CN101767903A - Method for simultaneously nitrifying and denitrifying garbage percolate in SBR reactor - Google Patents

Abstract

The invention discloses a method for simultaneously nitrifying and denitrifying garbage percolate in an SBR reactor. The method comprises the steps of: putting garbage waste water to be processed into an adjusting pond; guiding the garbage waste water into the SBR reactor which contains active sludge and garbage percolate with the function of a pump; and adding compressed air. Aiming at the SBR reactor, the operation has the steps of: adding water, reacting, depositing, discharging water, respectively performing 5 typical stages of an idle running period according to the traditional technology and an A/O work condition, and adjusting and controlling the water entering COD/N ratio and the dissolved oxygen concentration according to the condition of the quality of the entered water to achieve the aim of effectively removing the COD and simultaneously nitrifying and denitrifying. The method realizes the complementation of aerobic nitrification and anaerobic denitrification, has the effects that the nitrifying rate can reach more than 95%, the denitrifying efficiency is high to 90% and even more than 95%, and has the advantages of saving floor area of a biological treatment technology, and saving the investment cost and operation cost.

Description

Percolate is the while nitrification and denitrification method in the sbr reactor device

Technical field

The present invention relates to a kind of wastewater treatment, particularly nitration denitrification denitrogenation treatment process percolate the time.

Background technology

At present, China has the municipal solid waste about 93% to handle the employing burying method.As time goes by, these msw landfills are under the biochemical action of compacting effort and microorganism, and contained pollutent will be with the moisture stripping in the landfill body, and forms percolate with rainfall.Percolate composition complexity, the pollution load height, intractability is big, deals with improperly, and percolate can cause serious pollution to underground water, surface water and refuse landfill surrounding environment, directly threatens the safety at tap water and industrial or agricultural water water source.Therefore, must handle percolate.Although refuse leachate treatment technology has been obtained bigger progress, the processing of the complete harmless treatment, particularly its high ammonia nitrogen of percolate is still global problem.Mainly there is following key issue:

(1) the percolate water yield changes greatly.Especially the seasonal variation amount is very big, rainy season the water yield bigger.At this problem, general landfill yard is provided with the leachate collection equalizing tank, carries out the water yield and regulates the processing of water quality homogenizing.(2) the leachate quality characteristic variations is big.Different landfill yards, because all multifactor differences, there is very big-difference in its water quality, not necessarily also is applicable to the processing of another landfill percolate so be applicable to the treatment process of certain landfill percolate.(3) ammonia nitrogen concentration height in the percolate.And constantly raise along with the increase in landfill yard age, other components contents are also very high.Particularly aged garbage, waste-water has ammonia-nitrogen content height, not biodegradable COD material complexity, characteristics that content is high.(4) carbon source deficiency in the percolate, particularly aged percolate from garbage filling field biodegradability is poor.(5) cost of investment, processing cost costliness.

Sbr reactor device operation operation comprises into water, reaction, precipitation, water outlet, the idle cycle of operation 5 typical phases, treatment process for SBR (sequencing batch reactor) reactor routine is instantaneous water inlet → aeration (2-6h) → precipitation (2-6h) → draining, SRT:30d.It is that denitrification denitrogenation efficient is not high that there is subject matter in this technology.

From present treatment technology, can make stable " household refuse landfill sites pollution control criterion " (GB16889-1997) first discharge standard ((chemical oxygen demand (COD)) COD≤100mgL that is up to state standards of treat effluent ^-1, (biochemical oxygen demand (BOD)) BOD≤30mgL ^-1, NH ₄ ⁺-N≤15mgL ^-1, SS≤70mgL ^-1) sophisticated relatively percolate handle (200m on a large scale ³More than/the d) treatment process mainly contains: anaerobism (UASB--up-flow anaerobic sludge blanket+aerobic (SBR or MBR (membrane bioreactor))+film (NF (nanofiltration) or RO (reverse osmosis)) technology.Yet these technologies exist the cost height, investment is big, film is seriously polluted, concentrated solution productive rate height (near about 30%) and problem such as difficult.In addition, though being suitable for relatively large garbage loading embeading percolation liquid, this technology handles, but the key of its denitrogenation is how at aerobic section, effect by SBR or MBR, reduce the ammonia-nitrogen content in the percolate as far as possible, and carry out denitrification denitrogenation, because the carbon source deficiency, the nitric nitrogen that can not denitrification removes is handled by the film of back and is removed.Therefore, the nitration denitrification biological denitrificaion has the important engineering practical significance when carrying out the extensive treatment technology of percolate.

Summary of the invention

The objective of the invention is to handle the not high shortcoming of biological denitrificaion efficient on a large scale at domestic and international percolate, develop a kind of percolate and in SBR (Seqencing Batch Reactor), realize the method for high-efficiency biological denitrification, by while nitration denitrification (Simultaneous Nitrification and Denitrification-SND) technology, ammonia-nitrogen removal rate is reached more than 95% (to be better than national grade one discharge standard, to reach SBR water outlet NH ₄ ⁺-N≤5mgL ^-1), the denitrification rate reaches more than 90%.

To achieve the above object of the invention, the present invention has taked following technical scheme:

Earlier pending garbage, waste-water (refuse landfill equalizing tank water or UASB water outlet all can) is placed distribution reservoir (2), pass through the effect of pump (1) then, the garbage, waste-water introducing is equipped with in the SBR bio-reactor of active sludge, controls its flow by liquid meter (3); Simultaneously, by compressed air unit (9), the bottom with air is introduced the sbr reactor device by the flow of gas meter (8) control air, and by micropore aeration pipe (5), blasts pressurized air the bottom of SBR (4); Make the active sludge-garbage, waste-water-air three-phase suspension in the reactor realize homogenizing by whipping appts (6); The temperature of waste water is a state of nature, and the area, Guangdong is 26～36 ℃.

In order to realize the SND biological denitrificaion of SBR, also need adjust control water inlet COD/NH ₄ ⁺-N ratio, measure equation according to the contriver in the nitration reaction electronics that at first proposes in the world:

$\frac{5+{2\mathrm{<figure-callout\; id="40"\; label="f\; s"\; filenames="H2009101935138E00013.png,H2009101935138E00021.png"\; state="\{\{state\}\}">f</figure-callout>}}_s}{40}{\mathrm{<figure-callout\; id="4"\; label="NH"\; filenames="H2009101935138E00011.png,H2009101935138E00013.png"\; state="\{\{state\}\}">NH</figure-callout>}}_4^{+}+\frac{1-f_s}{4}{\mathrm{<figure-callout\; id="2"\; label="O"\; filenames="H2009101935138E00011.png,H2009101935138E00032.png"\; state="\{\{state\}\}">O</figure-callout>}}_2+\frac{{\mathrm{<figure-callout\; id="4"\; label="f\; s"\; filenames="H2009101935138E00011.png,H2009101935138E00013.png"\; state="\{\{state\}\}">f</figure-callout>}}_s}{4}{\mathrm{HCO}}_3^{-}=\frac{f_s}{20}{C}_5{H}_7{O}_{2}N+\frac{1}{8}{\mathrm{NO}}_3^{-}$

$+\frac{5-{4f}_s}{20}{H}^{+}+\frac{5+6f_s}{40}{H}_{2}O---\left(1\right)$

$\frac{10+3{\mathrm{<figure-callout\; id="60"\; label="f\; s"\; filenames="H2009101935138E00013.png,H2009101935138E00021.png"\; state="\{\{state\}\}">f</figure-callout>}}_s}{60}{\mathrm{<figure-callout\; id="4"\; label="NH"\; filenames="H2009101935138E00011.png,H2009101935138E00013.png"\; state="\{\{state\}\}">NH</figure-callout>}}_4^{+}+\frac{1-f_s}{4}{\mathrm{<figure-callout\; id="2"\; label="O"\; filenames="H2009101935138E00011.png,H2009101935138E00032.png"\; state="\{\{state\}\}">O</figure-callout>}}_2+\frac{{\mathrm{<figure-callout\; id="4"\; label="f\; s"\; filenames="H2009101935138E00011.png,H2009101935138E00013.png"\; state="\{\{state\}\}">f</figure-callout>}}_s}{4}{\mathrm{HCO}}_3^{-}=\frac{f_s}{20}{C}_5{H}_7{O}_{2}N+\frac{1}{6}{\mathrm{NO}}_2^{-}$

$+\frac{5-{3f}_s}{15}{H}^{+}+\frac{10+{9f}_s}{60}{H}_{2}O---\left(2\right)$

With biological denitrification denitrogenation COD/N than electronics metrology relational expression:

$\frac{\mathrm{COD}}{N-{\mathrm{<figure-callout\; id="3"\; label="NO"\; filenames="H2009101935138E00011.png"\; state="\{\{state\}\}">NO</figure-callout>}}_3}=\frac{2.86}{1-1.628Y}---\left(3\right)$

$\frac{\mathrm{COD}}{N-{\mathrm{<figure-callout\; id="2"\; label="NO"\; filenames="H2009101935138E00011.png,H2009101935138E00032.png"\; state="\{\{state\}\}">NO</figure-callout>}}_2}=\frac{1.714}{1-1.628Y}---\left(4\right)$

Analyze as can be known: compare with traditional nitration denitrification technology by the short-cut nitrification and denitrification of nitrous acid nitrogen approach and have significant advantage, the one, the nitrated stage is saved 25% oxygen requirement, and the 2nd, the denitrification stage is saved about 40% carbon source; Experimental study is the result show: pass through NO ₃ ^-The COD/N that the complete nitrification denitrification of approach needs is than generally in 2.86 above scopes. therefore, for realizing garbage seeping water nitration denitrification (SND) denitrogenation simultaneously, the rubbish water lower to COD/N can consider to add carbon sources such as liquid dung, methyl alcohol, improves the denitrification effect.

With respect to prior art, following characteristics and effect that the present invention has:

(1) changes traditional SBR operation scheme, make it to have A/O process characteristic or (A/O) ²Process characteristic helps the removal and the denitrification denitrogenation effect of ammonia nitrogen.

(2) the present invention is adjusted into the operation of sbr reactor device by A/O technology and handles, and passes through anaerobism, aerobic processes successively, helps the removal of total nitrogen, and its clearance can improve more than 15% than traditional technology.

(3) the present invention is adjusted into the sbr reactor device by (A/O) ²The technology operation, pass through anaerobism, aerobic successively, anaerobism, aerobic processes again, not only help the removal of ammonia nitrogen, also helping the raising of denitrification effect. its denitrification rate can improve more than 20% than traditional technology, particularly can realize nitration denitrification biological denitrificaion simultaneously, make of provide the complementation with aspects such as the generation of consumption, basicity and consumption of two processes, saving running cost at COD and oxygen.

The present invention has important engineering application value to percolate and other high ammonia nitrogen organic waste water.

Description of drawings

Fig. 1 is a percolate nitration denitrification denitrogenation process device synoptic diagram of the present invention;

Fig. 2 is the embodiment of the invention 2 used combination S BR bio-reactor synoptic diagram;

Fig. 3 is that preceding removal effect to COD and ammonia nitrogen is optimized in the embodiment of the invention 2 technological transformation;

Fig. 4 is that preceding removal effect to T-N is optimized in the embodiment of the invention 2 technological transformation;

Fig. 5 is to the removal effect of T-N after the embodiment of the invention 2 technological transformation optimizations;

Fig. 6 is the embodiment of the invention 3 used 2 combination S BR bio-reactor synoptic diagram;

The COD removal effect figure that Fig. 7 debugs by optimization technology for embodiment of the invention 3SBR;

The NH that Fig. 8 debugs by optimization technology for embodiment of the invention 3SBR ₄ ⁺-N removal effect figure.

Embodiment

Come below in conjunction with Figure of description that the invention will be further described, but the present invention's scope required for protection is not limited to the scope described in the embodiment.

As shown in Figure 1, percolate nitration denitrification denitrogenation process device of the present invention comprises sump pump 1, equalizing tank 2, liquid meter 3, SBR bio-reactor 4, micropore aeration pipe 5, agitator 6, water outlet, thief hole 7, gas meter 8, topping-up pump 9, wherein sump pump 1 is positioned at equalizing tank 2, be communicated with SBR bio-reactor 4 through pipeline, pipeline is provided with liquid meter 3, SBR bio-reactor 4 is provided with agitator 6 and micropore aeration pipe 5, and micropore aeration pipe 5 is connected with topping-up pump 9 through gas meter 8; SBR bio-reactor 4 is provided with water outlet, thief hole 7.

Embodiment 1:

The SBR bio-reactor adopts pmma material to make, and the effecting reaction volume is 0.05m ³Test waste water is the (operation existing 7 years so far of Guangdong city percolate from garbage filling field, begun to enter the aged phase, in order to strengthen the biological denitrification denitrification effect, according to denitrification denitrogenation electrometer magnitude relation formula, need to improve the CON/N ratio, so this landfill yard of suggestion has added a certain proportion of liquid dung in the percolate dosing chamber, make the percolate biodegradability increase), water inlet COD _CrConcentration is 1249～3673mg/L, and influent ammonium concentration changes greatly, between 448～923mg/L, fluctuate, and mostly between 700～800mg/L, pH value 7.61～8.64.Pending garbage, waste-water is placed equalizing tank 2, pass through the effect of pump 1 then, the garbage, waste-water introducing is equipped with in the SBR bio-reactor 4 of active sludge, simultaneously, by air boost pump 9, air is sent into the bottom of sbr reactor device, and pass through micropore aeration pipe 5 at the bottom of SBR bio-reactor 4 aeration; Make the active sludge-garbage, waste-water-air three-phase suspension in the reactor realize homogenizing by whipping appts 6; Moved more than 130 day.

SBR bio-reactor 4 operation beginning 100 surplus day adopt a traditional technology to carry out sludge acclimatization, COD remove with ammonia nitrogen removal after the steady stage, use A/O technology and (A/O) instead ²Technology is respectively moved 1 time-of-week.

Wherein the concrete grammar of A/O technology is:

A kind of percolate, comprises the steps and processing condition by A/O technology while nitrification and denitrification method at the sbr reactor device:

(1) anaerobism stirs:, start agitator percolate is carried out anaerobism stirring 1-4h through being pumped into bio-reactor from the percolate in the equalizing tank, rotating speed is 20～30rpm; COD/N when percolate enters the sbr reactor device is 5.0-7.0 than scope, crosses by control front UASB (up-flow anaerobic sludge blanket) level of response or at COD/N to add a certain amount of liquid dung when low or methyl alcohol is regulated and controlled.

(2) aerobic aeration: anaerobism stirs the back and by micropore aeration pipe and topping-up pump percolate is carried out aerobic aeration 2-7h, and by the Flow-rate adjustment of aeration, the control gas-water ratio is 1: 1-1: 2.5;

In the described control sbr reactor device percolate dissolved oxygen concentration by percolate dissolved oxygen concentration in the adjustments of gas under meter control sbr reactor device in the 0.5-2.0mg/l scope.

(3) precipitation: percolate is in sbr reactor device precipitation 1-4h, draining behind the aerobic aeration;

(4) mud stops: the mud in the sbr reactor device stopped in reactor 30～40 days.

Transmission technology can be reduced to:

(1) aerobic aeration: anaerobism stirs the back and by micropore aeration pipe and topping-up pump percolate is carried out aerobic aeration 2-6h, and by the Flow-rate adjustment of aeration, the control gas-water ratio is 1: 1-1: 2.5;

(2) precipitation: percolate is in sbr reactor device precipitation 2-6h, draining behind the aerobic aeration;

(3) mud stops: the mud in the sbr reactor device stopped in reactor 30～40 days.

Implementation result is as shown in table 1:

Principal pollutant removal effect (unit: mg/L) under the different operating modes of table 1

Annotate: Inlet and outlet water and clearance are all averaged; (A/O) ²Technology is present embodiment technology.

As seen, the operation process after the improvement, effluent COD concentration can reach national secondary discharge standard (≤300mg/l), water outlet NH ₄ ⁺-N concentration can reach national grade one discharge standard (≤15mg/l).Wherein, (A/O) ²The COD of technology and ammonia nitrogen removal frank have only in a small amount than traditional technology to be increased, but the denitrification rate is significantly increased: its total nitrogen (T-N) goes out water concentration and significantly reduces to 98mg/l by 242mg/l, and the T-N clearance is corresponding brings up to 87.2%, raising 19.4% from 67.8%.

Embodiment 2

Accompanying drawing 2 is depicted as Guangdong refuse landfill percolate sbr reactor device, and its useful volume is (1500m ³), totally 6 lattice are three cover SBR parallel connections.Because this refuse landfill was runed 7 years, begin to enter the aged phase, thus at first in equalizing tank, add certain excrement and urine water earlier, to improve the COD/N ratio of this type of waste water; Then, adopt above-mentioned optimization technology that this project example is optimized operation, obtained good result.

The operation beginning of SBR bio-reactor 100 surplus day adopt a traditional technology to carry out sludge acclimatization, COD remove with ammonia nitrogen removal after the steady stage, use A/O technology and (A/O) instead ²Technology 1 time of operation.

Wherein the concrete grammar of A/O technology is:

A kind of percolate, comprises the steps and processing condition by A/O technology while nitrification and denitrification method at the sbr reactor device:

(1) anaerobism stirs:, start agitator percolate is carried out anaerobism stirring 1-4h through being pumped into bio-reactor from the percolate in the equalizing tank, rotating speed is 20～30rpm; COD/N when percolate enters the sbr reactor device is 5.0-7.0 than scope, crosses by control front UASB (up-flow anaerobic sludge blanket) level of response or at COD/N to add certain two liquid dungs when low or methyl alcohol is regulated and controlled.

(2) aerobic aeration: anaerobism stirs the back and by micropore aeration pipe and topping-up pump percolate is carried out aerobic aeration 2-7h, and by the Flow-rate adjustment of aeration, the control gas-water ratio is 1: 1-1: 2.5;

In the described control sbr reactor device percolate dissolved oxygen concentration by percolate dissolved oxygen concentration in the adjustments of gas under meter control sbr reactor device in the 0.5-2.0mg/l scope.

(3) precipitation: percolate is in sbr reactor device precipitation 1-4h, draining behind the aerobic aeration;

(4) mud stops: the mud in the sbr reactor device stopped in reactor 30～40 days.

Transmission technology can be reduced to:

(1) aerobic aeration: anaerobism stirs the back and by micropore aeration pipe and topping-up pump percolate is carried out aerobic aeration 2-6h, and by the Flow-rate adjustment of aeration, the control gas-water ratio is 1: 1-1: 2.5;

(2) precipitation: percolate is in sbr reactor device precipitation 2-6h, draining behind the aerobic aeration;

(3) mud stops: the mud in the sbr reactor device stopped in reactor 30～40 days.

Be illustrated in figure 3 as COD, ammonia nitrogen removal effect before comprehensive technical is optimized.Influent concentration fluctuates between the 3061mg/L at 1207mg/L before the technology Modification, and effluent COD concentration fluctuates between the 429mg/L at 272mg/L, and average effluent COD concentration and average COD removal are respectively 348.71mg/L, 82.34%; The reactor effluent COD concentration still is higher than national grade ii standard 300mg/L, and after technological transformation was optimized, effluent COD concentration decreased, but still a little higher than 300mg/L mainly is because there is not biodegradable in a large number COD material in the aged percolate from garbage filling field.NH before and after adopting new technology ₄ ⁺-N water inlet mean concns is respectively 767.78mg/L and 609.64mg/L, water outlet NH ₄ ⁺-N mean concns is respectively 5.79mg/L and 1.65mg/L, and the removal effect gap is little, and all reliable and stable, water outlet NH ₄ ⁺-N mean concns all be better than national grade one discharge standard (≤15mg/l).But the T-N before and after the technological transformation alters a great deal, and before adopting new technology, the T-N clearance fluctuates between 19.07% to 41.50%, and average removal rate is 31.95%, as shown in Figure 4; After adopting new technology, the T-N clearance fluctuates between 70.21% to 83.37%, and average removal rate is 79.76%, than having improved 47.81% before the technological transformation optimization, illustrates that the denitrification effect is significantly increased, as shown in Figure 5.Should realize efficient while nitration denitrification denitrogenation in many group sbr reactor devices.

Embodiment 3

Be bulky refuse landfill yard percolate sbr reactor pond, Guangzhou as shown in Figure 6, totally 2 SBR parallel connections.This refuse landfill was runed 4 years, so percolate concentration is higher, so at first adopt anaerobic mud bed (UASB) to carry out anaerobic treatment in front, SBR pond, with the former water COD of suitable reduction concentration, with the COD/N of this type of waste water than remaining on suitable scope (3.1-8.9); Then, adopt above-mentioned optimization technology that the SBR debugging of this project example is optimized with operation, aeration phase has been obtained good result by adjusting aerator control dissolved oxygen concentration at 2.0-2.5mg/L.

After the SBR bio-reactor operation sludge acclimatization debugging, beginning to adopt A/O technology to handle, is further optimization process effect, and COD removal and ammonia nitrogen removal are used (A/O) instead after the steady stage ²Technology, each moves 1 month.

Wherein the concrete grammar of A/O technology is:

A kind of percolate, comprises the steps and processing condition by A/O technology while nitrification and denitrification method at the sbr reactor device:

(1) anaerobism stirs:, start agitator percolate is carried out anaerobism stirring 1-4h through being pumped into bio-reactor from the percolate in the equalizing tank, rotating speed is 20～30rpm; COD/N when percolate enters the sbr reactor device is 5.0-7.0 than scope, crosses by control front UASB (up-flow anaerobic sludge blanket) level of response or at COD/N to add certain two liquid dungs when low or methyl alcohol is regulated and controlled.

(2) aerobic aeration: anaerobism stirs the back and by micropore aeration pipe and topping-up pump percolate is carried out aerobic aeration 2-7h, and by the Flow-rate adjustment of aeration, the control gas-water ratio is 1: 1-1: 2.5;

In the described control sbr reactor device percolate dissolved oxygen concentration by percolate dissolved oxygen concentration in the adjustments of gas under meter control sbr reactor device in the 0.5-2.0mg/l scope.

(3) precipitation: percolate is in sbr reactor device precipitation 1-4h, draining behind the aerobic aeration;

(4) mud stops: the mud in the sbr reactor device stopped in reactor 30～40 days.

As Fig. 7, Figure 8 shows that SBR is by optimizing COD, the NH that technology is debugged ₄ ⁺-N removal effect.As seen from Figure 7, in a year of commissioning test, SBR water inlet COD change in concentration is very big, fluctuate between the 12000mg/L at 1980mg/L, but effluent COD concentration is controlled at below the 1000mg/L, the COD average removal rate is respectively 83.9%, the highest clearance is 96.0%, sbr reactor device effluent COD concentration is lower than national grade III Standard 1000mg/L, reached design requirements, after entering the micro-filtration and reverse osmosis advanced processing of follow-up flow process, effluent COD concentration is controlled at 1000mg/L, reaches national grade one discharge standard, and can realize reuse.As seen from Figure 8, in nearly a year of commissioning test, the SBR NH of intaking ₄ ⁺-N concentration is very big with seasonal variation, fluctuates between the 1798mg/L at 0mg/L, but water outlet NH ₄ ⁺N concentration is controlled at below the 5mg/L, in most cases water outlet NH ₄ ⁺-N concentration is lower than detectability, is 0mg/L, and the highest clearance is 100%, and stable and reliable operation, water outlet NH ₄ ⁺-N mean concns all be better than national grade one discharge standard (≤15mg/l).Illustrate that this sbr reactor device operation process has good nitrification effect.

But, because percolate exists variation water quality big, when this SBR water inlet COD/N is low, there is the unfavorable problem of denitrification, classify the NH of SBR system Inlet and outlet water in some month as table 2 ₄ ⁺-N, NO ₃ ^--N concentration value.

Certain month main Inlet and outlet water data of SBR of table 2

Be not difficult to find out: water inlet COD/N ratio is 6.22, and the COD clearance is 88.9%, and nitrated rate is 100%, and the denitrification rate is 66.4%.Average water outlet NO ₃-N concentration is up to 269.7mg/l.

By further optimization technological operation, control influent quality and DO concentration, the denitrification effect can be greatly improved.As shown in table 3 for process optimization stable after, the NH of SBR system Inlet and outlet water in some month ₄ ⁺-N, NO ₃ ^--N concentration value.

Table 3 is further optimized certain month main Inlet and outlet water data of SBR in operation back

Be not difficult to find out: after technology was further optimized, water inlet average COD/N ratio rose to 7.42, and the COD clearance is 90.4%, and nitrated rate still is 100%, and the denitrification rate rises to 97.82%, average water outlet NO ₃-N concentration is reduced to 19.7mg/l significantly.

Reached good while nitration denitrification effect.

Be noted that because garbage seeping water is complicated and changeable, and this efficient SND denitrogenation is difficult for long term maintenance, need according to the optimization operational conditions of the technical solution of the present invention adjustment SBR that runs quickly, just can accomplish according to practical situation.

Claims (6)

1. a percolate is characterized in that comprising the steps and processing condition at sbr reactor device while nitrification and denitrification method:

(1) anaerobism stirs:, start agitator percolate is carried out anaerobism stirring 1-4h through being pumped into bio-reactor from the percolate in the equalizing tank, rotating speed is 20～30rpm;

(2) aerobic aeration: anaerobism stirs the back and by micropore aeration pipe and topping-up pump percolate is carried out aerobic aeration 2-7h, and by the Flow-rate adjustment of aeration, the control gas-water ratio is 1: 1-1: 2.5;

(3) precipitation: percolate is in sbr reactor device precipitation 1-4h, draining behind the aerobic aeration;

(4) mud stops: the mud in the sbr reactor device stopped in reactor 30～40 days.

2. percolate according to claim 1 is at sbr reactor device nitrification and denitrification method simultaneously, it is characterized in that COD/N when described percolate enters the sbr reactor device is than (5.0-7.0): 1

3. percolate according to claim 1 is characterized in that by percolate dissolved oxygen concentration in the adjustments of gas under meter control sbr reactor device in the 0.5-2.0mg/l scope at sbr reactor device while nitrification and denitrification method.

4. a percolate is characterized in that comprising the steps and processing condition at sbr reactor device while nitrification and denitrification method:

(1) anaerobism stirs:, start agitator percolate is carried out anaerobism stirring 1-5h through being pumped into bio-reactor from the percolate in the equalizing tank, rotating speed is 20～30rpm;

(2) aerobic aeration: anaerobism stirs the back and by micropore aeration pipe and topping-up pump percolate is carried out aerobic aeration 2-10h, and by the Flow-rate adjustment of aeration, the control gas-water ratio is 1: 1-1: 2.5;

(3) the secondary anaerobism stirs; Stir 1-4h; Agitator speed is 20～30rpm;

(4) secondary aerobic aeration: aerobic aeration 1-6h

(5) precipitation: percolate is in sbr reactor device precipitation 1-2h, draining behind the aerobic aeration;

(6) mud stops: the mud in the sbr reactor device stopped in reactor 30～40 days.

5. percolate according to claim 4 is at sbr reactor device while nitrification and denitrification method, it is characterized in that the COD/N when described percolate enters the sbr reactor device is 5.0-7.0 than scope, cross by control UASB level of response or at COD/N and add liquid dung when low or methyl alcohol is regulated and controlled.

6. percolate according to claim 4 is characterized in that by percolate dissolved oxygen concentration in the adjustments of gas under meter control sbr reactor device in the 0.5-2.0mg/l scope at sbr reactor device while nitrification and denitrification method.

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