CN102838207A - Continuous flow aerobe fluidized bed process - Google Patents
Continuous flow aerobe fluidized bed process Download PDFInfo
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- CN102838207A CN102838207A CN2012103890152A CN201210389015A CN102838207A CN 102838207 A CN102838207 A CN 102838207A CN 2012103890152 A CN2012103890152 A CN 2012103890152A CN 201210389015 A CN201210389015 A CN 201210389015A CN 102838207 A CN102838207 A CN 102838207A
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Abstract
The invention discloses a continuous flow aerobe fluidized bed process, which comprises the following steps of: wastewater is stored in a water inlet groove, and is pumped into the bottom of a reactor through a constant flow pump so as to enter a main reactor; the wastewater is filled into the reactor through aeration of an aeration head at the bottom of an air lift pipe in the reactor; sludge is driven to upwards move in the air lift pipe by the airflow, and is subjected to a downward sedimentation movement in a sludge-water separation region at the upper part of the reactor until the sludge enters into the air lift pipe at the main reaction region at the bottom of the reactor again; the wastewater is full of the reactor, and the sludge with the poor sedimentation property is discharged to a water discharge groove at an effluent weir at the upper part of the reactor along with effluent; the main reaction region of the reactor is fully aerated and is in an aerobic condition, and the wastewater is subjected to nitration reactor; when DO (dissolved oxygen) in the sludge-water separation region of the reactor is relatively insufficient and is in an anaerobic condition, the wastewater is subjected to denitrification reaction, and the effect of denitriding is finally realized; phosphorus can be fully absorbed by polyphosphate accumulation bacteria in the sludge-water separation region of the reactor is relatively insufficient and is in an anaerobic condition under the anaerobic condition and the aerobic condition, the last part of the sludge is discharged along with the effluent, and most of sludge continues to react.
Description
Technical field
[0001] the invention belongs to wastewater processing technology, the method for the Industrial Wastewater Treatment that particularly nitrogenous phosphorus is higher.
Background technology
Existing method of wastewater treatment mainly is made up of aerobic, anaerobism and biomembrance process, and in aerobic method, is main with activated sludge process and various differentiation technology thereof mainly, generally includes a. conventional push streaming, the b. step aeration system; C. high loading aeration, d. extended aeration process, e. absorption regeneration method, the complete hybrid system of f.; G. deep well aeration method, h. pure-oxygen aeration method, i.Kraus method, j.AB method; The k.SBR method, l. oxidation ditch, m. circulating active sludge technology etc.These technologies part apply in the actual mechanical process, and certain effect is arranged, but still have some problems, and big such as the pond body bulk, capital cost and working cost are all higher, denitrogenation and organic matter degradation DeGrain, operational management trouble etc.At present, the existing scholar prilling mud that begins one's study is used for carrying out wastewater treatment, but this research mainly is confined in intermittent type sbr reactor device, cultivate domestication, and the relative control condition of SBR technology is comparatively strict, and management expectancy is high.
Summary of the invention
the purpose of this invention is to provide a kind of continuous aerobic biological fluid-bed technology.
A kind of continuous-flow aerobic organism fluidization bed process the steps include:
(1) waste water is stored in inlet flume, controls its temperature in 18～23 ℃, and pH value 6.0～6.5 through hose connection, gets into reactor bottom by constant flow pump (2) suction, gets into main reactor thus, and the control flooding velocity is 16.1～17.1mL/min;
(2) air is blasted by air compressor machine (5), and aeration head (3) aeration bottom air-lift tube in the reactor drum (7) charges into reactor drum, and aeration rate is by gas meter (4) control, and rising gas speed control is built in 100～120L/h;
(3) mud is driven by air-flow and in air-lift tube (7), moves upward, and the subsiding movement downwards in the mud-water separation district (9) on reactor drum top gets into air-lift tube (7) once more to the main reaction region of reactor bottom, forms at inside reactor to circulate;
(4) waste water is full of reactor drum from bottom to top, and hydraulic detention time is 0.49d
-1, under the drive of air-flow, organism fully reacts in mud and the waste water, in the mud-water separation district, and the sludge settling that settling property is good, and the relatively poor mud of settling property is drained into effluent trough (6) with the effluent weir (8) of water outlet in reactor drum top;
(5) the main reaction region aeration of reactor drum is sufficient in step (4), has been in oxygen condition, and waste water can carry out nitration reaction; The DO relative deficiency in the mud-water separation district (10) of reactor drum is in anoxic condition, and waste water can carry out anti-nitration reaction, finally reaches the effect of denitrogenation;
(6) in step (5) reactor drum mud-water separation district (10) under anoxic condition; PolyP bacteria can more fully be released phosphorus; Main reaction region contacts waste water again to the bottom along with sludge settling, and under good oxygen condition, polyP bacteria can fully be inhaled phosphorus; Final section mud is excluded with water outlet, and most of mud continues reaction.
Continuous-flow aerobic biological fluidized bed art breading waste water of the present invention and the cultured method that realizes prilling mud; Compare with existing traditional biological treatment process; Living weight with reactor drum is many; The volumetric loading rate is high, and the hydraulic detention time of waste water in reactor drum is shorter, makes granule sludge better form and improve organic loading and organic clearance.In addition, the main reaction region aeration of this reactor drum is sufficient, makes granular sludge form more easily, basically all in SBAR or sbr reactor device, carries out all about the research of aerobic particle mud at present.The present invention combines aerobic and characteristics anoxic reacter, operation under the even flow state, and not only operational management is convenient, and work simplification, need not the filling filler, does not also need in reaction zone, to establish mechanical stirring device, does not have blockage problem.Reactor drum has aerobic zone and relative oxygen-starved area, has good denitrogenation dephosphorizing effect, and stable through experiment proof last effect, effluent quality is good.There are DO, COD concentration gradient in the reactor drum, effectively control the expansion of prilling mud.Whole process flow is simple, cost is relatively low, need not to establish in addition settling tank and mud reflux, reduces floor space.The present invention is applicable to life and Industrial Wastewater Treatment, is used in particular for the Industrial Wastewater Treatment field nitrogenous, that phosphorus is higher.
Description of drawings
Fig. 1 adopts the process schematic representation based on continuous flow biological reaction bed main body of the present invention, among the figure "---" be gas circuit, "-" is the water route; Fig. 2 is the aspect graph of the seed sludge of embodiment 4; Fig. 3 is the aspect graph of the prilling mud of embodiment 5, and Fig. 4 is the aspect graph of the prilling mud of embodiment 6, and Fig. 5 is the microbial morphology figure among Fig. 2; Fig. 6 is the microbial morphology figure among Fig. 3, and Fig. 7 is the microbial morphology figure among Fig. 4.
Embodiment
The present invention is a kind of continuous-flow aerobic organism fluidization bed process, the steps include:
(1) waste water is stored in inlet flume (1), controls its temperature in 18～23 ℃, and pH value through hose connection, gets into reactor bottom by constant flow pump (2) suction 6.0～6.5, gets into main reactor thus, and the control flooding velocity is 16.1～17.1mL/min;
(2) air is advanced by air compressor machine (5) drum, and aeration head (3) aeration bottom air-lift tube in the reactor drum (7) charges into reactor drum, and aeration rate is by gas meter (4) control, and rising gas speed control is built in 100～120L/h;
(3) mud is driven by air-flow and in air-lift tube (7), moves upward, and the subsiding movement downwards in the mud-water separation district (9) on reactor drum top gets into air-lift tube (7) once more to the main reaction region of reactor bottom, forms at inside reactor to circulate;
(4) waste water is full of reactor drum from bottom to top; Under the drive of air-flow, organism fully reacts in mud and the waste water, in the mud-water separation district; The sludge settling that settling property is good, and the relatively poor mud of settling property is drained into effluent trough (6) with the effluent weir (8) of water outlet in reactor drum top;
(5) the main reaction region aeration of reactor drum is sufficient in step (4), has been in oxygen condition, and waste water can carry out nitration reaction; The DO relative deficiency in the mud-water separation district (10) of reactor drum is in anoxic condition, and waste water can carry out anti-nitration reaction, finally reaches the effect of denitrogenation;
(6) in step (5) reactor drum mud-water separation district (10) under anoxic condition; PolyP bacteria can more fully be released phosphorus; Main reaction region contacts waste water again to the bottom along with sludge settling, and under good oxygen condition, polyP bacteria can fully be inhaled phosphorus; Final section mud is excluded with water outlet, and most of mud continues reaction.
Below be the more concrete embodiment of the present invention.
Embodiment 1,2, and 3,4,5,6: all further describe with manual simulation's waste water.
Embodiment 1:
The temperature of manual simulation's waste water is 18～23 ℃ in the water distribution bucket, and pH value 6.0～6.5, flooding velocity are 17.1mL/min, and rising gas speed control is built in 100～120L/h, COD
CrContent is 889.44mg/L, NH
3-N content 110.73mg/L, TP content 6.51mg/L, manual simulation's waste water gets into reactor drum through the suction of Lange peristaltic pump, is 0.49d at hydraulic detention time
-1The time, water outlet COD
Cr, NH
3The concentration of-N, TP is respectively 140.35mg/L, 2.60mg/L, 0.60mg/L, and clearance reaches 84.22%, 97.65%, 90.78% respectively, and the sewage removal effect is better; Sludge quantity MLSS reaches 634mg/L, and MLVSS reaches 90mg/L; The settling property SV of mud
30Be 8%, the SVI value reaches 124.42mL/g, and sludge quantity and settling property are good.
Embodiment 2:
The temperature of manual simulation's waste water is 18～23 ℃ in the water distribution bucket, and pH value 6.0～6.5, flooding velocity are 17.1mL/min, and rising gas speed control is built in 100～120L/h, COD
CrContent is 1262.86mg/L, NH
3-N content 116.90mg/L, TP content 7.33mg/L, manual simulation's waste water gets into reactor drum through the suction of Lange peristaltic pump, is 0.49d at hydraulic detention time
-1The time, COD in the water outlet
Cr, NH
3The concentration of-N, TP is respectively 173.40mg/L, 11.81mg/L, 0.98mg/L, and clearance reaches 86.27%, 89.90%, 86.63% respectively, and the sewage removal effect is better; Sludge quantity MLSS reaches 394mg/L, and MLVSS reaches 50mg/L; The settling property SV of mud
30Be 5%, the SVI value reaches 139.59mL/g, and sludge quantity and settling property are good.
Embodiment 3:
The temperature of manual simulation's waste water is 18～23 ℃ in the water distribution bucket, and pH value 6.0～6.5, flooding velocity are 17.1mL/min, and rising gas speed control is built in 100～120L/h, COD
CrContent is 1617mg/L, NH
3-N content 149.48mg/L, TP content 8.63mg/L, manual simulation's waste water gets into reactor drum through the suction of Lange peristaltic pump, is 0.49d at hydraulic detention time
-1The time, water outlet COD
Cr, NH
3The concentration of-N, TP is respectively 268.62mg/L, 6.39mg/L, 0.18mg/L, and clearance reaches 83.38%, 95.72%, 97.90% respectively, and the sewage removal effect is better; Sludge quantity MLSS reaches 190mg/L, and MLVSS reaches 40mg/L; The settling property SV of mud
30Be 7.5%, the SVI value reaches 357.15mL/g, and sludge quantity and settling property are good.
Embodiment 4:
The temperature of manual simulation's waste water is 18～23 ℃ in the water distribution bucket, and pH value 6.0～6.5, flooding velocity are 17.1mL/min, and rising gas speed control is built in 100～120L/h, COD
CrContent is 1287.56mg/L, NH
3-N content 95.66mg/L, TP content 8.68mg/L, manual simulation's waste water gets into reactor drum through the suction of Lange peristaltic pump, and hydraulic detention time is 0.49d
-1, seed sludge amount MLSS reaches 6960mg/L, and MLVSS reaches 4020mg/L; The settling property SV of mud
30Be 10%, the SVI value reaches 14.36mL/g, and the form of seed sludge is as shown in Figure 2, and color is darker, does not have tangible profile, and uniform mixing is in water sample, and microflora mainly comprises some zoogloeas and the miniature metazoan of part, and is as shown in Figure 5.
Embodiment 5:
The temperature of manual simulation's waste water is 18～23 ℃ in the water distribution bucket, and pH value 6.0～6.5, flooding velocity are 17.1mL/min, and rising gas speed control is built in 100～120L/h, COD
CrContent is 889.44mg/L, NH
3-N content 110.73mg/L, TP content 6.51mg/L, manual simulation's waste water gets into reactor drum through the suction of Lange peristaltic pump, and hydraulic detention time is 0.49d
-1, granule sludge amount MLSS reaches 320mg/L, and MLVSS reaches 40mg/L; The settling property value of performance mud, SV
30Be 6.6%, the SVI value reaches 206.25mL/g, and the form of prilling mud is as shown in Figure 3; Small-particle is more, is white in color, minimum, the not enough 0.5mm of particle diameter, and flco is closely knit more; Mud-water separation is clear; Its coenosis is made up of filamentous fungus, and part constitutes a snap action by filamentous microorganism on the edge of, and half eyebrow worm is as shown in Figure 6 in the grain edges activity.
Embodiment 6:
The temperature of manual simulation's waste water is 18～23 ℃ in the water distribution bucket, and pH value 6.0～6.5, flooding velocity are 17.1mL/min, and rising gas speed control is built in 100～120L/h, COD
CrContent is 1287.56mg/L, NH
3-N content 95.66mg/L, TP content 8.68mg/L, manual simulation's waste water gets into reactor drum through the suction of Lange peristaltic pump, and hydraulic detention time is 0.49d
-1, granule sludge amount MLSS reaches 634mg/L, and MLVSS reaches 90mg/L; The settling property value of performance mud, SV
30Be 8%, the SVI value reaches 124.42mL/g, and the form of prilling mud is as shown in Figure 4, and color is rendered as brown, and particulate state is clearly arranged, and more smooth its coenosis of particle surface is main, as shown in Figure 7 with the thread fungus of mould Pseudomonas mainly.
Can find out that by above embodiment for manual simulation's waste water, this novel process is for COD
Cr, NH
3The clearance of-N, TP is higher, is 18～23 ℃ in temperature, and pH value is 6.0～6.5, and C:N:P is 100:10:1 in the waste water, and flooding velocity is 17.1mL/min, and rising gas speed control is built in 100～120L/h, and hydraulic detention time is 0.49d
-1The time, through the processing condition of water inlet, water outlet continuously, can turn out that settling property is good, living weight is abundant and the stable prilling mud of microflora, and through the processing of aerobic particle mud, the reactor drum water outlet is respond well, waste water is purified.
Claims (6)
1. a continuous-flow aerobic organism fluidization bed process the steps include:
(1) waste water is stored in inlet flume, controls its temperature in 18～23 ℃, and pH value 6.0～6.5 through hose connection, gets into reactor bottom by constant flow pump (2) suction, gets into main reactor thus, and the control flooding velocity is 16.1～17.1mL/min;
(2) air is blasted by air compressor machine (5), and aeration head (3) aeration bottom air-lift tube in the reactor drum (7) charges into reactor drum, and aeration rate is by gas meter (4) control, and rising gas speed control is built in 100～120L/h;
(3) mud is driven by air-flow and in air-lift tube (7), moves upward, and the subsiding movement downwards in the mud-water separation district (9) on reactor drum top gets into air-lift tube (7) once more to the main reaction region of reactor bottom, forms at inside reactor to circulate;
(4) waste water is full of reactor drum from bottom to top, and hydraulic detention time is 0.49d
-1, under the drive of air-flow, organism fully reacts in mud and the waste water, in the mud-water separation district, and the sludge settling that settling property is good, and the relatively poor mud of settling property is drained into effluent trough (6) with the effluent weir (8) of water outlet in reactor drum top;
(5) the main reaction region aeration of reactor drum is sufficient in step (4), has been in oxygen condition, and waste water can carry out nitration reaction; The DO relative deficiency in the mud-water separation district (10) of reactor drum is in anoxic condition, and waste water can carry out anti-nitration reaction, finally reaches the effect of denitrogenation;
(6) in step (5) reactor drum mud-water separation district (10) under anoxic condition; PolyP bacteria can more fully be released phosphorus; Main reaction region contacts waste water again to the bottom along with sludge settling, and under good oxygen condition, polyP bacteria can fully be inhaled phosphorus; Final section mud is excluded with water outlet, and most of mud continues reaction.
2. a kind of continuous-flow aerobic organism fluidization bed process according to claim 1, it is characterized in that: reactor drum can be divided into main reaction region, mud-water separation district and sludge settling district.
3. according to claim 1,2 described a kind of continuous-flow aerobic organism fluidization bed process, it is characterized in that: the main reaction region bottom of reactor drum is provided with aeration head, and aeration rate can be by gas meter control within the specific limits.
4. according to claim 1,2 described a kind of continuous-flow aerobic organism fluidization bed process, it is characterized in that: in main reaction region, can carry out nitration reaction and inhale the phosphorus effect, aeration makes organism fully contact with mud simultaneously, helps organic matter degradation.
5. according to claim 1,4 described a kind of continuous-flow aerobic organism fluidization bed process, it is characterized in that: the mud-water separation district of reactor drum is cylindrical, and this distinguishes relative anoxic; Mikrobe can carry out anti-nitration reaction and polyP bacteria is released the phosphorus effect; Mud rises to the surface, and the relatively poor mud of settling property is got rid of with water outlet to overflow weir, and settling property mud preferably is parabolic motion to both sides on this top, district because of the air-flow effect; Sink down into the sludge settling district thereupon, continue to participate in reaction.
6. a kind of continuous-flow aerobic organism fluidization bed process according to claim 1; It is characterized in that: organism is fully reaction under the state of water-in and water-out continuously in mikrobe in the reactor drum and the waste water; Adopt bottom water inlet, aeration; Draining is carried out on top, in draining, selects the good mud of settling property, in advantage is selected repeatedly, cultivates acclimation sludge and forms prilling.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288212A (en) * | 2013-05-22 | 2013-09-11 | 崔维 | Combined hyperoxia aeration muddy water integrated treatment system and method |
| CN104710009A (en) * | 2015-03-30 | 2015-06-17 | 深圳市环新环保技术有限公司 | Decentralized processing method and device for town sewage |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101333037A (en) * | 2008-07-01 | 2008-12-31 | 黑龙江科技学院 | Gas-lifting internal circulation intermission aerobic granule sludge reactor and water treatment process thereof |
| CN102139952A (en) * | 2011-04-28 | 2011-08-03 | 吉林大学 | Continuous flow air lifting type aerobic granular sludge fluidized bed device for processing difficult degradation waste water |
-
2012
- 2012-10-15 CN CN2012103890152A patent/CN102838207A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101333037A (en) * | 2008-07-01 | 2008-12-31 | 黑龙江科技学院 | Gas-lifting internal circulation intermission aerobic granule sludge reactor and water treatment process thereof |
| CN102139952A (en) * | 2011-04-28 | 2011-08-03 | 吉林大学 | Continuous flow air lifting type aerobic granular sludge fluidized bed device for processing difficult degradation waste water |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288212A (en) * | 2013-05-22 | 2013-09-11 | 崔维 | Combined hyperoxia aeration muddy water integrated treatment system and method |
| CN103288212B (en) * | 2013-05-22 | 2015-01-07 | 崔维 | Combined hyperoxia aeration muddy water integrated treatment system and method |
| CN104710009A (en) * | 2015-03-30 | 2015-06-17 | 深圳市环新环保技术有限公司 | Decentralized processing method and device for town sewage |
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Application publication date: 20121226 |