CN106554085A - Sewage total nitrogen processing meanss and method - Google Patents
Sewage total nitrogen processing meanss and method Download PDFInfo
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Abstract
The present invention relates to a kind of sewage total nitrogen processing meanss and method, belong to sewage treatment area.Sewage total nitrogen processing meanss of the present invention include the first biochemical reaction tank, the first settling tank, the second biochemical reaction tank, the second settling tank, sludge carbon source converter and supporting sludge reflux control system, and be respectively arranged with first biochemical reaction tank, the second biochemical reaction tank can individually several aerators of Valve controlling, filler, guiding gutter and air liquid level lifter, the water inlet end of wherein described guiding gutter in respective air liquid level lifter delivery port, to realize exporting the backflow of sewage sludge mixed liquor.Invention enhances the total nitrogen removal effect of biochemical reaction tank, the removal effect of COD is taken into account simultaneously, the efficient removal of COD, ammonia nitrogen, total nitrogen can be realized in a reaction tank, it is few with oxygen demand, mixed-liquor return required drive is little, total nitrogen removal efficiency is high, it is few compared with A/O technique structures, adapt to variation water quality, sludge yield it is few the features such as.
Description
Technical field
The invention belongs to sewage treatment area, more particularly to a kind of sewage total nitrogen processing meanss and method.
Background technology
Increasingly harsh with sewage drainage standard, the discharge index of total nitrogen is more and more stricter, national environmental protection agencies dictate 2017
From January 1, existing sewage-treatment plant performs the discharge standard of total nitrogen≤30mg/L.Existing most of sewage disposal systems
Total nitrogen processing mode is biochemical treatment, i.e., carry out total nitrogen removal by the anaerobic nitrification of microorganism, oxygen consumption denitrification.Micro- life
The nitrifying process of thing is that denitrification is by nitrite, nitrate transformation by the process that mineralized nitrogen is nitrite, nitrate
For the process of nitrogen, the removal effect of total nitrogen depends primarily on the degree of nitration denitrification.In the sewage of traditional nitration denitrification
It is related to aerobic reaction tank muddy water mixed solution in processing system and is back to anaerobic reation pool, in theory, the bigger total nitrogen of backflow ratio goes
Except the higher but big backflow ratio of rate necessarily causes high operating cost.Some trade effluents such as oil refining sewerage, water quality are complicated,
Ammonia nitrogen total nitrogen is all higher, and the organic carbon source in water is low and is difficult to be utilized by microorganism denitrification compared with carbon source in urban sewage, therefore total nitrogen
Removal efficiency is not high.The sewage farm that some early stages set up simultaneously, only devised nitration reaction pond, no denitrification work(at that time
Can, transformation is got up the capital expenditure and occupation of land that there is a problem of that newly-built denitrification pond causes.Part of contaminated water Treatment stations improve total nitrogen
After removal effect, water outlet COD may be caused to reach discharge standard.Excess sludge is processed and is always sewage treatment plant simultaneously
A difficult problem, if excess sludge carbon sourceization is used for denitrification, you can improve denitrification efficiency, excess sludge production can be reduced again.
The Chinese patent of Application No. 200710178684.4 disclose bio-denitrifying sewage and sludge decrement coupling bioreactor and
Its technique, the inside be related to along water (flow) direction construct successively Wei Yang areas to nitrify, anoxic zone wander about as a refugee capture sludge it is degraded and
Decrement simultaneously provides carbon source with denitrogenation, aerobic zone SND (synchronous nitration and denitrification effect) and further denitrogenation, and volume ratio is respectively
23%th, 45% and 32%, each area grows its suitable microorganism respectively.Although along water (flow) direction construct Wei Yang areas, anoxic zone,
Aerobic zone enhances denitrification effect, but volume ratio is fixed, the bad adaptability when raw water quality fluctuates, while the ball-shaped filling material of stacking
The short stream in water route is easily formed, is made water distribution uneven, is made the efficiency of sludge small molecule carbon source low.The present invention can realize Wei Yang areas,
Anoxic zone, aerobic zone, can adjust can also the ratio in each area, can preferably adapt to variation water quality, currently preferred suspension
Formula semi soft packing biofilm amount, will not form the phenomenon of the short stream in water route.
The Chinese patent of Application No. 201410120733.9 discloses the device and method for strengthening multistage A/O techniques biological denitrificaion,
The inside is related to three-level A/O technique, is followed successively by anoxic zone A- I, aerobic zone O- I-I, aerobic zone O- I-II, anoxic zone
A- II, aerobic zone O- II-I, aerobic zone O- II-II, anoxic zone A- III, aerobic zone O- III-I, aerobic zone O- III-II,
Each aerobic zone and anoxic zone volume ratio 0.8～1:1.In A- I, O- I-II, A- II, O- II-II, A- III, III-II point of O-
Not Zhuan Tian suspension wander about as a refugee ball；Stereo-spongy filler is loaded respectively in O- I-I, O- II-I, O- III-I；Three sections of device point is simultaneously
Anoxic zone is arrived in connection water inlet, and nitrification liquid is back to anoxic zone A- I from Aerobic Pond O- III-II.The invention is connected for multistage A/O techniques,
Equally exist anoxic zone, the area size of aerobic zone is fixed, the ball of wandering about as a refugee of suspension is easily formed the problem of the short stream in water route, while
In its Figure of description, mixed-liquor return is driven using water pump, there is high energy consumption, and the present invention adopts air liquid level lifter
Backflow mixed liquor, can realize under low energy consumption that vast scale flows back.
In sum, in current oil refining sewerage total nitrogen system operation, there is following technical problem：
1st, denitrification efficiency is not high.
2nd, easily it is hit when raw water quality fluctuates.
3rd, using water pump backflow mixed liquor, operating cost is raised.
4th, the carbon source nitrogen source ratio of raw water is not enough, and denitrification effect is restricted.
5th, by strengthening the filler that efficiencies of nitrogen removal is added, water route cutout is easily caused, declines reinforcing effect.If being in filler
Fluidized state then needs big energy consumption.
6th, excess sludge is more, and processing cost is high.
7th, be not provided with denitrification anaerobic unit when sewage disposal system is set up, increase denitrification functions exist take up an area, capital expenditure is asked
Topic.
The content of the invention
The technical problem to be solved is to overcome the above-mentioned problems in the prior art, there is provided a kind of to be applied to oil refining dirt
Water, chemical engineering sewage, sanitary sewage etc., are particularly suited for the total nitrogen processing meanss and method of the above-mentioned sewage of low ratio of carbon to ammonium.
Sewage total nitrogen processing meanss of the present invention include the first biochemical reaction tank, the first settling tank, the second biochemical reaction tank,
Two settling tanks, sludge carbon source converter and supporting sludge reflux control system；Wherein, the first biochemical reaction tank, first are sunk
Drop pond, the second biochemical reaction tank and the second settling tank are arranged in order, and in the first biochemical reaction tank, the second biochemical reaction tank respectively
Be provided with can individually several aerators of Valve controlling, filler, guiding gutter and air liquid level lifter, wherein the water conservancy diversion
The water inlet end of groove is in respective air liquid level lifter delivery port.
Described the first settling tank, the second settling tank are flat flow settling tank, vertical-flow settling tank or inclined plate sedimentation pond, described
Sludge carbon source converter is tubular type sludge crushing device, ultrasonic sludge destroyer or anaerobic sludge digestion reactor.
Described aerator arranges valve along water (flow) direction, and adopts perforated pipe aerating regulation or micro-pore aeration, preferred microporous aeration.
Front end or end of the water side of described guiding gutter in any dissolved oxygen region of corresponding biochemical reaction tank, are preferably placed at corresponding
Biochemical reaction tank entrance point.
Described air liquid level lifter is arranged on the end in different dissolved oxygen area, is preferably provided at the biochemical reaction tank port of export.
Described device also includes the additional carbon dosing system being connected with the first biochemical reaction tank or the second biochemical reaction tank.
Sewage total nitrogen processing method of the present invention is：Wastewater influent is entered by the first biochemical reaction tank import, and water outlet is entered
First settling tank, the first settling tank water outlet and remaining wastewater influent enter the second biochemical reaction tank, and the second biochemical reaction tank water outlet is entered
Enter the second settling tank, the second settling tank water outlet enters subsequent processes, and the first settling tank, the sludge part of the second settling tank are returned
Corresponding biochemical reaction tank is flow to, remaining sludge enters sludge carbon source converter to supplement denitrifying carbon in the second biochemical reaction tank
Source；Wherein, filler is added in the first biochemical reaction tank, the second biochemical reaction tank, and adjust aerator and respectively switched, control
In corresponding biochemical reaction tank, the aeration rate of diverse location, is divided into more than 2 different dissolved oxygen regions, and adopts air fluid
Position lifter will be exported after sewage sludge mixed liquor is lifted and be flowed back by guiding gutter.Wherein, air liquid level lifter only will need to be exported
Liquid level lifts 0.3～0.6m, is capable of achieving the outlet sewage sludge mixed-liquor return of vast scale.
Described filler be suspension type semi soft packing, spherical suspending filling material or ring-type floating stuffing, preferred suspension type semi soft packing.
The wastewater influent fully enters the first biochemical reaction tank or into the wastewater influent of the first biochemical reaction tank and into the second life
The volume ratio for changing the remaining wastewater influent of reaction tank is 5 ﹕, 1～3 ﹕ 1.
Described different dissolved oxygen region is：First biochemical reaction tank, the preferred anaerobic zone of the second biochemical reaction tank, aerobic zone it is suitable
Before sequence, preferably the first biochemical reaction tank, 1/3 region is that anaerobic zone is used to nitrify for aerobic zone for anti-nitration reaction, rear 2/3 region
Reaction；Before second biochemical reaction tank, 2/3 region is that anaerobic zone is used to nitrify instead for aerobic zone for anti-nitration reaction, rear 1/3 region
Should be up to standard with guarantee water outlet COD.The first described biochemical reaction tank anaerobic zone dissolved oxygen be 0～2.0mg/L, preferably 0.5～
1.0mg/L, aerobic zone dissolved oxygen are 2.0～7.0mg/L, preferably 3.0～4.0mg/L；The second described biochemical reaction tank anaerobic zone
Dissolved oxygen is 0～2.0mg/L, and preferably 0.5～1.0mg/L, aerobic zone dissolved oxygen are 2.0～7.0mg/L, preferably 4.0～6.0mg/L.
Pass through additional carbon dosing system when raw water carbon-nitrogen ratio (concentration ratio of COD and total nitrogen in wastewater influent) is less than 2 ﹕ 1
Add carbon source, the carbon source is methyl alcohol, ethanol, sodium acetate, glucose or easy biochemical sewage, preferably easy biochemical sewage.
The distribution of the dissolved oxygen in the controllable biochemical reaction tank of aerator of the present invention；The filler of setting can form dissolved oxygen ladder
Degree, advantageously forms the process of short-cut nitrification and denitrification, synchronous nitration and denitrification, reduces and expose while nitrogen removal rate is improved
Tolerance, reduction carbon source consumption and reduction sludge yield；Air liquid level lifter can be by the backflow of mixed liquor low energy consumption vast scale.This
Invention enhances the total nitrogen removal effect of biochemical reaction tank, while taking into account the removal effect of COD, can realize in a reaction tank
COD, ammonia nitrogen, the efficient removal of total nitrogen, few with oxygen demand, mixed-liquor return required drive is little, and total nitrogen removal efficiency is high,
The features such as, adaptation variation water quality few compared with A/O technique structures, sludge yield lack.By the biochemical reaction of the two or more present invention
Total nitrogen removal effect can be further strengthened in pond series connection.Remaining sludge is converted to carbon source is used for the denitrification of the second biochemical reaction tank
In, sludge reduction is realized while additional carbon dosage is reduced.
The present invention has following excellent effects：
1st, denitrification efficiency is high, and water outlet is while total nitrogen is up to standard, it is ensured that COD is up to standard.
2nd, in biochemical reaction tank, any region soluble oxygen can control, and can adjust aerobic zone in time according to the conversion of water inlet carbon-nitrogen ratio and detest
The ratio and order in oxygen area, guarantees standard water discharge in variation water quality.
3rd, air liquid level lifter can flow back in vast scale under low energy consumption, improve denitrifying efficiency.
, there is no water route short circuit problem in the 4th, preferred suspension type semi soft packing, water distribution is uniform.Biomembrane on filler exists molten
Solution oxygen gradient, easily synchronizes nitration denitrification and short-cut nitrification and denitrification process, is reducing aeration rate and denitrifying carbon source
While consumption, sludge yield is reduced.
5th, by excess sludge carbon source, the carbon source into the second biochemical reaction tank is supplemented, while total nitrogen treatment effect is strengthened,
Reduce excess sludge production.
6th, reduce than traditional A/O techniques nitration denitrification structures, in former design, do not have the sewage farm of denitrification function can
By biochemical reaction tank construction transformed so as to possess denitrification function and without structures.
Description of the drawings
Fig. 1 is the sewage total nitrogen process chart of the present invention.
Fig. 2 is the biochemical reaction tank structural map of the present invention.
Reference described in figure：The first biochemical reaction tanks of 1-, the first settling tanks of 2-, the second biochemical reaction tanks of 3-, 4- second are settled
Pond, 5- sludge carbon source converters, 6- aerators, 7- fillers, 8- guiding gutters, 9- air liquid level lifters.
Specific embodiment
The invention will be further described below in conjunction with the accompanying drawings：
Embodiment 1
Device provided by the present invention is described with reference to the drawings first：
As shown in Figure 1 and Figure 2, sewage total nitrogen processing meanss provided by the present invention include that the first biochemical reaction tank 1, first is settled
Pond 2, the second biochemical reaction tank 3, the second settling tank 4, sludge carbon source converter 5 and supporting sludge reflux control system；
Wherein, the first biochemical reaction tank 1, the first settling tank 2, the second biochemical reaction tank 3 and the second settling tank 4 are arranged in order, and the
Be respectively arranged with one biochemical reaction tank 1, the second biochemical reaction tank 3 can independent Valve controlling several aerators 6, filler
7th, guiding gutter 8 and air liquid level lifter 9, wherein the water inlet end of the guiding gutter 8 is in 9 water outlet of respective air liquid level lifter
Mouthful.
The method that the present invention is provided is described in detail below in conjunction with accompanying drawing：
Certain factory's oil refining sewerage, water yield 230m are processed using the present invention3/ h, COD 300mg/L, total nitrogen 88mg/L, ammonia nitrogen 42mg/L,
180m3/ h wastewater influents are entered by 1 import of the first biochemical reaction tank, and adjustment aerator 6 is each to be switched, and control first is biochemical anti-
Before answering pond 1,1/3 region is that anaerobic zone dissolved oxygen is used for anti-nitration reaction for 0.5～1.0mg/L, and 2/3 region is that aerobic zone is molten afterwards
Solution oxygen is that 3.0～4.0mg/L is used for nitration reaction.First biochemical reaction tank 1 is exported sewage sludge and is mixed by air liquid level lifter 9
The backflow of 400% ratio of liquid is closed, water outlet enters the first settling tank 2,2 water outlet of the first settling tank and 50m3/ h water inlets are into the second life
Change reaction tank 3, adjustment aerator 6 is each to be switched, and 2/3 region for anaerobic zone dissolved oxygen is before controlling the second biochemical reaction tank 3
0.5～1.0mg/L be used for anti-nitration reaction, afterwards 1/3 region be aerobic zone dissolved oxygen be 4.0～6.0mg/L be used for nitration reaction and
Ensure that water outlet COD is up to standard, the second biochemical reaction tank 3 is exported 100% ratio of sewage sludge mixed liquor by air liquid level lifter 9
Backflow.Second biochemical reaction tank 3 enters the second settling tank 4, and 4 water outlet of the second settling tank enters subsequent processes.First life
Change reaction tank 1 and add suspension type semi-soft packing, it is 2000～2500mg/L control sludge concentration, and the second biochemical reaction tank 3 adds
Suspension type semi-soft packing, with clear water mode operation, the first settling tank 2, the sludge part of the second settling tank 4 are back to corresponding life
Change reaction tank, remaining sludge enters sludge carbon source converter 5 to supplement denitrifying carbon source in the second biochemical reaction tank 3, no
Enable additional carbon dosing system.As a result it is：COD 38mg/L, total nitrogen 11mg/L, ammonia nitrogen are not detected, the backflow of 400% ratio
When power of motor be 7kWh.
Embodiment 2
The sewage total nitrogen processing meanss of the present embodiment are same as Example 1, therefore repeat no more.
The method that the present invention is provided is described in detail below in conjunction with accompanying drawing：
Certain factory's oil refining sewerage, water yield 250m are processed using the present invention3/ h, COD 200mg/L, total nitrogen 90mg/L, ammonia nitrogen 45mg/L,
200m3/ h wastewater influents are entered by 1 import of the first biochemical reaction tank, and adjustment aerator 6 is each to be switched, and control first is biochemical anti-
Before answering pond 1,1/3 region is that anaerobic zone dissolved oxygen is used for anti-nitration reaction for 0.5～1.0mg/L, and 2/3 region is that aerobic zone is molten afterwards
Solution oxygen is that 3.0～4.0mg/L is used for nitration reaction.First biochemical reaction tank 1 is exported sewage sludge and is mixed by air liquid level lifter 9
The backflow of 400% ratio of liquid is closed, water outlet enters the first settling tank 2,2 water outlet of the first settling tank and 50m3/ h water inlets are into the second life
Change reaction tank 3, adjustment aerator 6 is each to be switched, and 2/3 region for anaerobic zone dissolved oxygen is before controlling the second biochemical reaction tank 3
0.5～1.0mg/L be used for anti-nitration reaction, afterwards 1/3 region be aerobic zone dissolved oxygen be 4.0～6.0mg/L be used for nitration reaction and
Ensure that water outlet COD is up to standard, 3 mouthfuls of 100% ratios of sewage sludge mixed liquor of the second biochemical reaction tank are returned by air liquid level lifter 9
Stream.Second biochemical reaction tank 3 enters the second settling tank 4, and 4 water outlet of the second settling tank enters subsequent processes.First is biochemical
Reaction tank 1 adds suspension type semi-soft packing, and sludge concentration is 2000～2500mg/L, and the second biochemical reaction tank 3 adds suspension type
Semi-soft packing, with clear water mode operation, the first settling tank 2, the sludge part of the second settling tank 4 are back to corresponding biochemical reaction
Pond, remaining sludge enter sludge carbon source converter 5 to supplement denitrifying carbon source in the second biochemical reaction tank 3, do not enable outer
Plus carbon source dosing system.As a result it is：COD 35mg/L, total nitrogen 22mg/L, ammonia nitrogen are not detected, motor when 400% ratio flows back
Power is 7.2kWh, and when 100% ratio flows back, power of motor is 1.8kWh.
Embodiment 3
The sewage total nitrogen processing meanss of the present embodiment are same as Example 1, therefore repeat no more.
The method that the present invention is provided is described in detail below in conjunction with accompanying drawing：
Chemical engineering sewage, water yield 200m are processed using the present invention3/ h, COD 200mg/L, total nitrogen 40mg/L, ammonia nitrogen 30mg/L,
150m3/ h wastewater influents are entered by 1 import of the first biochemical reaction tank, and adjustment aerator is respectively switched, and controls the first biochemical reaction
Before pond 1,1/2 region is that anaerobic zone dissolved oxygen is used for anti-nitration reaction for 0.5～1.0mg/L, and 1/2 region is that aerobic zone is dissolved afterwards
Oxygen is that 3.0～4.0mg/L is used for nitration reaction.First biochemical reaction tank 1 is exported sewage sludge mixing by air liquid level lifter 9
300% ratio of liquid flows back, and water outlet enters the first settling tank 2,2 water outlet of the first settling tank and 50m3/ h water inlets are biochemical into second
Reaction tank 3, adjustment aerator 6 is each to be switched, before control the second biochemical reaction tank 3 2/3 region be anaerobic zone dissolved oxygen for 0.5～
1.0mg/L is used for anti-nitration reaction, and 1/3 region is that aerobic zone dissolved oxygen is 4.0～6.0mg/L for nitration reaction and ensures afterwards
Water COD is up to standard, and the second biochemical reaction tank 3 is exported the backflow of 100% ratio of sewage sludge mixed liquor by air liquid level lifter 9.
Second biochemical reaction tank 3 enters the second settling tank 4, and 4 water outlet of the second settling tank enters subsequent processes.First biochemical reaction
Pond 1 adds suspension type semi-soft packing, and sludge concentration is 1000～2000mg/L, and the second biochemical reaction tank 3 adds suspension type medium-soft
Filler, sludge concentration are 1000～2000mg/L, and the first settling tank 2, the sludge part of the second settling tank 4 are back to corresponding life
Change reaction tank, remaining sludge enters sludge carbon source converter 5 to supplement denitrifying carbon source in the second biochemical reaction tank 3, no
Enable additional carbon dosing system.As a result it is：COD 40mg/L, total nitrogen 10mg/L, ammonia nitrogen are not detected, the backflow of 300% ratio
When power of motor be 5.4kWh, 100% ratio flow back when power of motor be 1.8kWh.
Comparative example 1
The oil refining sewerage of certain factory's embodiment 1, water yield 230m are processed using the present invention3/ h, COD 300mg/L, total nitrogen 88mg/L,
Ammonia nitrogen 42mg/L, factory's flow process are the first biochemical reaction tank-the first settling tank-the second biochemical reaction tank-the second settling tank.
230m3/ h wastewater influents are entered by the first biochemical reaction tank import, and aeration control full response pond dissolved oxygen is 0.2～0.5mg/L,
First biochemical reaction tank water outlet enters the first settling tank, and the first settling tank water outlet enters the second biochemical reaction tank, and aeration control is all-trans
Pond dissolved oxygen is answered for 6.0～7.0mg/L, the second settling tank water outlet enters subsequent processes.First biochemical reaction tank does not add outstanding
Hanging semi-soft packing, controls sludge concentration for 6000～8000mg/L, and the second biochemical reaction tank does not add suspension type semi-soft packing,
Sludge concentration is controlled for 2000～4000mg/L, the first settling tank, the sludge part of the second settling tank are back to biochemical reaction tank,
Without sludge carbon source converter and additional carbon dosing system.As a result it is：COD 38mg/L, total nitrogen 55mg/L, ammonia nitrogen are not detected.
Comparative example 2
The oil refining sewerage of certain factory's embodiment 1, water yield 230m are processed using the present invention3/ h, COD 300mg/L, total nitrogen 88mg/L,
Ammonia nitrogen 42mg/L, factory's flow process are the first biochemical reaction tank-the first settling tank-the second biochemical reaction tank-the second settling tank.
230m3/ h wastewater influents are entered by the first biochemical reaction tank import, and aeration control full response pond dissolved oxygen is 0.2～0.5mg/L,
First biochemical reaction tank water outlet enters the first settling tank, and the first settling tank water outlet enters the second biochemical reaction tank, and aeration control is all-trans
Pond dissolved oxygen is answered for 6.0～7.0mg/L, the second settling tank water outlet enters subsequent processes.First biochemical reaction tank does not add outstanding
Hanging semi-soft packing, controls sludge concentration for 6000～8000mg/L, and the second biochemical reaction tank does not add suspension type semi-soft packing,
Sludge concentration is controlled for 2000～4000mg/L, the second biochemical reaction tank outlet 200% ratio of mixed liquor is back to biochemical reaction tank
Front end, the first settling tank, the sludge part of the second settling tank are back to biochemical reaction tank, without sludge carbon source converter and external carbon
Source dosing system.As a result it is：COD 34mg/L, total nitrogen 33mg/L, ammonia nitrogen are not detected, and 200% ratio backflow power of motor is
30kWh。
Claims (10)
1. a kind of sewage total nitrogen processing meanss, it is characterised in that including the first biochemical reaction tank (1), the first settling tank (2),
Second biochemical reaction tank (3), the second settling tank (4), sludge carbon source converter (5) and supporting sludge reflux control system；
Wherein, the first biochemical reaction tank (1), the first settling tank (2), the second biochemical reaction tank (3) and the second settling tank (4) according to
Be respectively arranged with secondary arrangement, and the first biochemical reaction tank (1), the second biochemical reaction tank (3) can independent Valve controlling it is some
Individual aerator (6), filler (7), guiding gutter (8) and air liquid level lifter (9), wherein the guiding gutter (8)
Water inlet end is in respective air liquid level lifter (9) delivery port.
2. a kind of sewage total nitrogen processing meanss as claimed in claim 1, it is characterised in that described the first settling tank (2),
Second settling tank (4) is flat flow settling tank, vertical-flow settling tank or inclined plate sedimentation pond, described sludge carbon source converter (5)
For tubular type sludge crushing device, ultrasonic sludge destroyer or anaerobic sludge digestion reactor.
3. a kind of sewage total nitrogen processing meanss as claimed in claim 1, it is characterised in that described aerator (6) edge
Water (flow) direction arranges valve, and adopts perforated pipe aerating regulation or micro-pore aeration, and the water side of described guiding gutter (8) is corresponding biochemical
The front end or end in any dissolved oxygen region of reaction tank, is preferably placed at corresponding biochemical reaction tank entrance point, and described air liquid level is carried
The end that device (9) is arranged on different dissolved oxygen region is risen, preferably in the corresponding biochemical reaction tank port of export.
4. a kind of sewage total nitrogen processing meanss as claimed in claim 1, it is characterised in that also include and the first biochemical reaction tank
(1) the additional carbon dosing system that or the second biochemical reaction tank (3) connects.
5. a kind of usage right requires the sewage total nitrogen processing method of sewage total nitrogen processing meanss described in 1-4 any one, its feature
It is that wastewater influent is entered by the first biochemical reaction tank (1) import, water outlet enters the first settling tank (2), the first settling tank
(2) water outlet and remaining wastewater influent enter the second biochemical reaction tank (3), and the second biochemical reaction tank (3) water outlet is heavy into second
Drop pond (4), the second settling tank (4) water outlet enter subsequent processes, the first settling tank (2), the second settling tank (4)
Sludge part is back to corresponding biochemical reaction tank, and remaining sludge enters sludge carbon source converter (5) to supplement the second biochemical reaction
Denitrifying carbon source in pond (3)；Wherein, filler is added in the first biochemical reaction tank (1), the second biochemical reaction tank (3)
(7), and adjust aerator (6) and respectively switch, control the aeration rate of diverse location in corresponding biochemical reaction tank, be divided into 2
Individual above different dissolved oxygen region, and will be exported after sewage sludge mixed liquor is lifted by leading using air liquid level lifter (9)
Chute (8) flows back.
6. a kind of sewage total nitrogen processing method as claimed in claim 5, it is characterised in that described filler (7) is suspension type
Semi soft packing, spherical suspending filling material or ring-type floating stuffing.
7. a kind of sewage total nitrogen processing method as claimed in claim 5, it is characterised in that the wastewater influent fully enters
One biochemical reaction tank (1) enters the wastewater influent of the first biochemical reaction tank (1) and enters the surplus of the second biochemical reaction tank (3)
The volume ratio of remaining wastewater influent is 5 ﹕, 1～3 ﹕ 1.
8. a kind of sewage total nitrogen processing method as claimed in claim 5, it is characterised in that described different dissolved oxygen region is：
Before first biochemical reaction tank (1) 1/3 region be anaerobic zone, rear 2/3 region be aerobic zone, before the second biochemical reaction tank (3)
2/3 region is anaerobic zone, rear 1/3 region is aerobic zone.
9. a kind of sewage total nitrogen processing method as claimed in claim 8, it is characterised in that described the first biochemical reaction tank (1)
Anaerobic zone dissolved oxygen be 0～2.0mg/L, preferably 0.5～1.0mg/L, aerobic zone dissolved oxygen be 2.0～7.0mg/L, preferably 3.0～
4.0mg/L；Described the second biochemical reaction tank (3) anaerobic zone dissolved oxygen be 0～2.0mg/L, preferably 0.5～1.0mg/L, it is good
Oxygen area dissolved oxygen is 2.0～7.0mg/L, preferably 4.0～6.0mg/L.
10. a kind of sewage total nitrogen processing method as claimed in claim 5, it is characterised in that be less than 2 ﹕ 1 in raw water carbon-nitrogen ratio
When carbon source is added by additional carbon dosing system, the carbon source is methyl alcohol, ethanol, sodium acetate, glucose or easy biochemical sewage.
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