CN101862613A - Method and equipment for promoting gas to dissolve in liquid and sewage treatment system using equipment - Google Patents
Method and equipment for promoting gas to dissolve in liquid and sewage treatment system using equipment Download PDFInfo
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- CN101862613A CN101862613A CN201010183937A CN201010183937A CN101862613A CN 101862613 A CN101862613 A CN 101862613A CN 201010183937 A CN201010183937 A CN 201010183937A CN 201010183937 A CN201010183937 A CN 201010183937A CN 101862613 A CN101862613 A CN 101862613A
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract
The invention provides equipment and a method for promoting gas to dissolve in liquid. The equipment comprises a stirrer and a pressure controller, wherein the first end of the stirrer is provided with an air inlet for inputting gas and a liquid inlet for inputting liquid, the second end of the stirrer is provided with an output port for outputting the liquid, and a stirring mechanism for enabling the input liquid and the input gas to generate a turbulent function is arranged among the gas inlet, the liquid inlet and the output port; and the pressure controller is arranged on the output port and is used for controlling the pressure of the output liquid to be smaller than the gas inlet pressure and the liquid inlet pressure, but larger than zero. The invention also provides a sewage treatment system adopting the equipment.
Description
Technical field
The present invention relates to a kind of method that promotes that gas dissolves in liquid, the quick gas-liquid mass transfer method of specifically a kind of supercharging, the quick dissolved oxygen aeration method in the sewage disposal process particularly, can make sewage reach the hypersaturated state of dissolved oxygen, thereby guarantee enough dissolved oxygen supply microbial consumption in moment; The addition of control gas that can be quantitative reduces the waste of gas, and reduces the energy that uses the continuous inflation of aerator to be consumed at present, thereby reaches the purpose that reduces cost of sewage disposal.
Background technology
Biodegradation process is a most important step in the sewage disposal process, and utilizes activated sludge process to come organic substance and nutrients in the degradation of sewage for a long time always.Activated sludge process is the artificial-strengthening method of the self-purification of water, is that a kind of dependence activated sludge operative body removes organic method in the sewage.At present widely used is aerobe method, and the aerobic microbiological that is present in the activated sludge must just can work under the condition that has oxygen to exist.In the aeration tank of sewage disposal biochemical system, oxygen-transfer efficiency becomes positive correlation with the growth of aerobic microorganisms amount.The quantity delivered of dissolved oxygen will be taken all factors into consideration according to quantity, physiological property, medium property and the concentration of aerobic microbiological.Like this, activated sludge just can be in the state of best degradation of organic substances, if the oxygen supply deficiency, the activated sludge performance is poor, causes water treatment effect to descend.For guaranteeing to have sufficient dissolved oxygen in the water, present widely used method is an aeration, and corresponding apparatus is an aerator.
Aeration is a kind of means that air and water are contacted strongly, and its purpose is airborne oxygen is dissolved in the water, and perhaps unwanted gas and volatile materials in the water is banished in the air, and it is a kind of means that promote mass exchange between gas and the liquid.
Existing aeration type is divided into two classes substantially: a class is blast aeration, and a class is mechanical aeration.
Blast aeration claims the compressed air aeration again.Adopt the aeration tank of this method, mostly be the rectangle concrete sump, be divided into the compartment of several independent water inlets in the pond with partition wall, each compartment is divided into several gallerys again.Sewage is gone into behind the pond and is flowed in gallery in turn, discharges to the other end.Air is to be transported to the air-diffuser that is located at the bottom of the pond with air compressor by pipeline, becomes the bubble disperse and overflows, and at gas-liquid interface oxygen is dissolved in the water.Disperser has antipriming pipe, fixing four kinds of different types such as spiral aerator, water sprayer and micropore diffuser plate.The shortcoming of this mode is in use to be polluted by mud easily and blocking microporous.
Mechanical aeration generally is to utilize the mechanical wheel rotation that is contained in the aeration tank, and waste water in the vigorous agitation pond dissolves in the water airborne oxygen.Impeller is contained in waste water surface in the pond and carries out aeration, is called surface aeration.The water lift effect of this device by impeller impels that waste water constantly circulates in the pond in, brings in constant renewal in the gas-liquid contact-making surface with the increase oxygen absorbed.Form hydraulic jump at periphery during the impeller rotation, can entrain into air effectively; The blade rear side produces negative pressure, can suck air, so the inflation effect is better.Impeller immersed depth and rotating speed can be regulated, to guarantee optimum efficiency.Typical mechanical aeration basin has circular surface aero-accelerator, standard type aero-accelerator, IO type aero-accelerator and square aero-accelerator etc.But the also coupling sometimes of two kinds of methods of blast aeration and mechanical aeration, to improve oxygenation capacity, this is applicable to the sewage that organic concentration is higher.
Above-mentioned several aerator all exists problems such as the not high and oxygen of oxygen utilization rate retention time in water is short, if there is not the continual oxygen that provides just can not satisfy the needed oxygen of microorganism oxygen consumption.
In order further to increase the solubility of oxygen, the existing at present aeration method that adopts pure oxygen.On pure oxygen aeration and the preceding two kinds of aeration mode mechanism is identical substantially, all is by aerobic microbiological the organic matter in the sewage to be carried out biochemical reaction sewage is purified.Different is that the former fills pure oxygen in sewage, and the latter fills air in sewage.One big characteristics of oxygen method are exactly that treatment effeciency is apparently higher than the air method.To same level, the required aeration time of oxygen method only is about 1/3 of an air method generally with same sewage disposal.This is because the concentration of pure oxygen is 4.7 times of oxygen concentration in the air (21%), therefore the dividing potential drop of oxygen in the oxygen method system, that is the motive force of dissolved oxygen, also high 4.7 times than air method, also increased by 4.7 times at the saturation value C of oxygen in water, oxygenation rate has also increased by 4.7 times, has significantly improved the transfer rate of oxygen, thereby the concentration of aerobic microbiological and activity are all improved, obviously improved the deficiency of traditional activated sludge process.But its shortcoming makes the dissolved oxygen of the sewage level that reaches capacity for using pure oxygen, and the use pure oxygen aeration can cause the cost increase.
As mentioned above,, just need the dissolution velocity that a kind of method can be accelerated oxygen, improve the utilization rate of oxygen, improve activation of microorganism, do not increase processing cost simultaneously again in order to solve described problem.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of equipment that promotes that gas dissolves in liquid, its in can accelerating liquid the gas dissolution velocity and improve gas solubility, can reduce processing cost again.
In order to reach the foregoing invention purpose, the invention provides a kind of equipment that promotes that gas dissolves in liquid, it comprises: agitator, described agitator has the air inlet of supplied gas input and the inlet of importing for liquid at first end, have the delivery outlet of output for liquid at second end, and between air inlet and inlet and delivery outlet, have the rabbling mechanism that makes input liquid and input gas generation action of turbulent flow; Pressure controller, described pressure controller is arranged on described equipped at outlet port, and the pressure of controlling described output liquid is less than described admission pressure and described inlet hydraulic, but greater than zero.
Another technical problem to be solved by this invention is to provide a kind of method that promotes that gas dissolves in liquid, its in can accelerating liquid the gas dissolution velocity and improve gas solubility, can reduce processing cost again.
In order to reach the foregoing invention purpose, the invention provides a kind of method that promotes that gas dissolves in liquid, may further comprise the steps: import gas and liquid respectively from first end of agitator; In described agitator, described gas and described liquid are stirred the generation turbulent flow; With the second end output of the liquid after stirring from described agitator, and the pressure of the described output liquid of control control is less than described admission pressure and described inlet hydraulic, but greater than zero.
Another technical problem to be solved by this invention is to provide a kind of sewage disposal system with the said equipment.
In order to reach the foregoing invention purpose, the invention provides a kind of sewage disposal system, comprise: the sewage storage pool, Aerobic Pond, between described sewage storage pool and described Aerobic Pond, be provided with oxygen increasing equipment, described sewage storage pool links to each other with described oxygen increasing equipment by first pipeline, described oxygen increasing equipment links to each other with Aerobic Pond by the 3rd pipeline, at least part of contaminated water flows into described oxygen increasing equipment through described first pipeline and forms heavy-oxygen-enriched water, described then heavy-oxygen-enriched water flows into Aerobic Pond through described the 3rd pipeline, wherein said oxygen increasing equipment comprises: agitator, described agitator has the air inlet of supplied gas input and the inlet of importing for liquid at first end, have the delivery outlet of output for liquid at second end, and between air inlet and inlet and delivery outlet, have the rabbling mechanism that makes input liquid and input gas generation action of turbulent flow; And pressure controller, described pressure controller is arranged on pressure that described equipped at outlet port controls described output liquid less than described admission pressure and described inlet hydraulic, but greater than zero.
The present invention has the following advantages:
1. adopt equipment of the present invention and method, can increase dissolution velocity and the solubility of gas (for example oxygen), also reduced energy resource consumption simultaneously, reduced cost at liquid (for example water).
2. adopt agitator of the present invention, can produce a large amount of bubbles in dissolved oxygen speed that increases liquid and dissolved oxygen amount, the heavy-oxygen-enriched water that will have bubble promotes whole oxygen content greatly with hypoxemia water mixing energy.Needn't carry out oxygenation to all hypoxemia water like this, can reduce gas consumption and energy resource consumption, further reduce cost.
Below with reference to the drawings, the present invention is described in further detail.
Description of drawings
Fig. 1 is the schematic diagram that has the sewage disposal system of oxygen increasing equipment of the present invention.
Fig. 2 is the partial sectional view of the preferred embodiment of agitator in the oxygen increasing equipment of the present invention.
Fig. 3 is the profile of agitating device among Fig. 2.
The specific embodiment
Fig. 1 is the schematic diagram of a sewage disposal system.This sewage disposal system comprises sewage storage pool 1, oxygen increasing equipment 2 and Aerobic Pond 3.
As shown in Figure 1, oxygen increasing equipment 2 of the present invention comprises agitator 21 and pressure controller 22.Agitator 21 1 ends are provided with gas input port 211 and liquid inlet 212, and the other end is provided with delivery outlet 213, and the rabbling mechanism (not shown) is arranged between the above-mentioned input port and delivery outlet.Gas input port 211 links to each other with source of the gas, and the gas that allows source of the gas will have pressure is input in the agitator 21.This gas is air, also can be higher oxygen of concentration or pure oxygen.Liquid inlet 212 is connected with first pipeline 12, and under the situation of valve open, sewage can enter agitator 21.Pressure controller 22 is arranged on delivery outlet 213 places, controls the pressure of delivery outlet 213 place's liquid by the folding of control caliber.The fluid pressure of described delivery outlet 213 should less than the input gas pressure, also should less than the input liquid pressure.Preferably, the little 10%-70% of the described admission pressure of the pressure ratio of output liquid, the best is little 20%-60%; The little 10%-70% of the described inlet hydraulic of pressure ratio of while output liquid, the best is little 20%-60%.In a specific embodiment, the pressure limit of output liquid is 0.1-5kgf, is preferably 0.5-3kgf.
Under above-mentioned pressure condition, sewage and air stir in agitator 21, can improve the dissolution velocity of gas in liquid greatly, also can increase the degree of dissolution saturation of gas (oxygen) in liquid (water), the final sewage (heavy-oxygen-enriched water) that contains saturated dissolved oxygen that forms is discharged from delivery outlet 213, and enters Aerobic Pond 3 through the 3rd pipeline 14.
In order further to control degree of dissolution saturation, can according to circumstances regulate the gas flow that charges into liquid, gas flow accounts for the 10%-50% of liquid and volume of gas usually, is preferably 15-45%.Gas flow control and fluid flow control can realize that the present invention does not elaborate at this by usual manner in the art.But the range of flow of related in the present invention liquid is controlled at 10-1000L/s, and preferable range is at 10-800L/s; Gas flow is controlled at 1-500L/s, and preferable range is at 1-400L/s.In a preferred embodiment, fluid flow is 500L/s, and gas control can be adjusted in the scope of 50-250L/s automatically.
The rabbling mechanism of above-mentioned agitator can adopt the structure of various existing mixing plants in this area, for example existing turbine stirrer, dasher, emulsify at a high speed agitator etc.As long as this stirring structure can make liquids and gases produce violent action of turbulent flow, can be used as agitator of the present invention.
The invention provides a kind of agitator, it has better effect with respect to conventional agitator.As shown in Figure 2, this agitator can produce a large amount of microbubbles in water.In this preferred embodiment, agitator 21 has housing 20.Housing 20 is provided with stator 23, is provided with rotor 24 in the housing.Rotor 24 is positioned at the inboard of stator 23, but and rotates by rotating shaft 240 relative stator.The range of speeds of rotor 24 is preferably 100rpm-900rpm.Above-mentioned gas input port 211 and liquid inlet 212 are positioned at an end of housing 20, and above-mentioned delivery outlet 213 is positioned at the other end of housing.When under the pressure of pressure controller 22, when rotor 24 rotated with respect to stator 23, the gas of inflow fully contacted through stirring with liquid, can make gas be dissolved in apace in the liquid, and have higher solubility (saturation solubility).
Form many row's stator tooths 231 on the stator 23 vertically, every row's stator tooth 231 comprises a plurality of teeth of along the circumferential direction arranging.Also form many row's rotor tooths 241 on the rotor 24 vertically, every row's rotor tooth 241 comprises a plurality of teeth of along the circumferential direction arranging.Each arranges stator tooth 231 and rotor tooth 241 is staggered vertically, and cross sectional shape is roughly rectangle, as shown in Figure 3.Although shown in this cross sectional shape be rectangle, also can be other cross sectional shape, for example trapezoidal, triangle etc.
Each is arranged stator tooth 231 and equates preferably that with the end play L1 of rotor tooth 241 interstice coverage can be 0.2-2mm, is preferably 0.5-1mm.The radial distance L2 of each tooth top of arranging stator tooth 231 to the radial distance L2 of rotor 24 tooth roots and the tooth top of respectively arranging rotor tooth 241 to stator 25 tooth roots equates that preferably interstice coverage can be 0.2-2mm, is preferably 0.5-1mm.
After adopting agitator shown in Figure 2 to carry out the oxygenation processing, can produce a large amount of microbubbles and in liquid, discharge from delivery outlet 213 together.Like this, not only contained saturated dissolved oxygen in the liquid of output, also contained microbubble, and also have certain oxygen content in the microbubble.When only adopting part of contaminated water is carried out saturated inflation by oxygen increasing equipment, and other sewage are when directly entering the mode of Aerobic Pond, this contains the saturated dissolved oxygen sewage (heavy-oxygen-enriched water) of microbubble and mixes with sewage (hypoxemia water) without saturated inflation.Along with the increase of hypoxemia water, because the effect of hydraulic pressure, the microbubble that can slow down in the heavy-oxygen-enriched water overflows speed, has therefore increased the dissolved oxygen content of final sewage.
In another embodiment of the present invention, as shown in Figure 1, the 3rd pipeline 14 can be divided into a plurality of branch roads, wherein first branch road 141 links to each other with the front portion of Aerobic Pond 3, second branch road 142 links to each other with the middle part of Aerobic Pond 3, and the 3rd branch road 143 links to each other with the rear portion of Aerobic Pond 3, makes above-mentioned heavy-oxygen-enriched water to enter by each position of Aerobic Pond 3, further accelerates the speed of dissolution of contaminated water oxygen in the whole Aerobic Pond 3 and improves dissolved oxygen content.In above-mentioned first branch road 141, second branch road 142 and the 3rd branch road 143, valve is installed equally.
After the sewage of Aerobic Pond 3 was handled through above-mentioned saturated oxygen, sewage 31 after purified treatment and the mud 32 that produces were discharged from Aerobic Pond 3 respectively, enter the hypomere operation and handle.
Below data illustrate technique effect of the present invention by experiment.
Table one is the actual power consumption of a sewage treatment plant of the cities of secondary grade, and the Sewage Plant scale is pressed 25000m
3/ day
Sewage treatment plant of the typical cities of secondary grade of table one power consumption
| Unit process | Power consumption (Kwh/m 3) | Proportion (100%) |
| Intake pump | ??0.06 | ??22.6 |
| Grid, setting pot, sedimentation basin, concentration basin | ??0.0064 | ??2.4 |
| Return sludge pump | ??0.02 | ??7.5 |
| Unit process | Power consumption (Kwh/m 3) | Proportion (100%) |
| ?? Tradition aeration tank oxygen supply equipment | ?? 0.145 | ?? 54.5 |
| Treatment of Sludge | ??0.028 | ??10.5 |
| Auxiliary devices such as chemical examination, office | ??0.007 | ??2.6 |
From above-mentioned data as can be seen, the electrisity consumption that carries out oxygen supply with traditional aeration method will account for entire sewage and handle the over half of power consumption total amount.
In the sewage disposal of same scale, the actual power consumption amount that adopts equipment of the present invention and method to carry out oxygenation only is 0.035-0.055Kwh/m
3, can save 0.09-0.11Kwh/m
3Thereby, can save the 20.6%-33% of total power consumption.
Table two is handled for utilizing agitator shown in Figure 2 that part of contaminated water is carried out oxygenation, and part of contaminated water directly enters Aerobic Pond, DO after then heavy-oxygen-enriched water being mixed with hypoxemia water (refer to be dissolved in the molecular oxygen in the water, represent) content with the oxygen containing milligram number of institute in every premium on currency.
Table two different proportion heavy-oxygen-enriched water mixes back DO content with hypoxemia water
As can be seen from the above table, the actual DO that obtains after heavy-oxygen-enriched water and hypoxemia water mixed is than both average DO height, and promptly mixed actual oxygen content is not both simple average values.This is because utilize the agitator that can produce microbubble to make sewage not only be dissolved saturated oxygen, and produced a large amount of microbubbles, increased the contact area of gas and liquid, accelerated the oxygen dissolution velocity in the sewage, increase along with hypoxemia water, because the effect of hydraulic pressure, therefore the speed of overflowing that can slow down the microbubble in the heavy-oxygen-enriched water increased the dissolved oxygen content of final sewage.Like this can not will whole sewage all carry out oxygenation to be handled, and handle as long as part of contaminated water is carried out oxygenation, mixing can reach required oxygenation effect with raw sewerage then, can reduce gas consumption and energy resource consumption, thereby further reduce cost.
More than preferred embodiment of the present invention is described, but scope of the present invention is not limited to above-mentioned specific embodiment.Those skilled in the art can make modification and improvement to the present invention under the instruction of above-mentioned detailed description.Embodiments of the invention are to describe at increasing the solubility and the dissolution velocity of oxygen in water; but those skilled in the art are appreciated that from instruction of the present invention; equipment of the present invention and method are also applicable to other gases and/or other liquid, and these application also should be included within essence of the present invention and the protection domain.
Claims (43)
1. an equipment that promotes that gas dissolves in liquid is characterized in that, comprising:
Agitator, described agitator has the air inlet of supplied gas input and the inlet of importing for liquid at first end, have the delivery outlet of output for liquid at second end, and between air inlet and inlet and delivery outlet, have the rabbling mechanism that makes input liquid and input gas generation action of turbulent flow; And
Pressure controller, described pressure controller is arranged on described equipped at outlet port, and the pressure of controlling described output liquid is less than described admission pressure and described inlet hydraulic, but greater than zero.
2. the equipment that promotion gas as claimed in claim 1 dissolves in liquid is characterized in that, the little 10%-70% of the described admission pressure of the pressure ratio of described output liquid; The little 10%-70% of the described inlet hydraulic of pressure ratio of described output liquid of while.
3. the equipment that promotion gas as claimed in claim 2 dissolves in liquid is characterized in that, the little 20%-60% of the described admission pressure of the pressure ratio of described output liquid; The little 20%-60% of the described inlet hydraulic of pressure ratio of described output liquid of while.
4. the equipment that promotion gas as claimed in claim 1 dissolves in liquid is characterized in that, described agitator comprises for producing the agitator of microbubble:
Housing, described gas input port and liquid inlet are formed on an end of described housing, and described delivery outlet is formed on the other end of described housing;
Be arranged on the stator on the described housing, described stator forms many row's stator tooths vertically, and every row's stator tooth comprises a plurality of teeth of along the circumferential direction arranging; And
Be arranged on the rotor in the described housing, described rotor is positioned at the inboard of described stator, and by rotating shaft can be described relatively the stator rotation, described rotor forms many row's rotor tooths vertically, every row's rotor tooth comprises a plurality of teeth of along the circumferential direction arranging, and each arranges stator tooth and rotor tooth is staggered vertically.
5. the equipment that promotion gas as claimed in claim 4 dissolves in liquid is characterized in that, the cross sectional shape of described stator tooth and described rotor tooth is a rectangle.
6. the equipment that promotion gas as claimed in claim 4 dissolves in liquid is characterized in that, each is arranged stator tooth and equates that with the end play of rotor tooth described interstice coverage is 0.2-2mm.
7. the equipment that promotion gas as claimed in claim 6 dissolves in liquid is characterized in that, described interstice coverage is 0.5-1mm.
8. the equipment that promotion gas as claimed in claim 4 dissolves in liquid, it is characterized in that, each tooth top of arranging stator tooth and the radial distance of rotor tooth root and the tooth top of respectively arranging rotor tooth equate that with the radial distance of stator tooth root the scope of described radial distance is 0.2-2mm.
9. the equipment that promotion gas as claimed in claim 8 dissolves in liquid is characterized in that, the scope of described radial distance is 0.5-1mm.
10. the equipment that dissolves in liquid as each described promotion gas among the claim 1-9 is characterized in that, described gas is air, and described liquid is water.
11. a method that promotes that gas dissolves in liquid is characterized in that, may further comprise the steps:
Import gas and liquid respectively from first end of agitator;
In described agitator, described gas and described liquid are stirred the generation turbulent flow; And
With the second end output of the liquid after stirring from described agitator, and the pressure of controlling described output liquid is less than described admission pressure and described inlet hydraulic, but greater than zero.
12. the method that promotion gas as claimed in claim 11 dissolves in liquid is characterized in that, the little 10%-70% of the described admission pressure of the pressure ratio of described output liquid; The little 10%-70% of the described inlet hydraulic of pressure ratio of described output liquid of while.
13. the method that promotion gas as claimed in claim 12 dissolves in liquid is characterized in that, the little 20%-60% of the described admission pressure of the pressure ratio of described output liquid; The little 20%-60% of the described inlet hydraulic of pressure ratio of described output liquid of while.
14. the method that promotion gas as claimed in claim 11 dissolves in liquid is characterized in that, the 10%-50% of the cumulative volume of described input gas of described input gas comprises and described input liquid.
15. the equipment that promotion gas as claimed in claim 15 dissolves in liquid is characterized in that, the 15%-45% of the cumulative volume of described input gas of described input gas comprises and described input liquid.
16. the method that promotion gas as claimed in claim 11 dissolves in liquid is characterized in that, the air inflow of described gas is 1-500L/s, and the feed liquor amount of described liquid is 1-1000L/s.
17. the method that promotion gas as claimed in claim 16 dissolves in liquid is characterized in that, the air inflow of described gas is 1-400L/s, and the feed liquor amount of described liquid is 10-800L/s.
18. the method that promotion gas as claimed in claim 11 dissolves in liquid is characterized in that, the output pressure of described second end is 0.1-5kgf.
19. the method that promotion gas as claimed in claim 18 dissolves in liquid is characterized in that, the output pressure of described second end is 0.5-3kgf.
20. the method that promotion gas as claimed in claim 11 dissolves in liquid is characterized in that, described agitator comprises for producing the agitator of microbubble:
Housing, described gas input port and liquid inlet are formed on an end of described housing, and described delivery outlet is formed on the other end of described housing;
Be arranged on the stator on the described housing, described stator forms many row's stator tooths vertically, and every row's stator tooth comprises a plurality of teeth of along the circumferential direction arranging; And
Be arranged on the rotor in the described housing, described rotor is positioned at the inboard of described stator, and by rotating shaft can be described relatively the stator rotation, described rotor forms many row's rotor tooths vertically, every row's rotor tooth comprises a plurality of teeth of along the circumferential direction arranging, and each arranges stator tooth and rotor tooth is staggered vertically.
21. the method that promotion gas as claimed in claim 20 dissolves in liquid is characterized in that, the cross sectional shape of described stator tooth and described rotor tooth is a rectangle.
22. the method that promotion gas as claimed in claim 20 dissolves in liquid is characterized in that, each is arranged stator tooth and equates that with the end play of rotor tooth described interstice coverage is 0.2-2mm.
23. the equipment that promotion gas as claimed in claim 22 dissolves in liquid is characterized in that, described interstice coverage is 0.5-1mm.
24. the method that promotion gas as claimed in claim 20 dissolves in liquid, it is characterized in that, each tooth top of arranging stator tooth and the radial distance of rotor tooth root and the tooth top of respectively arranging rotor tooth equate that with the radial distance of stator tooth root the scope of described radial distance is 0.2-2mm.
25. the method that promotion gas as claimed in claim 24 dissolves in liquid is characterized in that, the scope of described radial distance is 0.5-1mm.
26. the method as each described promotion gas among the claim 11-25 dissolves in liquid is characterized in that described gas is air, described liquid is water.
27. sewage disposal system, comprise: sewage storage pool, Aerobic Pond, it is characterized in that: between described sewage storage pool and described Aerobic Pond, be provided with oxygen increasing equipment, described sewage storage pool links to each other with described oxygen increasing equipment by first pipeline, described oxygen increasing equipment links to each other with Aerobic Pond by the 3rd pipeline, at least part of contaminated water flows into described oxygen increasing equipment through described first pipeline and forms heavy-oxygen-enriched water, described then heavy-oxygen-enriched water flows into Aerobic Pond through described the 3rd pipeline, and wherein said oxygen increasing equipment comprises:
Agitator, described agitator has the air inlet of supplied gas input and the inlet of importing for liquid at first end, have the delivery outlet of output for liquid at second end, and between air inlet and inlet and delivery outlet, have the rabbling mechanism that makes input liquid and input gas generation action of turbulent flow; And
Pressure controller, described pressure controller is arranged on described equipped at outlet port, and the pressure of controlling described output liquid is less than described admission pressure and described inlet hydraulic, but greater than zero.
28. the equipment that promotion gas as claimed in claim 27 dissolves in liquid is characterized in that, the little 10%-70% of the described admission pressure of the pressure ratio of described output liquid; The little 10%-70% of the described inlet hydraulic of pressure ratio of described output liquid of while.
29. the equipment that promotion gas as claimed in claim 28 dissolves in liquid is characterized in that, the little 20%-60% of the described admission pressure of the pressure ratio of described output liquid; The little 20%-60% of the described inlet hydraulic of pressure ratio of described output liquid of while.
30. sewage disposal system as claimed in claim 27 is characterized in that, described agitator comprises for producing the agitator of microbubble:
Housing, described gas input port and liquid inlet are formed on an end of described housing, and described delivery outlet is formed on the other end of described housing;
Be arranged on the stator on the described housing, described stator forms many row's stator tooths vertically, and every row's stator tooth comprises a plurality of teeth of along the circumferential direction arranging; And
Be arranged on the rotor in the described housing, described rotor is positioned at the inboard of described stator, and by rotating shaft can be described relatively the stator rotation, described rotor forms many row's rotor tooths vertically, every row's rotor tooth comprises a plurality of teeth of along the circumferential direction arranging, and each arranges stator tooth and rotor tooth is staggered vertically.
31. sewage disposal system as claimed in claim 30 is characterized in that, the cross sectional shape of described stator tooth and described rotor tooth is a rectangle.
32. sewage disposal system as claimed in claim 30 is characterized in that, each is arranged stator tooth and equates that with the end play of rotor tooth described interstice coverage is 0.2-2mm.
33. sewage disposal system as claimed in claim 32 is characterized in that, described interstice coverage is 0.5-1mm.
34. sewage disposal system as claimed in claim 30 is characterized in that, each tooth top of arranging stator tooth and the radial distance of rotor tooth root and the tooth top of respectively arranging rotor tooth equate that with the radial distance of stator tooth root the scope of described radial distance is 0.2-2mm.
35. sewage disposal system as claimed in claim 34 is characterized in that, the scope of described radial distance is 0.5-1mm.
36. sewage disposal system as claimed in claim 27, it is characterized in that, also link to each other between described sewage storage pool and the described Aerobic Pond, flow into the sewage of Aerobic Pond by described second pipeline and in described Aerobic Pond, mix with heavy-oxygen-enriched water by described the 3rd pipeline inflow Aerobic Pond by second pipeline.
37. sewage disposal system as claimed in claim 27, it is characterized in that described the 3rd pipeline comprises first branch road that links to each other with the front portion of described Aerobic Pond, second branch road that links to each other with the middle part of described Aerobic Pond and the 3rd branch road that links to each other with the rear portion of described Aerobic Pond.
38. sewage disposal system as claimed in claim 27 is characterized in that, the 10%-50% of the cumulative volume of described input gas of described input gas comprises and described input liquid.
39. sewage disposal system as claimed in claim 38 is characterized in that, the 15%-45% of the cumulative volume of described input gas of described input gas comprises and described input liquid.
40. sewage disposal system as claimed in claim 39 is characterized in that, the air inflow of described gas is 1-500L/s, and the feed liquor amount of described liquid is 1-1000L/s.
41. sewage disposal system as claimed in claim 40 is characterized in that, the air inflow of described gas is 1-400L/s, and the feed liquor amount of described liquid is 10-800L/s.
42. sewage disposal system as claimed in claim 27 is characterized in that, the output pressure of described second end is 0.1-5kgf.
43. sewage disposal system as claimed in claim 42 is characterized in that, the output pressure of described second end is 0.5-3kgf.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101839379A CN101862613B (en) | 2010-05-25 | 2010-05-25 | Method and equipment for promoting gas to dissolve in liquid and sewage treatment system using equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101839379A CN101862613B (en) | 2010-05-25 | 2010-05-25 | Method and equipment for promoting gas to dissolve in liquid and sewage treatment system using equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101862613A true CN101862613A (en) | 2010-10-20 |
| CN101862613B CN101862613B (en) | 2012-09-26 |
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| CN2010101839379A Active CN101862613B (en) | 2010-05-25 | 2010-05-25 | Method and equipment for promoting gas to dissolve in liquid and sewage treatment system using equipment |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2529449A (en) * | 2014-08-20 | 2016-02-24 | Zen Cassinath | A device and method for high shear liquid metal treatment |
| CN107188312A (en) * | 2017-06-12 | 2017-09-22 | 广西大学 | A kind of method and apparatus that dissolution of contaminated water oxygen content is improved without aeration |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4735709A (en) * | 1985-07-05 | 1988-04-05 | Deister Concentrator Company, Inc. | Method and apparatus for concentration of minerals by froth flotation using dual aeration |
| US4838434A (en) * | 1979-11-15 | 1989-06-13 | University Of Utah | Air sparged hydrocyclone flotation apparatus and methods for separating particles from a particulate suspension |
| CN1067227A (en) * | 1991-05-29 | 1992-12-23 | 美商国际环境系统公司 | Gas dissolving and releasing liquid treatment system |
| CN101448562A (en) * | 2006-05-23 | 2009-06-03 | Otv股份有限公司 | Aerating device for a water filtering system with immersed membranes, including a floor provided with means for injecting a gas and at least one pressure balancing system |
| CN201770530U (en) * | 2010-05-25 | 2011-03-23 | 上海誉辉化工有限公司 | Device for promoting dissolution of gas in liquid and sewage treatment system using the device |
-
2010
- 2010-05-25 CN CN2010101839379A patent/CN101862613B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4838434A (en) * | 1979-11-15 | 1989-06-13 | University Of Utah | Air sparged hydrocyclone flotation apparatus and methods for separating particles from a particulate suspension |
| US4735709A (en) * | 1985-07-05 | 1988-04-05 | Deister Concentrator Company, Inc. | Method and apparatus for concentration of minerals by froth flotation using dual aeration |
| CN1067227A (en) * | 1991-05-29 | 1992-12-23 | 美商国际环境系统公司 | Gas dissolving and releasing liquid treatment system |
| CN101448562A (en) * | 2006-05-23 | 2009-06-03 | Otv股份有限公司 | Aerating device for a water filtering system with immersed membranes, including a floor provided with means for injecting a gas and at least one pressure balancing system |
| CN201770530U (en) * | 2010-05-25 | 2011-03-23 | 上海誉辉化工有限公司 | Device for promoting dissolution of gas in liquid and sewage treatment system using the device |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2529449A (en) * | 2014-08-20 | 2016-02-24 | Zen Cassinath | A device and method for high shear liquid metal treatment |
| GB2529449B (en) * | 2014-08-20 | 2016-08-03 | Cassinath Zen | A device and method for high shear liquid metal treatment |
| CN107188312A (en) * | 2017-06-12 | 2017-09-22 | 广西大学 | A kind of method and apparatus that dissolution of contaminated water oxygen content is improved without aeration |
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|---|---|
| CN101862613B (en) | 2012-09-26 |
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