta of the helical shear blade is 20-50 degrees.
The invention is further characterized in that a plurality of second aerators are arranged between the second inner cylinder and the first inner cylinder, and the second aerators are rod-shaped aerators with upward aeration holes and are suspended in the second inner cylinder.
The invention is further arranged that the diameters and the lengths of the first inner cylinder and the second inner cylinder are equal, and the ratio of the space between the two inner cylinders to the diameter of the inner cylinder is (0.3-0.6): 1, the ratio of the total height of the two inner cylinders to the height of the aerobic biological fluidized bed is (0.65-0.8): 1, the ratio of the sectional area of the inner cylinder to the annular space area between the inner cylinder and the outer cylinder is 1:1.
the invention has the beneficial effects that:
(1) The invention adopts the aerobic biological fluidized bed reactor, has small occupied area and short hydraulic retention time, and the untreated macromolecular organic matters are hydrolyzed and acidified again into small molecular organic matters by refluxing part of sewage in the aerobic biological fluidized bed to the anoxic biological reactor, so that the sewage treatment effect of the system is improved, the exhaust valve and the reflux valve of the aerobic biological fluidized bed are controlled in a linkage way through the liquid level meter, the sewage reflux quantity and the top pressure are automatically controlled, the self-adaptive treatment of sewage is realized, and the manual regulation is reduced.
(2) The invention utilizes the combination of the obliquely arranged micro-bubble aerator and the suspended rod type aerator to respectively generate a large number of micro-bubbles and large-bubbles, controls the rising speed of the bubbles in the sewage by controlling the size of the micro-bubbles, increases the residence time of the bubbles in the sewage, improves the dissolved oxygen in the sewage, increases the capacity of the aerobic organisms for obtaining oxygen by huge gas-liquid contact area, and increases the rising speed of the micro-bubbles by rotational flow, thereby enhancing the diffusion speed of the micro-bubbles; the rod type aerator swings freely along with aeration, so that the aeration uniformity is improved, the generated large bubbles can not only increase turbulence and enhance mass transfer, but also accelerate coalescence and rising of micro bubbles, reduce the oxygen content of sewage flowing back to the anoxic bioreactor from the top, and meet the anoxic requirement of anoxic reaction.
(3) The aerobic biological fluidized bed forms circulating flow around the inner cylinder, the circulating flow speed is larger than the settling speed of the carrier terminal, the aerator is not easy to be blocked by settled sludge, and the service life is prolonged.
Drawings
FIG. 1 is a process flow diagram of a wastewater treatment process according to the present invention;
FIG. 2 is a schematic structural view of an aerobic biological fluidized bed according to the present invention;
FIG. 3 is a cross-sectional view of the B-B plane of FIG. 1;
FIG. 4 is a schematic view showing the installation angle of the micro-bubble aerator according to the present invention;
FIG. 5 is a schematic view showing the structure of a fine bubble aerator according to the present invention;
FIG. 6 is a schematic view of the structure of a spiral shear blade of the fine bubble aerator according to the present invention;
FIG. 7 is a cross-sectional view taken along the A-A plane in FIG. 1.
Wherein, 1-anoxic bioreactor, 2-booster pump, 3-heat exchanger, 4-air blower, 5-aerobe fluidized bed, 6-sewage inlet, 7-first gas phase inlet, 8-second gas phase inlet, 9-reflux outlet, 10-waste gas outlet, 11-drainage outlet, 12-liquid level meter, 13-mud-water separator, 14-water phase outlet, 15-sludge treatment system, 16-sludge pump, 17-waste gas treatment system, 18-discharge valve, 19-reflux valve.
Detailed Description
The present invention is described in further detail below with reference to examples. It is to be understood that the following examples are given solely for the purpose of illustration and are not to be construed as limitations upon the scope of the invention, as will be apparent to those skilled in the art upon examination of the following, of various non-essential modifications and adaptations of the invention.
Example 1
The invention provides an enhanced aeration aerobic biological fluidized bed sewage treatment process and device, wherein the process flow chart is shown in figure 1, and sewage is treated by utilizing an aerobic biological fluidized bed device and an anoxic biological sewage treatment device in series.
The sewage treatment device comprises an anoxic bioreactor 1, an aerobic biological fluidized bed 5, a mud-water separator 13, a sludge treatment system 15 and an exhaust gas treatment system 17, raw sewage is acidified and hydrolyzed by the anoxic bioreactor 1, macromolecular organic matters in the sewage are decomposed into micromolecular organic matters, sewage after anoxic reaction treatment is introduced into the bottom of the aerobic biological fluidized bed 5 after passing through a booster pump 2 and a heat exchanger 3, and exhaust gas generated by reaction is introduced into the exhaust gas treatment system 17.
Referring to fig. 2, the aerobic biological fluidized bed 5 includes an outer cylinder 50, a first inner cylinder 51 and a second inner cylinder 52 are sequentially disposed in the outer cylinder 50 from bottom to top, a micro-bubble aerator 53 is disposed at the lower end of the first inner cylinder 51, and a second aerator 54 is disposed between the second inner cylinder 52 and the first inner cylinder 51, and is used for generating a large number of micro-bubbles and macro-bubbles respectively; the bottom of the outer cylinder 50 is provided with a first gas phase inlet 7 and a sewage inlet 6 which are respectively communicated with the gas-liquid phase inlet of the micro-bubble aerator 53, the side wall of the outer cylinder 50 is provided with a second gas phase inlet 8 which is communicated with the second aerator 54, the gas source of the fluidized bed 5 is respectively supplied through the first gas phase inlet 7 and the second gas phase inlet 8 by a blower 4, and sewage from the anoxic bioreactor 1 is introduced from the sewage inlet 6; the sewage introduced into the fluidized bed 5 flows upwards in the first inner cylinder 51 under the lifting action of a large number of micro bubbles to strengthen the reaction, reaches the second inner cylinder 52 to further strengthen the reaction under the action of the macro bubbles, and accelerates the rising of the bubbles and the coalescence and removal of the micro bubbles; the top of the outer cylinder 50 is provided with a reflux outlet 9, an exhaust outlet 10 and a drainage outlet 11, the exhaust is discharged from the exhaust outlet 10 into the exhaust treatment system 17, and part of sewage reaching the top of the fluidized bed 5 flows back to the bottom of the fluidized bed 5 from an annular gap between the inner cylinder and the outer cylinder and circulates into the first inner cylinder 51 due to the density difference between the inner cylinder and the outer cylinder of the first inner cylinder 51 and the second inner cylinder 52 to form circulating flow; part of sewage is returned to the anoxic bioreactor 1 again from the return outlet 9, a liquid level meter 12 is arranged at the top of the outer barrel 50, the return outlet 9 and the waste gas outlet 10 are respectively connected with a return valve 19 and an exhaust valve 18 for controlling the return flow and the exhaust flow, the valve opening is controlled in a linkage way through the liquid level meter 12, the sewage amount of the backflow anoxic bioreactor 1 is regulated and controlled, and the proper pressure at the top of the fluidized bed is kept to ensure the normal water outlet.
The sewage treated by the aerobic biological fluidized bed 5 is discharged from the water outlet 11 and enters the mud-water separator 13, the water phase after solid-liquid separation is discharged from the water phase outlet 14 of the mud-water separator 13, the sludge is discharged from the sludge outlet 20 at the lower part of the mud-water separator 13, part of the sludge is returned to the anoxic biological reactor 1 through the sludge pump 16, the rest is sent to the sludge treatment system 15 for treatment, or part of the sludge is sent back to the anoxic biological reactor 1, part of the sludge is sent back to the aerobic biological fluidized bed 5, and the rest is sent to the sludge treatment system 15 for treatment.
The anoxic bioreactor 1, the mud-water separator 13 and the waste gas treatment system 17 are all conventional technologies in the sewage treatment field, for example, the anoxic bioreactor is used for acidizing and hydrolyzing sewage under the anoxic condition, the mud-water separator is used for separating mud water through a cyclone separation mode or a natural sedimentation mode and the like, and the waste gas treatment system is used for treating waste gas generated by waste water treatment through adsorption, membrane separation and the like.
Furthermore, the heat exchanger 3 is used for maintaining the sewage temperature at 20-30 ℃, and the heat exchanger is used for controlling the sewage temperature at the most appropriate temperature condition of aerobic bacteria, so that the activity and the reaction rate of the aerobic bacteria are improved, and good effluent quality is obtained.
Further, as shown in fig. 3 and 4, the lower end of the first inner cylinder 51 is provided with a plurality of micro-bubble aerators 53, the micro-bubble aerators 53 are uniformly distributed along the circumference around the axis, are obliquely arranged along the tangential direction, and are uniformly inclined in the clockwise or counterclockwise direction, and the inclination angle α of the micro-bubble aerators 53 is 10 ° -40 °, preferably 20 °, so that the micro-bubbles and the sewage mixed solution generated by the micro-bubble aerators 53 generate rotational flow around the inner walls of the first inner cylinder 51 and the second inner cylinder 52, and the diffusion speed of the micro-bubbles is enhanced.
Further, a micro-bubble aerator 53 is disposed at the axis of the lower end of the first inner cylinder 51, and the micro-bubble aerator 53 is disposed vertically and upwardly, and generates a large number of micro-bubbles together with the micro-bubble aerators 53 distributed along the circumference.
Further, the micro-bubble aerator 53 generates a large number of micro-bubbles by liquid phase rotational flow shearing, as shown in fig. 5, a liquid phase tangential inlet 531 is provided on a side wall of the micro-bubble aerator 53, a gas phase axial inlet 532 is provided at a bottom end of the micro-bubble aerator 53, a mixing cavity 533 is provided in the micro-bubble aerator 53, which communicates with the liquid phase tangential inlet 531 and the gas phase axial inlet 532, an air inlet throat 534 is provided between the gas phase axial inlet 532 and the mixing cavity 533, a throat outlet 535 is provided at an upper end of the mixing cavity 533, and the throat outlet 535 is connected with the spiral shearing blade 536. The sewage enters the mixing cavity 533 from the liquid phase tangential inlet 531 to form a rotational flow, the gas is introduced from the gas phase axial inlet 532 and compressed by the air inlet throat 534 to enter the mixing cavity 533, a large amount of micro bubbles are generated under the action of liquid phase rotational flow shearing, and the gas-liquid mixed liquid containing a large amount of micro bubbles is compressed and discharged from the throat outlet 535 and further sheared by the rotational flow of the spiral shearing blade 536 to enter the first inner cylinder 51.
Further, the ratio of the height to the diameter of the mixing chamber 533, i.e., the ratio of the height to the diameter of the mixing chamber is (2-4): 1, preferably 2.8:1, a step of; the ratio of the diameter of the air inlet throat 534 to the diameter of the mixing chamber 533 is 0.05-0.3, preferably 0.1; as shown in FIG. 6, the helical angle β of the helical shear blade 536 is 20 ° -50 °, preferably 30 °; the gas-liquid phase feeding volume ratio of the micro-bubble aerator 53 is (0.3-1): 1.
further, as shown in fig. 7, a plurality of second aerators 54 are disposed between the second inner cylinder 52 and the first inner cylinder 51, the second aerators 54 are rod-shaped aerators with upward openings of the aeration holes 541, and are suspended in the second inner cylinder 52 to generate bubbles with larger size, so as to freely swing along with the aeration process, enhance the aeration uniformity, and the swing of the second aerators does not interfere with each other. Preferably, the second aerator 54 is suspended in the inner drum by a flexible wire.
Further, the diameters and lengths of the first inner cylinder 51 and the second inner cylinder 52 are equal, and the ratio of the space between the two inner cylinders to the diameter of the inner cylinder is (0.3-0.6): 1, the ratio of the total height of the two inner cylinders to the height of the aerobic biological fluidized bed 5 is (0.65-0.8): 1, and the ratio of the sectional area of the inner cylinder to the annular space area between the inner cylinder and the outer cylinder is 1:1.
further, the first inner cylinder 51 and the second inner cylinder 52 are fixed in the aerobic biological fluidized bed 5, and the shaking caused by the turbulence of bubbles is prevented by axial fixation and circumferential fixation, and preferably, the materials of the first inner cylinder 51 and the second inner cylinder 52 can be acrylic glass or stainless steel.
Further, the blower 4 provides air source feeding for the micro-bubble aerator 53 and the second aerator 54, the micro-bubble aerator 53 below generates micro-bubble groups, the average diameter of the micro-bubbles is 50-150 μm, and the micro-bubble groups can generate gas-liquid mixed liquid rising around the inner wall of the first inner cylinder 51 in a rotational flow way due to the inclined installation of the aerators, so that the contact probability of the gas-liquid-solid three phases is improved, and the aerobic bacteria can more easily absorb oxygen; when reaching the second inner cylinder 52 above, the second aerator 54, namely an aeration rod, generates large bubbles with the average diameter of 2-20mm, and the aeration rod swings back and forth under the reaction force of the gas to generate turbulence, so that aeration is more uniform, and the mixing effect is enhanced; the mixed liquid outside the first inner cylinder 51 and the second inner cylinder 52 flows back to the bottom of the fluidized bed 5 along an annular gap between the inner cylinder and the outer cylinder under the action of density difference due to low air content, and enters the inner cylinder again when reaching the bottom, so that the circulating flow taking the first inner cylinder 51 and the second inner cylinder 52 as the center is formed, the turbulence degree and the mixing effect of the whole fluidized bed are increased, the circulating flow velocity is larger than the settling velocity of a carrier terminal, the aerator is not easy to be blocked by settled sludge, and the service life is prolonged.
Further, the rising speed of micro-bubbles in the aerobic biological fluidized bed 5 is 0.005-0.009m/s, the oxygen power efficiency is 4-5 kg/(kW.h), the hydraulic retention time is 4-8 hours, the rising speed of bubbles in sewage is controlled by reducing the size of bubbles in the aerobic biological fluidized bed 5, the retention time of bubbles in the sewage is increased, the dissolved oxygen in the sewage is increased, the aeration distribution is uniform, the capacity of oxygen acquisition of aerobic organisms is increased by a huge gas-liquid contact area, the reaction efficiency is improved, the blast volume is reduced, and the energy consumption is saved.
Furthermore, a part of macromolecule organic matters which are not hydrolyzed and acidified by the anoxic reaction still remain in the sewage which is reacted by the aerobic biological fluidized bed 5, and the aerobic bacteria in the aerobic biological fluidized bed 5 can not take the macromolecule organic matters for metabolic reaction, and the sewage needs to be returned to the anoxic biological reactor 1 again for hydrolysis, acidification and decomposition into micromolecule organic matters, thereby being beneficial to complete taking reaction of the aerobic organisms and improving the drainage quality. Further, the volume ratio of the sewage reflux quantity of the inner and outer cylinder annular gaps to the sewage reflux quantity flowing back to the anoxic bioreactor is (2-4): 1.
Meanwhile, the large bubbles generated by the aeration rod in the second inner cylinder 52 can accelerate coalescence and rising of micro bubbles, reduce the oxygen content of sewage flowing back to the anoxic bioreactor 1 at the top of the aerobic biological fluidized bed 5, and reach the anoxic requirement of anoxic reaction by 0.2-0.5mg/L, and prevent the influence on the bacterial activity of the anoxic reaction.
Further, the liquid level meter 12 controls the reflux valve 19 and the exhaust valve 18 in a linkage way, regulates and controls the sewage amount of the reflux anoxic bioreactor 1, keeps proper pressure at the top of the fluidized bed to ensure that the water is discharged normally, specifically, the water inlet rate at the bottom of the aerobic biological fluidized bed 5 is kept constant, when the liquid level is too high, the reflux valve 19 is increased, the reflux amount of the reflux anoxic reaction is increased, the exhaust valve 18 is closed, the pressure is increased, the circulation rate of the annular gap liquid of the inner cylinder and the outer cylinder is increased, and the water discharge is ensured; when the liquid level is too low, the reflux valve 19 is reduced, the reflux amount of the reflux anoxic reaction is reduced, the exhaust valve 18 is opened, the internal pressure of the fluidized bed is reduced, and the circulation rate of the annular space liquid of the inner cylinder and the outer cylinder is reduced.
Further, the pressure at the top of the aerobic biological fluidized bed 5 is in the range of 0.2-0.35MPa.
Further, the sludge reflux ratio of the aerobic biological fluidized bed 5 is (0-0.6): 1, wherein the sludge reflux ratio refers to the volume ratio of the sludge reflux amount to the water inflow of the device, the sludge reflux amount refers to the sludge amount flowing back to the bottom of the aerobic biological fluidized bed 5, and the water inflow of the device refers to the sewage amount entering the aerobic biological fluidized bed 5.
Further, the sludge concentration of the aerobic biological fluidized bed 5 is 3-5g/L, and COD and NH in the aerobic biological fluidized bed 5 3 -the ratio of N to total P is (100-150): (4-6): 1, the volume load of the aerobic biological fluidized bed 5 is 2-6 kgCOD/(m) 3 ·d)。
Example 2
The aerobic biological fluidized bed sewage treatment process and the device in the embodiment 1 are adopted to treat certain petrochemical comprehensive sewage.
The pH value of the inlet water of the sewage is 7.0, the CODcr is 670mg/L, and the SS is 170mg/L. 2g/L of activated sludge is added into the aerobic biological fluidized bed, and the culture of the strain is carried out for 2 days, so that the biological concentration in the fluidized bed is measured to be 6g/L.
The aeration amount of the aerobic biological fluidized bed is 2m 3 And/h, wherein the total aeration rate of the micro-bubble generator is 1.2m 3 And/h, the aeration rate of the second aerator is 0.8m 3 And/h. The hydraulic retention time in the aerobic biological fluidized bed is 5 hours, and the oxygen content of sewage flowing back to the anoxic bioreactor is in the range of 0.2-0.5mg/L.
After the treatment by the process, the water quality of the obtained water is measured as follows: CODcr of 78mg/L, SS of 7mg/L and pH of 7.2; CODcr volume load was 3.6 COD/(m) 3 D), CODcr removal of 88.4% and SS removal of 95.8%.
Comparative example 2
The aerobic biological fluidized bed sewage treatment process and the device in the embodiment 1 are adopted to treat certain petrochemical comprehensive sewage.
The water quality condition of the inlet water and the sewage treatment process and the device are the same as those of the embodiment 2, and the difference is that: the second aerator is not arranged in the aerobic biological fluidized bed, and only the micro-bubble aerator is arranged.
As no large bubbles promote the coalescence and removal of micro bubbles in the aerobic biological fluidized bed, the oxygen content of the sewage reaching the top of the aerobic biological fluidized bed is still kept high and is about 0.8-1.5 mg/L, so that the oxygen content of the sewage flowing back to the anoxic biological reactor does not meet the condition of low oxygen content.
After the treatment by the process, the water quality of the effluent is finally measured as follows: CODcr is 120mg/L, SS is 9mg/L, and pH value is 7.2; CODcr volume load was 3.0 COD/(m) 3 D) CODcr removal of 82.1% and SS removal of 94.7%.
Example 3
The aerobic biological fluidized bed sewage treatment process and the device in the embodiment 1 are adopted to treat certain coal glycol wastewater.
The water inflow average CODcr of the wastewater is 730mg/L, NH 3 N is 62mg/L and TN is 237mg/L. The aeration quantity of the aerobic biological fluidized bed is 5m 3 And/h, wherein the total aeration rate of the micro-bubble generator is 3.6m 3 And/h, wherein the second aerator is a rod-shaped aerator, and the aeration rate is 1.4m 3 And/h, the hydraulic retention time in the aerobic biological fluidized bed is 8 hours.
After the treatment by the process, the water quality of the effluent is finally measured as follows: CODcr 57mg/L, NH 3 -N is 7mg/L, TN is 46mg/L, COD and NH 3 The removal rate of N, TN reaches 92.2%,88.7% and 80.6% respectively.
Comparative example 3
The aerobic biological fluidized bed sewage treatment process and the device in the embodiment 1 are adopted to treat certain coal glycol wastewater.
The water quality condition of the inlet water and the sewage treatment process and the device are the same as those of the embodiment 3, and the difference is that: the second aerator in the aerobic biological fluidized bed is an annular bubbler, the annular bubbler interferes with the uplink sewage, and meanwhile, the annular bubbler aerates unevenly in the aerobic biological fluidized bed, and micro bubbles can not be gathered and separated locally.
After the treatment by the process, the water quality of the effluent is finally measured as follows: CODcr 106mg/L, NH 3 -N is 11mg/L, TN is 62mg/L, COD, NH 3 The removal rate of-N, TN is 85.5%,82.2% and 73.8% respectively.
Claims (13)
1. The sewage treatment process of the aerobic biological fluidized bed for strengthening aeration adopts an anoxic bioreactor and an aerobic biological fluidized bed for combining treatment, and is characterized in that sewage is treated by the anoxic bioreactor and then is introduced into the bottom of the aerobic biological fluidized bed, a micro-bubble aerator, a first inner cylinder, a second aerator and a second inner cylinder are sequentially arranged in the aerobic biological fluidized bed from bottom to top, an air source is respectively aerated by the micro-bubble aerator and the second aerator to respectively generate micro-bubbles and large bubbles, the sewage introduced into the fluidized bed flows upwards in the first inner cylinder under the action of the micro-bubbles and strengthens the reaction, the sewage reaches the second inner cylinder to further strengthen the reaction under the action of the large bubbles, the rising of the bubbles and the coalescence and removal of the micro-bubbles are accelerated, the average diameter of the micro-bubbles is 50-150 mu m, and the average diameter of the large bubbles is 2-20mm;
part of sewage reaching the top of the aerobic biological fluidized bed flows back to the bottom along an annular gap outside the first inner cylinder and the second inner cylinder and circulates into the first inner cylinder to form circulating flow; a part of sewage flows back to the anoxic bioreactor; the waste gas generated by the reaction is discharged from the top;
the top of the aerobic biological fluidized bed is provided with a liquid level meter, the sewage quantity and the waste gas discharge quantity of the reflux anoxic bioreactor are controlled in a linkage way, the pressure of the top of the aerobic biological fluidized bed is regulated and controlled, and the normal water outlet is ensured;
and the sewage treated by the aerobic biological fluidized bed is discharged from the top of the aerobic biological fluidized bed.
2. The process according to claim 1, wherein the fine bubble aerator has a gas-liquid phase feed volume ratio of (0.3-1): 1, the rising speed of the micro-fine bubbles is 0.005-0.009m/s, the oxygen power efficiency is 4-5 kg/(kW.h), and the hydraulic residence time of the aerobic biological fluidized bed is 4-8 hours.
3. The treatment process according to claim 1, wherein a reflux valve and an exhaust valve for regulating and controlling the sewage amount and the exhaust gas discharge amount of the reflux anoxic bioreactor are arranged at the top of the aerobic biological fluidized bed, the water inlet rate at the bottom of the aerobic biological fluidized bed is kept constant, when the liquid level is too high, the reflux valve is increased, the reflux amount of the reflux anoxic reaction is increased, the exhaust valve is closed, the pressure increase increases the annular gap liquid circulation rate and ensures the water outlet; when the liquid level is too low, the reflux valve is reduced, the reflux quantity of the reflux anoxic reaction is reduced, the exhaust valve is opened, the internal pressure of the fluidized bed is reduced, and the circulation rate of the annular space liquid of the inner cylinder and the outer cylinder is reduced.
4. The process according to claim 1, wherein the volume ratio of the return of the sewage in the annulus to the return of the sewage flowing back to the anoxic bioreactor is (2-4) 1; the pressure range of the top of the aerobic biological fluidized bed is 0.2-0.35MPa; the oxygen content in the sewage of the reflux anoxic bioreactor at the top of the aerobic biological fluidized bed is 0.2-0.5mg/L.
5. The process according to claim 1, wherein the sludge concentration in the aerobic biological fluidized bed is 3-5g/L, and the COD and NH in the aerobic biological fluidized bed are 3 -the ratio of N to total P is (100-150): (4-6): 1, the volume load of the aerobic biological fluidized bed is 2-6 kgCOD/(m) 3 •d)。
6. The treatment process according to claim 1, wherein a part of sludge after solid-liquid separation of the sewage discharged from the aerobic biological fluidized bed is returned to the anoxic bioreactor, and the remaining part is sent to a sludge treatment system for treatment; or a part of the sludge is sent back to the anoxic bioreactor, a part of the sludge is sent back to the aerobic biological fluidized bed, and the rest of the sludge is sent to a sludge treatment system for treatment; the sludge reflux ratio of the aerobic biological fluidized bed is (0-0.6): 1.
7. an aerobic biological fluidized bed sewage treatment device for strengthening aeration, which comprises an anoxic bioreactor and an aerobic biological fluidized bed, and is characterized in that,
the aerobic biological fluidized bed comprises an outer cylinder, wherein a first inner cylinder and a second inner cylinder are arranged in the outer cylinder from bottom to top, a micro-bubble aerator is arranged at the lower end of the first inner cylinder, a second aerator is arranged between the second inner cylinder and the first inner cylinder and is used for generating a large number of micro-bubbles and macro-bubbles respectively, the average diameter of the micro-bubbles is 50-150 mu m, and the average diameter of the macro-bubbles is 2-20mm;
the bottom of the outer cylinder is provided with a first gas phase inlet and a sewage inlet which are respectively communicated with the gas-liquid phase inlet of the micro-bubble aerator, the sewage inlet is communicated with the anoxic bioreactor, and the side wall of the outer cylinder is provided with a second gas phase inlet which is communicated with the second aerator;
the top of the outer cylinder is provided with a reflux outlet, an exhaust gas outlet and a drainage outlet which are respectively used for refluxing part of sewage at the top of the outer cylinder to the anoxic bioreactor, and discharging the exhaust gas at the top and the treated sewage;
the top of the outer cylinder is provided with a liquid level meter which is used for controlling a reflux valve and an exhaust valve which are respectively connected with the reflux outlet and the exhaust outlet in a linkage way.
8. The wastewater treatment plant of claim 7, further comprising an exhaust gas treatment system, a sludge-water separator, and a sludge treatment system, wherein the exhaust gas treatment system is configured to collect and treat exhaust gas generated by the anoxic bioreactor and the aerobic biological fluidized bed; the mud-water separator is connected with the drainage outlet and is used for solid-liquid separating the sewage treated by the aerobic biological fluidized bed; the sludge treatment system is connected with a sludge outlet of the sludge-water separator, and the sludge outlet is connected with the anoxic bioreactor and the aerobic biological fluidized bed.
9. The sewage treatment apparatus according to claim 7, wherein the first inner cylinder lower end comprises a plurality of micro-bubble aerators which are uniformly distributed circumferentially around the shaft center and are arranged in a tangential tilt manner, the tilt directions are uniform, and the tilt angle α of the micro-bubble aerators is 10 ° to 40 °.
10. The sewage treatment device according to claim 7, wherein the micro-bubble aerator produces a large number of micro-bubbles through liquid phase rotational flow shearing, a liquid phase tangential inlet is arranged on the side wall of the micro-bubble aerator, a gas phase axial inlet is arranged at the bottom end of the micro-bubble aerator, a mixing cavity which is communicated with the liquid phase tangential inlet and the gas phase axial inlet is arranged in the micro-bubble aerator, an air inlet throat is arranged between the gas phase axial inlet and the mixing cavity, a throat outlet is arranged at the upper end of the mixing cavity, and the throat outlet is connected with a spiral shearing blade.
11. The wastewater treatment apparatus of claim 10, wherein the ratio of height to diameter of the mixing chamber is (2-4): 1, a step of; the ratio of the diameter of the air inlet throat to the diameter of the mixing chamber is (0.05-0.3): 1, a step of; the helix angle beta of the helical shear blade is 20-50 degrees.
12. The sewage treatment apparatus according to claim 7, wherein a plurality of second aerators are provided between the second inner cylinder and the first inner cylinder, and the second aerators are rod-shaped aerators with aeration holes opening upwards and are suspended in the second inner cylinder.
13. The wastewater treatment device of claim 7, wherein the first inner cylinder and the second inner cylinder are equal in diameter and length, and the ratio of the space between the two inner cylinders to the diameter of the inner cylinder is (0.3-0.6): 1, the ratio of the total height of the two inner cylinders to the height of the aerobic biological fluidized bed is (0.65-0.8): 1, the ratio of the sectional area of the inner cylinder to the annular space area between the inner cylinder and the outer cylinder is 1:1.
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| JP2001212587A (en) * | 2000-02-04 | 2001-08-07 | Kubota Corp | Method and apparatus for diffusing air of membrane separation activated sludge method |
| US6531058B1 (en) * | 2002-05-13 | 2003-03-11 | Juan Carlos Josse | Biological fluidized bed apparatus |
| KR20060054266A (en) * | 2006-05-01 | 2006-05-22 | 임광희 | Package type-multistage reactor combining the upperpart of aerobic fluidized biofilm process and thelower part of anoxic process |
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