CN103601347B - Domestic sewage treatment method and UAFB-EGSB coupled system quick start method - Google Patents

Domestic sewage treatment method and UAFB-EGSB coupled system quick start method Download PDF

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CN103601347B
CN103601347B CN201310653598.XA CN201310653598A CN103601347B CN 103601347 B CN103601347 B CN 103601347B CN 201310653598 A CN201310653598 A CN 201310653598A CN 103601347 B CN103601347 B CN 103601347B
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uafb
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CN103601347A (en
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高大文
丛岩
黄晓丽
王小龙
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Beijing University of Civil Engineering and Architecture
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Harbin Institute of Technology
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Abstract

The invention relates to a sewage treatment method and a UAFB-EGSB coupled system quick start method, particularly a domestic sewage treatment method and a UAFB-EGSB coupled system quick start method. The quick start method comprises the following steps: 1. connecting a UAFB reactor with an EGSB reactor; 2. adding activated sludge into the reactors; 3. performing a first start stage; and 4. performing a second start stage, thereby completing the quick start of the UAFB-EGSB coupled system. The domestic sewage treatment method comprises the following steps: 1. introducing domestic sewage into the UAFB reactor; and 2. introducing effluent water of the UAFB reactor into the EGSB reactor, thereby implementing domestic sewage treatment. The methods are suitable for the field of sewage treatment.

Description

The quick start method of the treatment process of one way of life sewage and UAFB-EGSB coupled system
Technical field
The present invention relates to a kind for the treatment of process of sewage and the quick start method of UAFB-EGSB coupled system.
Background technology
Water is the necessary irreplaceable a kind of resources of the mankind, is one of mainstay of social sustainable development.Water scarcity, energy shortage and Greenhouse effect become mankind's outstanding problem urgently to be resolved hurrily.And domestic town domestic sewage total emission volumn is large, effluent quality becomes increasingly complex, and how by domestic sewage resource utilization and to reach reuse standard be the important channel that solves water resources shortage, becomes gradually the focus of research.
Mainly to adopt activated sludge process to the treatment process of sanitary sewage, along with constantly bringing forth new ideas and Introduced From Abroad advanced person's technology of researcher, also there is a lot of new technique for the processing of sanitary sewage, as cyclic activated sludge system, SBR treatment process, MBR treatment process, oxidation ditch process, stabilization pond etc.Also be accompanied by and occur some problems simultaneously, as the energy consumption aspect of process operation, Yang Lingbo etc. are to China's more than 500 Sewage Plant in 2006 energy consumption analysis of disposing of sewage, reach a conclusion, China's urban wastewater treatment firm is processed the sanitary sewage mean consumption electric energy 0.28kWh of a cubic metre, running cost is increased, wasted the unnecessary energy.In addition, adopt aerobic treatment method, although fine to the treatment effect of sewage, can produce a large amount of excess sludges, for processing and the same increase running cost of disposal of mud, even can cause secondary pollution to environment.
Anaerobic Microbiological Treatment Technology is because operation is simple, cost is low, and sludge quantity is few, can reclaim again energy gas, and have very high volumetric loading, becomes the main treatment process of high concentrated organic wastewater.Anaerobic Microbiological Treatment Technology is fine to the COD removal effect in sanitary sewage, but very low to the clearance of nitrogen, so back segment will add aerobic treatment method to remove the nitrogen in sewage conventionally, but also need to add carbon source, and resource has been caused to waste.If Anaerobic Microbiological Treatment Technology and nitration denitrification coupling, need organism for denitrifying bacterium provides carbon source, also can produce greenhouse gases carbonic acid gas.
So, not yet have more satisfactory domestic sewage processing method at present.
Summary of the invention
The present invention is the problem of various deficiencies that exists in order to solve current domestic sewage processing method, and a kind for the treatment of process that is better than existing sanitary sewage disposal effect is provided.
UAFB-EGSB coupled system of the present invention starts according to the following steps fast:
One, UAFB reactor is connected with EGSB reactor, the water outlet of UAFB reactor is the water inlet of EGSB reactor;
Two, in UAFB reactor, add anaerobically digested sludge, in EGSB reactor, add AOB-ANAMMOX granule sludge;
Three, start the first stage, to the combined sewage that passes into simulated domestic wastewater and real life sewage in UAFB-EGSB coupled system, simulated domestic wastewater and real life sewage ratio are 100%-n5%:n5%, and n is startup first stage days running;
Four, start subordinate phase, in UAFB-EGSB coupled system, pass into real life sewage, starting subordinate phase days running is 7～9 days; Complete the quick startup of UAFB-EGSB coupled system;
Wherein, in step 3, the main component of simulated domestic wastewater is: anhydrous sodium acetate 133mg/L, ammonium chloride 145mg/L, potassium primary phosphate 44mg/L, magnesium sulfate 53mg/L, Calcium Chloride Powder Anhydrous 13mg/L, urea 30mg/L and micro-0.67mL/L;
It is 14～16 days that step 3 starts first stage days running;
In step 3 and four, the control of UAFB reactor temperature is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h; In step 3 and four, the control of UAFB reactor temperature is 30 ± 2 DEG C, hydraulic detention time is 6 ± 0.2h, the Recycle design that EGSB inside reactor adopts aeration 1h, stop aeration 1h is carried out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 150～250mL/min in EGSB reactor reaction zone.
Sanitary sewage passes into the UAFB-EGSB coupled system that success starts fast as stated above and carries out sanitary sewage disposal:
One, sanitary sewage passes into UAFB reactor, and the control of UAFB reactor temperature is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h, then water outlet;
Two, the water outlet of UAFB reactor is passed into EGSB reactor, the control of EGSB reactor temperature is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h, EGSB inside reactor intermittently decline oxygen aeration, then water outlet; Realize the processing of sanitary sewage;
The Recycle design that adopt aeration 1h in step 2, stops aeration 1h is carried out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 150～250mL/min in reaction zone.
The disposal methods 1m of sanitary sewage of the present invention 3sanitary sewage mean consumption electric energy 0.171kWh, saves the energy.
The treatment process excess sludge production of sanitary sewage of the present invention is low, is only 12.63mg/d, has reduction cost of water treatment, is difficult for causing the advantage of secondary pollution.In the treatment process of sanitary sewage of the present invention, do not comprise aerobic treatment, without adding carbon source.
UAFB-EGSB coupled system of the present invention starts fast needs about 23 days, the COD in sanitary sewage and total nitrogen is synchronously removed after starting successfully, and COD clearance is more than 85%, and nitrogen removal rate is more than 65%.
Brief description of the drawings
Fig. 1 is UAFB-EGSB coupled system schematic diagram, and wherein 1 is water inlet bucket, and 2 is peristaltic pump, 3 is UAFB reactor, and 3-1 is UAFB reactor filler, and 4 is EGSB reactor, 8 is temperature controller, 9 is air collector, and 10 is wet test meter, and 11 is settling tank, 4-1 is EGSB reactor aeration bar, 4-2 is EGSB reactor refluxing opening, and 17 is aeration pump, and 18 for going out bucket.
Fig. 2 is the graphic representation of UAFB-EGSB coupled system COD clearance in embodiment 1 performance during rapid starting period.
Fig. 3 is the graphic representation of various VFA content in the water outlet of UAFB-EGSB coupled system in embodiment 1 performance during rapid starting period.
Fig. 4 is the change curve of TN concentration in the water outlet of UAFB-EGSB coupled system in embodiment 1 performance during rapid starting period.
Fig. 5 is NH in the water outlet of UAFB-EGSB coupled system in embodiment 1 performance during rapid starting period 4 +the change curve of-N concentration.
Fig. 6 is NO in the water outlet of UAFB-EGSB coupled system in embodiment 1 performance during rapid starting period 2 --N and NO 3 -the change curve of-N concentration.
Fig. 7 is COD concentration curve in embodiment 2 sanitary sewage disposal process UAFB-EGSB coupled systems.
Fig. 8 is TN concentration curve in embodiment 2 sanitary sewage disposal process UAFB-EGSB coupled systems.
Fig. 9 is NH in embodiment 2 sanitary sewage disposal process UAFB-EGSB coupled systems 4 +-N concentration curve.
Figure 10 is NO in embodiment 2 sanitary sewage disposal process UAFB-EGSB coupled systems 2 --N and NO 3 --N concentration curve.
Embodiment
Technical solution of the present invention is not limited to following cited embodiment, also comprises the arbitrary combination between each embodiment.
Embodiment one: in conjunction with Fig. 1, present embodiment is described, present embodiment UAFB-EGSB coupled system starts according to the following steps fast:
One, UAFB reactor 3 is connected with EGSB reactor 4, the water outlet of UAFB reactor is the water inlet of EGSB reactor;
Two, the interior interpolation anaerobically digested sludge of UAFB reactor 3, the interior interpolation of EGSB reactor 4 AOB-ANAMMOX granule sludge;
Three, start the first stage, to the combined sewage that passes into simulated domestic wastewater and real life sewage in UAFB-EGSB coupled system, simulated domestic wastewater and real life sewage ratio are 100%-n5%:n5%, and n is startup first stage days running;
Four, start subordinate phase, in UAFB-EGSB coupled system, pass into real life sewage, starting subordinate phase days running is 7～9 days; Complete the quick startup of UAFB-EGSB coupled system;
Wherein, in step 3, the main component of simulated domestic wastewater is: anhydrous sodium acetate 133mg/L, ammonium chloride 145mg/L, potassium primary phosphate 44mg/L, magnesium sulfate 53mg/L, Calcium Chloride Powder Anhydrous 13mg/L, urea 30mg/L and micro-0.67mL/L;
It is 14～16 days that step 3 starts first stage days running;
In step 3 and four, the control of UAFB reactor temperature is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h; In step 3 and four, the control of UAFB reactor temperature is 30 ± 2 DEG C, hydraulic detention time is 6 ± 0.2h, the Recycle design that EGSB inside reactor adopts aeration 1h, stop aeration 1h is carried out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 150～250mL/min in reaction zone.
It is as shown in table 1 below that present embodiment starts real life sewage (100%) water quality of using fast:
Table 1
Project Content (mg/L) Mean value (mg/L) Project Content (mg/L) Mean value (mg/L)
COD 104.9～408.4 194.5 TN 32.3～56.55 42.9
PO 4 2- 10.32～26.25 20.43 NH 4 +-N 14.98～59.92 41.24
Cl -1 115.2～140.3 130.6 NO 2 --N 0～0.39 0.085
pH 7.14～7.82 7.45 NO 3 --N 0～2.69 0.55
EGSB(Expanded Granular Sludge Bed) reactor is the third generation ultra-high efficiency anaerobic reactor of developing on the basis of up-flow anaerobic sludge blanket (UASB) reactor, and organism is had to good removal effect, is mainly used in removing COD.
Present embodiment is coupled two anaerobic reactors, and EGSB reactor can further reduce the COD in sewage in the present embodiment, has more effectively reduced the total nitrogen in water; And EGSB reactor in the process of denitrogenating without additionally adding carbon source.
AOB-ANAMMOX granule sludge in present embodiment step 2 is cultivated according to the following steps:
One, add ANAMMOX granule sludge in EGSB reactor, then pass into nitrogenous simulated wastewater, and the nitrogenous simulated wastewater nitrogen that exposes to the sun is made to drop to gradually 1.0mg/L in water dissolved oxygen concentration 24h; Be 33 ± 2 DEG C in temperature, hydraulic detention time is 2.3h, under the condition that in EGSB reactor, upflow velocity is 7m/h, cultivates 26～28 days;
Two, carry out micro-oxygen aeration to entering the nitrogenous simulated wastewater of EGSB reactor, control dissolved oxygen concentration is 1.2 ± 0.3mg/L; Be 33 ± 2 DEG C in temperature, hydraulic detention time is 2.3h, under the condition that in EGSB reactor, upflow velocity is 7m/h, cultivates 41～43 days;
Three, carry out micro-oxygen aeration to entering the nitrogenous simulated wastewater of EGSB reactor, aeration rate is 150mL/min; Be 33 ± 2 DEG C in temperature, hydraulic detention time is 2.3h, under the condition that in EGSB reactor, upflow velocity is 7m/h, cultivates 26～28 days;
Four, the Recycle design that adopt aeration 1h to entering the nitrogenous simulated wastewater of EGSB reactor, stops aeration 1h is carried out the oxygen aeration that declines intermittence, and aeration rate is 200mL/min; Be 33 ± 2 DEG C in temperature, hydraulic detention time is 4h, under the condition that in EGSB reactor, upflow velocity is 7m/h, cultivates 10～12 days, obtains AOB-ANAMMOX granule sludge;
Wherein, in step 1, to keep ammonia nitrogen concentration in nitrogenous simulated wastewater be 240 ± 5mg/L, keep nitrogenous simulated wastewater nitrogen concentration of nitrite is 273 ± 5mg/L;
In step 2, to keep ammonia nitrogen concentration in nitrogenous simulated wastewater be 240 ± 5mg/L, keep nitrogenous simulated wastewater nitrogen concentration of nitrite is 273 ± 5mg/L;
In step 3, keep ammonia nitrogen concentration in nitrogenous simulated wastewater to be 240 ± 5mg/L, nitrogenous simulated wastewater nitrogen concentration of nitrite is reduced to 0mg/L gradually by 273 ± 5mg/L;
In step 4, ammonia nitrogen concentration in nitrogenous simulated wastewater being gradually reduced to 50mg/L, keeping nitrogenous simulated wastewater nitrogen concentration of nitrite is 0～25mg/L.
NH in nitrogenous simulated wastewater 4the concentration of Cl is 97.5～900mg/L, NaNO 2concentration be 127.7～1352mg/L, KHCO 3concentration be 1000mg/L, KH 2pO 4concentration be 50mg/L, MgSO 47H 2the concentration of O is 200mg/L, CaCl 22H 2the concentration of O is that the concentration of 151mg/L, VITAMIN is that 0.25ml/L, micro-concentration are 0.31ml/L.
Embodiment two: the difference of present embodiment and embodiment one is: in step 2, the effective volume of UAFB reactor 3 is 2.55L, the addition of anaerobically digested sludge is 300～450mL.Other step and parameter are identical with embodiment one.
Anaerobically digested sludge is from the UASB reactor of Harbin Institute of Technology's city water resource and water surrounding National Key Laboratory.
Embodiment three: the difference of present embodiment and embodiment one or two is: in step 2, the effective volume of EGSB reactor 4 is 1.53L, reaction zone volume is 1L, settling region volume is 0.53L, and the addition of AOB-ANAMMOX granule sludge is 250～350mL.Other step and parameter are identical with embodiment one or two.
Embodiment four: the difference of present embodiment and embodiment one, two or three is: in step 2, the effective volume of UAFB reactor 3 is 2.55L, and reaction zone volume is 2.0L, and settling region volume is 0.55L; In UAFB reactor 3, filler is housed, packing volume is 1.0L.Other step and parameter are identical with embodiment one, two or three.
The present embodiment UAFB-EGSB coupled system amount of disposing of sewage every day is 6.0L, and UAFB reactor reaction zone internal diameter is 80mm, and upflow velocity is 0.05m/h.
Present embodiment filler is the circular annular packing of diameter 10mm.
Embodiment five: the difference of one of present embodiment and embodiment one to four is: in step 2, the aspect ratio of EGSB reactor 4 is 20.Other step and parameter are identical with one of embodiment one to four.
Embodiment six: the difference of one of present embodiment and embodiment one to five is: regulate EGSB reactor outer circulation ratio in step 3 and four, control upflow velocity is 6.0～9.0m/h.Other step and parameter are identical with one of embodiment one to five.
The present embodiment UAFB-EGSB coupled system amount of disposing of sewage every day is 6.0L, EGSB reactor reaction zone internal diameter is 40mm, after calculating, upflow velocity is only 0.2m/h, but in order to ensure the swelling state of granule sludge, need to keep certain upflow velocity, therefore in step 3 and four, regulate EGSB reactor outer circulation ratio, control upflow velocity is 6.0～9.0m/h.
Embodiment seven: sanitary sewage passes into the UAFB-EGSB coupled system life starting fast by method success described in concrete enforcement one and carries out sewage disposal:
One, sanitary sewage passes into UAFB reactor 3, and the interior temperature control of UAFB reactor 3 is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h, then water outlet;
Two, the water outlet of UAFB reactor is passed into EGSB reactor 4, the interior temperature control of EGSB reactor 4 is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h, EGSB inside reactor intermittently decline oxygen aeration, then water outlet; Realize the processing of sanitary sewage;
The Recycle design that adopt aeration 1h in step 2, stops aeration 1h is carried out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 150～250mL/min in EGSB reactor reaction zone.
Present embodiment be applicable to process low ratio of carbon to ammonium, both COD below 450mg/L, the sanitary sewage of ammonia nitrogen below 60mg/L.
Embodiment eight: the difference of present embodiment and embodiment seven is: regulate EGSB reactor outer circulation ratio in step 2, control upflow velocity is 6.0～9.0m/h.Other step and parameter are identical with embodiment seven.
The present embodiment UAFB-EGSB coupled system amount of disposing of sewage every day is 6.0L, EGSB reactor reaction zone internal diameter is 40mm, after calculating, upflow velocity is only 0.2m/h, but in order to ensure the swelling state of granule sludge, need to keep certain upflow velocity, therefore in step 3 and four, regulate EGSB reactor outer circulation ratio, control upflow velocity is 6.0～9.0m/h.
Embodiment 1
UAFB-EGSB coupled system starts according to the following steps fast:
One, UAFB reactor 3 is connected with EGSB reactor 4, the water outlet of UAFB reactor is the water inlet of EGSB reactor;
Two, the interior interpolation anaerobically digested sludge of UAFB reactor 3, the interior interpolation of EGSB reactor 4 AOB-ANAMMOX granule sludge;
Three, start the first stage, to the combined sewage that passes into simulated domestic wastewater and real life sewage in UAFB-EGSB coupled system, simulated domestic wastewater and real life sewage ratio are 100%-n5%:n5%, and n is startup first stage days running;
Four, start subordinate phase, in UAFB-EGSB coupled system, pass into real life sewage, starting subordinate phase days running is 8 days; Complete the quick startup of UAFB-EGSB coupled system;
Wherein, in step 3, the main component of simulated domestic wastewater is: anhydrous sodium acetate 133mg/L, ammonium chloride 145mg/L, potassium primary phosphate 44mg/L, magnesium sulfate 53mg/L, Calcium Chloride Powder Anhydrous 13mg/L, urea 30mg/L and micro-0.67mL/L;
It is 15 days that step 3 starts first stage days running;
In step 3 and four, the control of UAFB reactor temperature is 30 DEG C, and hydraulic detention time is 6h; In step 3 and four, the control of UAFB reactor temperature is 30 DEG C, hydraulic detention time is 6h, the Recycle design that EGSB inside reactor adopts aeration 1h, stop aeration 1h is carried out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 200mL/min in reaction zone.
The COD value that the present embodiment starts the real life sewage of using fast fluctuates between 177.6～414.3mg/L, and COD value is on average more than 200mg/L; The total nitrogen value of real life sewage fluctuates between 32.3～56.55mg/L, and mean value is more than 42mg/L.
In the present embodiment step 2, the effective volume of UAFB reactor 3 is 2.55L, and reaction zone volume is 2.0L, and settling region volume is 0.55L, and the addition of anaerobically digested sludge is 300～450mL, in UAFB reactor 3, filler is housed, and packing volume is 1.0L.
In the present embodiment step 2, the effective volume of EGSB reactor 4 is 1.53L, and reaction zone volume is 1L, and settling region volume is 0.53L, and the aspect ratio of EGSB reactor is that the addition of 20, AOB-ANAMMOX granule sludge is 250～350mL.
In the present embodiment step 3 and four, regulate EGSB reactor outer circulation ratio, control upflow velocity is 6.0～9.0m/h.
In the present embodiment performance during rapid starting period, UAFB-EGSB coupled system COD clearance as shown in Figure 2.The present embodiment start first stage UAFB-EGSB coupled system to the clearance of COD more than 80%.UAFB reactor stable, has reduced the operating pressure to EGSB reactor, has ensured that UAFB-EGSB coupled system has very strong water resistant profit impact capacity.
In performance during rapid starting period, the average effluent COD of UAFB reactor is 48.3mg/L, and the average effluent COD of EGSB reactor is 30.0mg/L, and visible UAFB reactor water outlet has met national town domestic sewage discharge water quality one-level A standard.In EGSB reactor, mainly taking ammonia oxidizing bacteria (AOB bacterium) and anaerobic ammonia oxidizing bacteria (ANAMMOX bacterium) as main, COD is had to removal effect more than 15mg/L, reason is that ANAMMOX bacterium has utilized part small molecular organic acid to cause the removal of COD.
In the present embodiment performance during rapid starting period, in the water outlet of UAFB-EGSB coupled system, the content of various VFA is as shown in Figure 3.In the water outlet of the water outlet of UAFB reactor and EGSB reactor, the amount of VFA is taking acetic acid and propionic acid as main, and the content of butyric acid and valeric acid does not almost have.Comparison diagram 2 finds out that the increase of influent COD directly causes the increase of water outlet VFA content, illustrates that the COD major part of water outlet is VFA.The mean value that starts acetic acid, propionic acid, butyric acid, valeric acid in the water outlet of first stage UAFB reactor is respectively 17.35mg/L, 9.61mg/L, 1.07mg/L, 0.554mg/L, and in the water outlet of EGSB reactor, the mean value of acetic acid, propionic acid, butyric acid, valeric acid is respectively 11.05mg/L, 1.688mg/L, 0.443mg/L, 0.195mg/L.The mean value that starts acetic acid, propionic acid, butyric acid, valeric acid in the water outlet of subordinate phase UAFB reactor is respectively 15.99mg/L, 8.55mg/L, 1.098mg/L, 0.72mg/L, and in the water outlet of EGSB reactor, the mean value of acetic acid, propionic acid, butyric acid, valeric acid is respectively 8.85mg/L, 3.0mg/L, 0.856mg/L, 0.56mg/L.Illustrate in EGSB reactor, butyric acid and valeric acid be utilized seldom, and the clearance of propionic acid will be higher than the clearance of acetic acid, analysis is that propionic acid will first be decomposed into acetic acid while being utilized by microorganism, so acetic acid is existing be consumed also have a generation, cause the clearance to reduce.
In the present embodiment, UAFB reactor is mainly used in removing the COD in sanitary sewage, and ammonia nitrogen in sanitary sewage is mainly consumed utilization by the AOB bacterium in EGSB reactor and ANAMMOX bacterium synergy, is converted into nitrogen.In the present embodiment performance during rapid starting period, in the water outlet of UAFB-EGSB coupled system, the concentration of TN is as shown in Figure 4.UAFB reactor is not only removed total nitrogen, the total nitrogen outline of water outlet is higher than the total nitrogen of water inlet on the contrary, and reason is that under anaerobic condition, nitrobacteria is difficult to existence, and only has ammonia nitrogen in water inlet, lack the necessary substrate of denitrifying bacterium, so total nitrogen is not had to removal effect; In sanitary sewage, contain the compositions such as protein simultaneously, after anaerobic hydrolysis-acidification, be not decomposed into the small-molecule substances such as amino acid, increased the content of water outlet total nitrogen.Start the combined sewage that first stage water inlet is simulated wastewater and real life sewage, water inlet total nitrogen fluctuates within the scope of 41.61～56.55mg/L, the change that startup has just started environment is larger on the impact of EGSB reactor, the clearance of total nitrogen only has 30% left and right, it is mainly the activity that the flip-flop of influent quality has affected granule sludge, granule sludge conforms gradually subsequently, and the clearance of total nitrogen is brought up to more than 80%, and water outlet total nitrogen is reduced to below 10mg/L.The real life sewage that startup subordinate phase is 100%, within the 16th day, the total nitrogen that starts to intake is elevated to 55.4mg/L from 46.3mg/L gradually, and water outlet total nitrogen is also in continuous rising, treatment effect drops to below 60%, illustrate that now the anti-volumetric loading ability of EGSB reactor is poor, the fluctuation of influent quality has a strong impact on AOB-ANAMMOX granule sludge removing nitrogen.Within the 23rd day, reactor is basicly stable, and water outlet total nitrogen maintains 12mg/L left and right.
NH in the water outlet of UAFB-EGSB coupled system in the present embodiment performance during rapid starting period 4 +the concentration of-N as shown in Figure 5.The rising of UAFB reactor water outlet total nitrogen is mainly the increase of ammonia nitrogen concentration, and that EGSB reactor is affected by change of water quality is larger, major cause is the activity decreased of ANAMMOX bacterium, while causing just adding part real life sewage, the clearance of ammonia nitrogen drops to below 40%, EGSB reactor has adapted to the change of environment gradually subsequently, and the clearance of ammonia nitrogen constantly rises to 80%.After the 16th day, water inlet is 100% sanitary sewage, and water outlet ammonia nitrogen concentration is below 10mg/L, and the 24th day water outlet ammonia nitrogen concentration, below 5mg/L, illustrates that AOB-ANAMMOX granule sludge synergy has played excellent ammonia nitrogen removal effect.
NO in the water outlet of UAFB-EGSB coupled system in the present embodiment performance during rapid starting period 2 --N and NO 3 -the concentration of-N as shown in Figure 6.Start first 6 days of first stage, nitrite nitrogen in the water outlet of UAFB-EGSB coupled system and nitrate nitrogen are below 1.0mg/L, major cause is in water, there is no nitrite nitrogen and nitrate nitrogen, ANAMMOX bacterium activity is suppressed simultaneously, nitrate nitrogen does not almost accumulate, and nitrate nitrogen accumulates to some extent subsequently, and water inlet is afterwards 100% real life sewage to start the 16th day, water outlet nitrate nitrogen mean value is 6.1mg/L, and water outlet does not almost have nitrite nitrogen.
The present embodiment UAFB-EGSB coupled system is got EGSB reactor endoparticle mud and is done fish analysis and TEM (transmission electron microscope) analysis after starting fast successfully.AOB bacterium and a small amount of nitrifier (NOB) are on the top layer of granule sludge, consume the dissolved oxygen in water, and be nitrite nitrogen by the ammonia nitrogen Partial Conversion in sanitary sewage, for inner ANAMMOX bacterium provides anaerobic environment and necessary matrix substrate, thereby reach the effective removal to nitrogen in sanitary sewage.AOB bacterium quantitatively has very large growth compared with before starting, and reason is that AOB is with CO 2for carbon source is carried out autophyting growth, simultaneously also can carry out taking organism as carbon source mixture growth, and enter COD concentration in the sewage of EGSB reactor and, in 45mg/L left and right, for AOB bacterium provides organism, accelerated the breeding of AOB bacterium.
Transmission electron microscope observing is various to EGSB reactor endoparticle mud outer microtube biomorph, more complicated than startup flora structure in period first stage, has a large amount of bacillus to occur, length is at 3.0～4.0 μ m, and analysis may be denitrifying bacterium.Amplify granule sludge is outer local, still can observe the cell that much meets AOB bacterium morphological specificity, and other circular microbial morphology be similar to ANAMMOX bacterium, side light enter the reason of ammonia nitrogen removal after real life sewage.In the inside of granule sludge, cellular form is basically identical, is illustrated as a kind of microorganism, only has the shaft-like microorganism of only a few, and visible particle mud has very strong adaptive faculty to the sanitary sewage of water quality complexity.Have in granule sludge inside in significantly " gully ", these " gullies " may be that the nitrogen that anaerobic ammonia oxidizing bacteria produces flocks together from the pore of granule interior eliminating, are conducive to the transmission of matrix substrate in granule sludge inside simultaneously.
Embodiment 2
Sanitary sewage passes into the UAFB-EGSB coupled system life starting fast by method success described in concrete enforcement one and carries out sewage disposal:
One, sanitary sewage passes into UAFB reactor 3, and the interior temperature control of UAFB reactor 3 is 30 DEG C, and hydraulic detention time is 6h, then water outlet;
Two, the water outlet of UAFB reactor is passed into EGSB reactor 4, the interior temperature control of EGSB reactor 4 is 30 DEG C, and hydraulic detention time is 6h, EGSB inside reactor intermittently decline oxygen aeration, then water outlet; Realize the processing of sanitary sewage;
The Recycle design that adopt aeration 1h in step 2, stops aeration 1h is carried out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 150～250mL/min in EGSB reactor reaction zone.
In the present embodiment step 2, regulate EGSB reactor outer circulation ratio, control upflow velocity is 6.0～9.0m/h.
The sanitary sewage water quality of the present embodiment processing is as shown in table 2, and sanitary sewage adopts teaching and administrative staff living quarters, Harbin Industry University 2ed School District sanitary sewage.
Table 2
Project Content (mg/L) Mean value (mg/L) Project Content (mg/L) Mean value (mg/L)
COD 104.9～408.4 194.5 TN 32.3～56.55 42.9
PO 4 2- 10.32～26.25 20.43 NH 4 +-N 14.98～59.92 41.24
Cl -1 115.2～140.3 130.6 NO 2 --N 0～0.39 0.085
pH 7.14～7.82 7.45 NO 3 --N 0～2.69 0.55
In sanitary sewage disposal process water inlet and water outlet in COD concentration as shown in Figure 7.The inlet COD concentration of sanitary sewage fluctuates within the scope of 104.9～408.4mg/L, when UAFB-EGSB coupled system moves the 13rd day, influent COD is 136.1mg/L, the 14th day time, increase to suddenly 408.4mg/L, but do not affect the removal situation of UAFB reactor to COD, water outlet COD can be stabilized in below 50mg/L, the water outlet of observing EGSB reactor changes and can find out, the concentration of water outlet COD is all less than the water outlet of UAFB reactor, organism divides and is utilized at EGSB inside reactor, and UAFB-EGSB coupled system water outlet COD can maintain below 25mg/L.
In sanitary sewage disposal process water inlet and water outlet in TN concentration as shown in Figure 8.UAFB reactor does not have removal effect to total nitrogen, and reactor UAFB water outlet total nitrogen concentration is greater than into water total nitrogen concentration, be mainly that in anaerobic fermentation process, the protein in water inlet is broken down into small molecules amino acid, the meta-bolites after amino acid is utilized by cell raises total nitrogen concentration.The concentration of water inlet total nitrogen fluctuates within the scope of 32.3～56.55mg/L, and mean value is 42.9mg/L, the removal effect excellence of EGSB reactor to total nitrogen, and water outlet total nitrogen mean value is 12.92mg/L, has reached town domestic sewage discharge one-level A standard.
NH in water inlet and water outlet in sanitary sewage disposal process 4 +the concentration of-N as shown in Figure 9.NO in water inlet and water outlet in sanitary sewage disposal process 2 --N and NO 3 -the concentration of-N as shown in figure 10.Comparison diagram 9 and Figure 10, UAFB reactor water outlet total nitrogen, higher than water inlet total nitrogen concentration, is mainly the increase of ammonia nitrogen concentration.The water outlet ammonia nitrogen concentration of EGSB reactor is stabilized in 5mg/L left and right, and nitrate nitrogen has partial, and on average going out water concentration is 3.3mg/L, and UAFB-EGSB coupled system has and has excellent treatment effect sanitary sewage.

Claims (8)

  1. The quick start method of 1.UAFB-EGSB coupled system, is characterized in that UAFB-EGSB coupled system starts according to the following steps fast:
    One, UAFB reactor is connected with EGSB reactor, the water outlet of UAFB reactor is the water inlet of EGSB reactor;
    Two, in UAFB reactor, add anaerobically digested sludge, in EGSB reactor, add AOB-ANAMMOX granule sludge;
    Three, start the first stage, to the combined sewage that passes into simulated domestic wastewater and real life sewage in UAFB-EGSB coupled system, simulated domestic wastewater and real life sewage ratio are 100%-n5%:n5%, and n is startup first stage days running;
    Four, start subordinate phase, in UAFB-EGSB coupled system, pass into real life sewage, starting subordinate phase days running is 7～9 days; Complete the quick startup of UAFB-EGSB coupled system;
    Wherein, in step 3, the main component of simulated domestic wastewater is: anhydrous sodium acetate 133mg/L, ammonium chloride 145mg/L, potassium primary phosphate 44mg/L, magnesium sulfate 53mg/L, Calcium Chloride Powder Anhydrous 13mg/L, urea 30mg/L and micro-0.67mL/L;
    It is 14～16 days that step 3 starts first stage days running;
    In step 3 and four, the control of UAFB reactor temperature is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h; In step 3 and four, EGSB inside reactor adopts aeration 1h, the Recycle design that stops aeration 1h carries out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 150～250mL/min in reaction zone.
  2. 2. the quick start method of UAFB-EGSB coupled system according to claim 1, the effective volume that it is characterized in that UAFB reactor in step 2 is 2.55L, the addition of anaerobically digested sludge is 300～450mL.
  3. 3. the quick start method of UAFB-EGSB coupled system according to claim 1, the effective volume that it is characterized in that EGSB reactor in step 2 is 1.53L, reaction zone volume is 1L, and settling region volume is 0.53L, and the addition of AOB-ANAMMOX granule sludge is 250～350mL.
  4. 4. the quick start method of UAFB-EGSB coupled system according to claim 1, the effective volume that it is characterized in that UAFB reactor in step 2 is 2.55L, and reaction zone volume is 2.0L, and settling region volume is 0.55L; In UAFB reactor, filler is housed, packing volume is 1.0L.
  5. 5. the quick start method of UAFB-EGSB coupled system according to claim 3, the aspect ratio that it is characterized in that EGSB reactor in step 2 is 20.
  6. 6. the quick start method of UAFB-EGSB coupled system according to claim 1, is characterized in that regulating EGSB reactor outer circulation ratio in step 3 and four, and control upflow velocity is 6.0～9.0m/h.
  7. 7. the treatment process of one way of life sewage, is characterized in that sanitary sewage passes into the UAFB-EGSB coupled system successfully starting fast by method described in claim 1 and carries out sanitary sewage disposal:
    One, sanitary sewage passes into UAFB reactor, and the control of UAFB reactor temperature is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h, then water outlet;
    Two, the water outlet of UAFB reactor is passed into EGSB reactor, the control of EGSB reactor temperature is 30 ± 2 DEG C, and hydraulic detention time is 6 ± 0.2h, EGSB inside reactor intermittently decline oxygen aeration, then water outlet; Realize the processing of sanitary sewage;
    The Recycle design that adopt aeration 1h in step 2, stops aeration 1h is carried out the oxygen aeration that declines intermittence, when aeration, carries out aeration by the aeration rate of the every liter of volume 150～250mL/min in EGSB reactor reaction zone.
  8. 8. the treatment process of sanitary sewage according to claim 7, is characterized in that regulating EGSB reactor outer circulation ratio in step 2, and control upflow velocity is 6.0～9.0m/h.
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