CN104671410A - Method for further denitrifying high ammonia-nitrogen wastewater based on A/O (Anaerobic/Oxic) process - Google Patents
Method for further denitrifying high ammonia-nitrogen wastewater based on A/O (Anaerobic/Oxic) process Download PDFInfo
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- CN104671410A CN104671410A CN201510051225.4A CN201510051225A CN104671410A CN 104671410 A CN104671410 A CN 104671410A CN 201510051225 A CN201510051225 A CN 201510051225A CN 104671410 A CN104671410 A CN 104671410A
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- dissolved oxygen
- aeration tank
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- pond
- high ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
Abstract
The invention discloses a method for further denitrifying high ammonia-nitrogen wastewater based on an A/O (Anoxic/Oxic) process. The method comprises the following steps that: the high ammonia-nitrogen wastewater is treated through an improved A/O process, wherein the improved A/O process is that mud and water mixed solution at a dissolved oxygen jumping position of an aeration tank is used as nitrification solution and back flows into an anoxic tank on the basis of the traditional A/O process; at the same time, a carbon source is added at the dissolved oxygen jumping position of the aeration tank; and the dissolved oxygen jumping position is the position that the dissolved oxygen in the aeration tank is jumped from less than 0.5mg/L to more than 2mg/L. The method disclosed by the invention overcomes the bottleneck that the denitrification rate of the traditional A/O process is limited by a reflux ratio; the denitrification rate is high and can achieve 100%; outlet water COD (Chemical Oxygen Demand) is less than 50mg/L; and the method is simple to operate, wide in application range and can be put into industrial implementation easily.
Description
Technical field
The present invention relates to a kind of on A/O Process ba-sis the method to the further denitrogenation of high ammonia-nitrogen wastewater.
Background technology
For tackling the degeneration day by day of quality of water environment, environmental capacity is close to exhaustion, 2002, urban wastewater treatment firm was discharged total nitrogen limit value and is less than 15mg/L (the one-level A standard in " urban wastewater treatment firm pollutant emission standard " GB18918-2002) by China.In fact, according to existing result of study, when total nitrogen content is higher than 0.6mg/L, namely water body considered to be in eutrophic state, even if therefore meet existing total nitrogen emission standard, sewage enters natural water still can aggravate body eutrophication.Therefore, in water pollution, polluted by nitrogen rises to main polluted factors, controls total nitrogen quantity discharged imperative.To ammonia nitrogen and oxynitride, the Chinese government promises to undertake, during " 12 ", control discharge total amount cuts down 10% respectively, therefore can predict, in following 5 ~ 10 years, waste water total nitrogen emission standard can be further harsh.Particularly for chemical industry, coking, gas washing, nitrogenous fertilizer, food, monosodium glutamate, aquatic products, livestock and poultry, the industry or field that produce high ammonia-nitrogen wastewater such as to butcher, nitrogen emission reduction is more outstanding.
With regard to the concentrated emission control technique of the high ammonia-nitrogen wastewater of above-mentioned industry, A/O technique is widely used with its cheap construction cost and working cost.But it should be noted that, A/O technique is adopted to process, its denitrification percent is by the restriction (denitrification percent=R/ (R+1)) of reflux ratio R (reflux ratio herein refers to nitrification liquid and return sludge ratio sum), and water outlet total nitrogen content is still higher.Such as, certain high ammonia-nitrogen wastewater ammonia-nitrogen content is 500mg/L, and adopt A/O technique to carry out denitrogenation processing, reflux ratio R=4 routinely, theoretical denitrification percent is 80%, and in water outlet, total nitrogen content is 100mg/L; Even if denitrification percent reaches 95% (theoretical reflux ratio R=19), water outlet total nitrogen content is still at 25mg/L.Therefore, how to break through the restriction of denitrification percent by reflux ratio of A/O technique, improve the denitrification percent of A/O technique further, become a great problem of A/O process modification.And for the solution of an above-mentioned difficult problem, prior art is generally adopt independent denitrification technology to improve A/O technique, further denitrogenation is carried out to its water outlet.Denitrification technology wherein mainly contains SBR technique, denitrification granular sludge or fixed bed etc., but, these denitrification technology, add the complexity of A/O process system on the one hand, cost is high; On the other hand, after denitrification, remaining organism can bring secondary pollution.
Therefore, this area need badly a kind of newly on A/O Process ba-sis to the method for the further denitrogenation of high ammonia-nitrogen wastewater, to solve above-mentioned technical barrier.
Summary of the invention
Technical problem to be solved by this invention is the restriction of denitrification percent by reflux ratio in order to overcome existing A/O technique or its improving technique, water outlet total nitrogen content is high, denitrification percent is low, system complex and water outlet exist the defects such as secondary pollution, and provide a kind of on A/O Process ba-sis the method to the further denitrogenation of high ammonia-nitrogen wastewater.Method of the present invention overcomes the bottleneck of traditional A/O technique denitrification percent by reflux ratio restriction, and denitrification percent can reach 100%, and denitrification percent is high, and water outlet COD is lower than 50mg/L, simple to operate, applied widely, is easy to industrializing implementation.
The present invention solves above-mentioned technical barrier mainly through following technical scheme.
The invention provides a kind of on A/O Process ba-sis the method to the further denitrogenation of high ammonia-nitrogen wastewater, it comprises the following steps: the improving technique process of high ammonia-nitrogen wastewater through A/O,, wherein, the improving technique of described A/O is on traditional A/O Process ba-sis, and the muddy water mixed solution that aeration tank (O pond) dissolved oxygen rises to position (i.e. DO hop point) is back to anoxic pond (A pond) as nitrification liquid; Meanwhile, rise to position at the dissolved oxygen of aeration tank and add carbon source; Described dissolved oxygen rises to position and refers to that dissolved oxygen in aeration tank is less than 0.5mg/L by dissolved oxygen and rises to dissolved oxygen and be greater than position corresponding to 2mg/L.
Described dissolved oxygen rises to position and is generally positioned at O pond along water (flow) direction 75% ~ 85% position, and described per-cent (%) refers to that O pond starting point to O pond dissolved oxygen rises to the distance of position and the per-cent of O pond total length.
The measuring method that described dissolved oxygen rises to position can be the method for this area routine, and the present invention adopts dissolved oxygen instrument to measure.
Described high ammonia-nitrogen wastewater generally refers to ammonia nitrogen concentration >100mg/L, C/N waste water than <10.
Described carbon source can be the carbon source of this area routine, is preferably one or more in methyl alcohol, second alcohol and glucose.The addition of described carbon source can be the addition of this area routine, represents in the present invention with A, A=(r+1) × Q × C
nO3-N× b, wherein, A is the addition of carbon source, gCOD/h; R is return sludge ratio; Q is flooding velocity, m
3/ h; C
nO3-Nfor dissolved oxygen rises to the nitrate nitrogen concentration of position, mg/L; B is reduction factor, 5.0 ~ 10.0, and the denitrification percent of its correspondence is 85% ~ 100%.
Described traditional A/O technique refers to described high ammonia-nitrogen wastewater successively through anoxic pond, aeration tank and second pond being carried out the technique processed.Wherein, anoxic pond, aeration tank and second pond are cascaded, the principle of tradition A/O technique is that organic matter degradation and Ammonia Nitrification occur high ammonia-nitrogen wastewater in aeration tank, and the nitrate that nitration reaction produces is back to anoxic pond by aeration tank end and carries out denitrification denitrogenation.Described traditional A/O technique also can be substituted by the A/O technique of the improvement based on A/O process regime further; Such as A-O-A-O technique or A-A-O-O technique etc.When in the A/O technique improved, during containing two or more O ponds, the muddy water mixed solution that the dissolved oxygen in wherein one or more O ponds can be selected to rise to position is back to arbitrary anoxic pond as nitrification liquid, meanwhile, rises to position add carbon source at the dissolved oxygen in O pond.
In the improving technique of described A/O, the retention time of sewage in described anoxic pond is preferably 8 ~ 12h, and temperature is preferably 20 ~ 30 DEG C, and pH value is preferably 7.0 ~ 7.5.
In the improving technique of described A/O, the retention time of sewage in described aeration tank is preferably 16 ~ 24h, and temperature is preferably 20 ~ 30 DEG C, and pH value is preferably 7.0 ~ 7.5.Nitrification liquid in described aeration tank is preferably back in anoxic pond by reflux ratio 3.0 ~ 4.0.
Waste water after the process of A/O improving technique enters second pond, discharges supernatant liquor after precipitation, and the partial sludge in second pond is preferably back in anoxic pond by reflux ratio 0.5 ~ 1.0.
Mud in the improving technique of described A/O is generally suspended active mud, and its MLSS is preferably 5 ~ 10g/L.
Without prejudice to the field on the basis of common sense, above-mentioned each optimum condition, can arbitrary combination, obtains the preferred embodiments of the invention.
Agents useful for same of the present invention and raw material are all commercially.
Positive progressive effect of the present invention is:
Method of the present invention overcomes the bottleneck of traditional A/O technique denitrification percent by reflux ratio restriction, and denitrification percent can reach 100%, and denitrification percent is high, and water outlet COD value is lower than 50mg/L; Simple to operate, applied widely, be easy to industrializing implementation.
Accompanying drawing explanation
Fig. 1 embodiments of the invention 1 on A/O Process ba-sis to the method flow schematic diagram of the further denitrogenation of high ammonia-nitrogen wastewater.
Fig. 2 is that in aeration tank, dissolved oxygen concentration rises to phenomenon figure.
Fig. 3 is the graph of a relation of b value and denitrification percent in the formula of carbon source addition in embodiment 1.
Embodiment
Mode below by embodiment further illustrates the present invention, but does not therefore limit the present invention among described scope of embodiments.The experimental technique of unreceipted actual conditions in the following example, conventionally and condition, or selects according to catalogue.
In following embodiment, COD, BOD, TN, NH
3-N and NO
3the detection method of-N all performs " water and waste water method for monitoring and analyzing " by national standard, China Environmental Science Press, the third edition, 1989; Be specially: COD examination criteria is GB11914-89 potassium dichromate process; TN examination criteria is GB11894-89 potassium persulfate oxidation ultraviolet spectrophotometry; NH
3-N examination criteria is GB7478-87 Nessler's reagent photometer; NO
3-N examination criteria is GB7480-87 phenol disulphonic acid spectrophotometry.
Embodiment 1
The present invention is utilized to carry out transformation and upgrade to A/O art breading high ammonia-nitrogen wastewater denitrogenation engineering.Wastewater treatment capacity 1000m
3d
-1, waste water COD 2500mgL
-1, TN 450mgL
-1, NH
3-N 350mgL
-1.Former treatment process is A/O technique, A pond useful volume 1600m
3, O pond useful volume 3400m
3, be divided into two gallerys, second pond useful volume 500m
3.O pond end mixed liquid recycle ratio is 4.0, and second pond return sludge ratio is 1.0.Original system water outlet TN 72.9mgL
-1, NH
3-N 0.2mgL
-1, TN clearance is about 83.8%, and water outlet COD value is 50.0mgL
-1.
Find after testing, in above-mentioned A/O technique, O pond is located ammonia nitrogen along water (flow) direction about 75% and is down to 1.0mgL
-1below, dissolved oxygen rises to 3.0mgL
-1.
Now aeration tank is transformed as follows: aeration tank nitrification liquid return line is moved forward to aeration tank along water (flow) direction 75% place; Thereafter setting up carbon source chemical feed pipe, take methyl alcohol as carbon source, and addition is A=(r+1) × Q × C
nO3-N× b, wherein r=1, Q=1000m
3d
-1, C
nO3-N=72.9mgL
-1, b gets 4.0,5.0,6.0,7.0,8.0,9.0,10.0 respectively and tests, and namely the addition of carbon source is respectively 583.2kg CODd
-1, 729kg CODd
-1, 874.8kg CODd
-1, 1020.6kg CODd
-1, 1166.4kg CODd
-1, 1312.2kg CODd
-1with 1458kg CODd
-1, TN clearance is respectively 84.1%, 85.5%, 88.1%, 93.5%, 96.2%, 98.2%, 100% (specifically seeing Fig. 3); Water outlet COD value is all lower than 50.0mgL
-1.
Embodiment 2
The present invention is utilized to carry out transformation and upgrade to certain nitrogen fertilizer plant's height ammonia nitrogen, low C/N waste water treatment engineering.
Certain wastewater from nitrogenous fertilizer industry COD is 600mgL
-1, TN is 200mgL
-1, NH
3-N is 150mgL
-1, the process water yield is 10000m
3d
-1, existing treatment process is A/O technique, A pond useful volume 5000m
3, O pond useful volume 10000m
3, be divided into four gallerys, second pond useful volume 1500m
3.O pond end mixed liquid recycle ratio is 4.0, and second pond return sludge ratio is 0.5.After process, water outlet COD is 30.0 ~ 50.0mgL
-1, NH
3-N<1.0mgL
-1, but TN still has 36.5mgL
-1left and right, cannot reach TN advanced treatment and require (i.e. GB18918-2002, primary standard).
Detect and find, in above-mentioned A/O technique, O pond is located ammonia nitrogen at the 4th gallery about 1/3 and is down to 1.0mgL
-1below, corresponding dissolved oxygen rises to 3.5mgL
-1.
Now by method of the present invention, original system is improved: aeration tank nitrification liquid return line is moved forward to gallery 1/3 place, O pond the 4th (corresponding gallery overall length 83%), thereafter setting up carbon source chemical feed pipe, take glucose as carbon source, addition A=(r+1) × Q × C
nO3-N× b, wherein r=0.5, Q=10000m
3d
-1, C
nO3-N=36.5mgL
-1, b gets 5.0,8.0,10.0 respectively and tests, and namely carbon source addition is respectively 2737.5kg CODd
-1, 4380kg CODd
-1with 5475kg CODd
-1time, TN clearance is respectively 86.5%, 96.7% and 99.9%, and water outlet COD is all lower than 50.0mgL
-1.
Comparative example 1
On the basis of embodiment 2, when aeration tank nitrification liquid return line and carbon source chemical feed pipe are arranged on other positions, O pond, the TN removal effect of test macro and water outlet COD value, concrete operations are as follows: aeration tank nitrification liquid return line is moved forward to O pond the 1st gallery end, the 2nd gallery end and the 4th gallery 2/3 place (corresponding gallery overall length 25%, 50% and 92%), and setting up carbon source chemical feed pipe thereafter, take glucose as carbon source, addition A=(r+1) × Q × C
nO3-N× b, wherein r=0.5, Q=10000m
3d
-1, C
nO3-N=36.5mgL
-1, b all gets 8.0 and tests, and found that TN clearance is respectively 85.5%, 89.6% and 97.1%, water outlet COD is respectively 45.0,50.0 and 80.0mgL
-1.
Above-mentioned experiment finds, when aeration tank nitrification liquid return line and carbon source chemical feed pipe move to the 4th gallery 2/3 place (corresponding gallery overall length 92%), although denitrification percent can reach 97.1%, denitrification percent is high, but due to aeration tank nitrification liquid return line and carbon source chemical feed pipe position too rearward, the organism that water outlet is also residual certain, makes water outlet COD up to 80.0mgL
-1left and right.Therefore the dissolved oxygen that aeration tank nitrification liquid return line and carbon source chemical feed pipe position are preferably positioned at O pond rises to position (i.e. DO hop point).
Claims (10)
1. one kind on A/O Process ba-sis to the method for the further denitrogenation of high ammonia-nitrogen wastewater, it is characterized in that, it comprises the following steps: the improving technique process of high ammonia-nitrogen wastewater through A/O,, wherein, the improving technique of described A/O is that the muddy water mixed solution that aeration tank dissolved oxygen rises to position is back to anoxic pond as nitrification liquid on traditional A/O Process ba-sis; Meanwhile, rise to position at the dissolved oxygen of aeration tank and add carbon source; Described dissolved oxygen rises to position and refers to that dissolved oxygen in aeration tank is less than 0.5mg/L by dissolved oxygen and rises to dissolved oxygen and be greater than position corresponding to 2mg/L.
2. the method for claim 1, it is characterized in that, described dissolved oxygen rises to position and is positioned at O pond along water (flow) direction 75% ~ 85% position, and described per-cent refers to that aeration tank starting point to aeration tank dissolved oxygen rises to the distance of position and the per-cent of aeration tank total length.
3. the method for claim 1, is characterized in that, described high ammonia-nitrogen wastewater refers to ammonia nitrogen concentration >100mg/L, C/N waste water than <10.
4. the method for claim 1, is characterized in that, described carbon source is one or more in methyl alcohol, second alcohol and glucose.
5. the method for claim 1, is characterized in that, addition A=(r+1) × Q × C of described carbon source
nO3-N× b, wherein, A is the addition of carbon source, gCOD/h; R is return sludge ratio; Q is flooding velocity, m
3/ h; C
nO3-Nfor dissolved oxygen rises to the nitrate nitrogen concentration of position, mgN/L; B is reduction factor, 5.0 ~ 10.0.
6. the method for claim 1, is characterized in that, described traditional A/O technique refers to described high ammonia-nitrogen wastewater successively through anoxic pond, aeration tank and second pond being carried out the technique processed.
7. the method for claim 1, is characterized in that, described traditional A/O technique is also substituted by A-O-A-O technique or A-A-O-O technique further.
8. the method for claim 1, is characterized in that, in the improving technique of described A/O, the retention time of sewage in described anoxic pond is 8 ~ 12h, and temperature is 20 ~ 30 DEG C, and pH value is 7.0 ~ 7.5.
9. the method for claim 1, is characterized in that, in the improving technique of described A/O, the retention time of sewage in described aeration tank is 16 ~ 24h, and temperature is 20 ~ 30 DEG C, and pH value is 7.0 ~ 7.5.
10. the method for claim 1, is characterized in that, in the improving technique of described A/O, the nitrification liquid in described aeration tank is back in anoxic pond by reflux ratio 3.0 ~ 4.0; Mud in second pond is back in anoxic pond by reflux ratio 0.5 ~ 1.0; Mud in the improving technique of described A/O is suspended active mud, and its MLSS is 5 ~ 10g/L.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101746894A (en) * | 2009-12-25 | 2010-06-23 | 华东理工大学 | Method for eliminating nitrogen from waste water through simultaneous nitrification and denitrification |
| US8012352B1 (en) * | 2010-09-20 | 2011-09-06 | American Water Works Company, Inc. | Optimized nutrient removal from wastewater |
| CN103011410A (en) * | 2012-12-06 | 2013-04-03 | 杭州绿色环保技术开发有限公司 | Synchronous degradation process and device for COD (Chemical Oxygen Demand) and N (Nitrogen) of high concentration wastewater in same pool |
-
2015
- 2015-01-30 CN CN201510051225.4A patent/CN104671410B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101746894A (en) * | 2009-12-25 | 2010-06-23 | 华东理工大学 | Method for eliminating nitrogen from waste water through simultaneous nitrification and denitrification |
| US8012352B1 (en) * | 2010-09-20 | 2011-09-06 | American Water Works Company, Inc. | Optimized nutrient removal from wastewater |
| CN103011410A (en) * | 2012-12-06 | 2013-04-03 | 杭州绿色环保技术开发有限公司 | Synchronous degradation process and device for COD (Chemical Oxygen Demand) and N (Nitrogen) of high concentration wastewater in same pool |
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Effective date of registration: 20180511 Address after: 272100 Jining hi tech Zone East Outer Ring Road No. 6, Shandong Patentee after: Shandong Lukang Zhonghe Environmental Protection Technology Co., Ltd. Address before: 200237 No. 130, Meilong Road, Shanghai, Xuhui District Patentee before: East China University of Science and Technology |