CN1948184A - Control method and device of A2/O oxidation trench technology synchronous nitration and denitrification - Google Patents
Control method and device of A2/O oxidation trench technology synchronous nitration and denitrification Download PDFInfo
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 86
- 230000003647 oxidation Effects 0.000 title claims abstract description 84
- 238000000034 method Methods 0.000 title claims abstract description 46
- 238000005516 engineering process Methods 0.000 title claims abstract description 35
- 230000001360 synchronised effect Effects 0.000 title claims abstract description 31
- 238000006396 nitration reaction Methods 0.000 title claims description 50
- 238000005273 aeration Methods 0.000 claims abstract description 72
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 238000012544 monitoring process Methods 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 48
- 239000010802 sludge Substances 0.000 claims description 31
- 241000894006 Bacteria Species 0.000 claims description 20
- 238000010992 reflux Methods 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 229920000388 Polyphosphate Polymers 0.000 claims description 5
- 229920000037 Polyproline Polymers 0.000 claims description 5
- 239000001205 polyphosphate Substances 0.000 claims description 5
- 235000011176 polyphosphates Nutrition 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 230000001580 bacterial effect Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 27
- 239000010865 sewage Substances 0.000 abstract description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 40
- 229910052757 nitrogen Inorganic materials 0.000 description 19
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 12
- 230000000694 effects Effects 0.000 description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 7
- 230000001546 nitrifying effect Effects 0.000 description 5
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- 238000005276 aerator Methods 0.000 description 3
- CMLMFNACXHHYRY-UHFFFAOYSA-N azanylidynetin Chemical compound [N].[Sn] CMLMFNACXHHYRY-UHFFFAOYSA-N 0.000 description 3
- -1 effect by nitrifier Chemical compound 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000009293 extended aeration Methods 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 2
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 2
- 150000001413 amino acids Chemical class 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 2
- 150000002897 organic nitrogen compounds Chemical class 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 241001495402 Nitrococcus Species 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 1
- 241000337007 Oceania Species 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000001272 nitrous oxide Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Abstract
The present invention relates to an A2/O oxidation channel process synchronous nitrification and denitrification control method and its equipment, belonging to the field of domestic sewage biodenitrogenation technology. It is characterized by that said method includes the following steps: utilizing DO on-line monitoring apparatus to monitor the macroscopic aerobic-anoxic environment formed in oxidation channel aeration basin; utilizing ORP on-line monitoring apparatus to monitor the microscopic aerobic-anoxic environment formed in oxidation channel aeration basin; and utilizing computer to control frequency conversion air blower to control aeration quantity so as to ensure that the macroscopic and microscopic nitrification reaction and denitrification reaction can be simultaneously implemented.
Description
Technical field
A kind of A of the present invention
2/ O oxidation trench technology synchronous nitration denitrification control method and device, what relate to is the technical field of domestic sewage denitrifying, particularly a kind of biological denitrificaion.
Background technology
Oxidation Ditch Technology
Oxidation ditch (oxidation ditch) has another name called continuous circulated aeration tank (Continuous loop reactor), is a kind of distortion of activated sludge process.Oxidation ditch is applied to Holland at first, has become a kind of important sewage disposal technology of Europe, Oceania, South Africa and North America at present.In recent years, adopt the speed of oxidation ditch treatment plant that breakthrough has been arranged.The growth in sewage work's quantity of China's oxidation ditch process at present is rapider, and oxidation ditch process be the first-selected technology of present domestic and international newly-built sewage work.
Oxidation ditch has special hydromechanics fluidised form, and the characteristics of existing complete mixing reactor have the characteristics of plug flow reactor again, have tangible dissolved oxygen concentration gradient in the ditch.The oxidation ditch section is a rectangle or trapezoidal, and it is oval that planeform mostly is, and the depth of water is generally 2～5m in the ditch, and current V-bar is 0.3m/s in the ditch.Oxidation ditch aeration and mixing has surface aeration machine, aeration rotary brush or rotating disk, jet aerator, catheter type aerator and promotes tubular type aerator etc., and what be used in recent years also has pusher under water.
Oxidation ditch process is stable because of it, convenient operating maintenance, and effluent quality is good.Improved in recent years oxidation ditch process has preferably, and the denitrogenation dephosphorizing ability makes this technology become one of the most practical technology both at home and abroad.
Bio-denitrification technology
The traditional biological denitrogenation is in traditional two stage biological is handled organonitrogen to be converted on the basis of ammonia nitrogen, effect by nitrifier, ammonia nitrogen is converted into nitrite nitrogen, nitric nitrogen by nitrification, and then utilize denitrifying bacteria that nitric nitrogen and nitrite nitrogen are converted into nitrogen, discharge into the atmosphere, thereby reach the purpose of denitrogenation from waste water.
Biological denitrificaion is mainly three kinds of reactions, i.e. aminating reaction, and nitration reaction and anti-nitration reaction:
In the raw sewerage, the principal mode that nitrogenous compound exists is: (1) organonitrogen, as protein, amino acid, urea, aminated compounds and aminocompound class; (2) ammonia-state nitrogen (NH
3, NH
4 +), generally based on the former.
Nitrogenous compound produces following reaction in succession under action of microorganisms.
(1) aminating reaction
Organic nitrogen compound under the effect of Ammonifying bacteria, is converted into NH with the organic nitrogen compound deaminizating
3, be example with amino acid, its reaction formula is (1):
No matter ammonification is aerobic or under anaerobic, and acid, neutral or all can carry out under alkaline condition, just the power of the kind effect of the microorganism of effect differs.
(2) nitration reaction
Under the effect of nitrifier, the further oxidation of ammonia-state nitrogen is carried out in two stages, and at first under the effect of nitrococcus, ammonia-state nitrogen is converted into nitrite nitrogen.Reaction formula is (2):
Subsequently, nitrous acid further is converted into nitrate nitrogen under the effect of nitrifier, and its reaction formula is (3):
The net reaction of nitration reaction is (4):
Do not consider that cell is synthetic, but the needed basicity through type of nitrifying process (5) calculates:
From the nitration reaction net reaction as can be seen, nitrification needs a large amount of oxygen, consumes certain basicity simultaneously.Can cause pH value decline in the environment.
Consider a part of NH of synthetic utilization of cell
4 +, then the ammonia nitrogen nitrifying process is represented with formula (6):
According to formula (6) as can be known, transform every gram ammonia nitrogen, need utilize 4.25 gram oxygen, the new cell of synthetic 0.16 gram needs to consume 7.07 gram basicity, utilizes the synthetic new cell of the inorganic carbon source of 0.08 gram simultaneously.
(3) anti-nitration reaction
Anti-nitration reaction is meant that nitrate and nitrite are reduced to the process of gaseous nitrogen and Nitrous Oxide under the effect of denitrifying bacteria.Most of denitrifying bacterias are heterotrophic facultative anaerobic bacterias, and it can utilize the electron donor of various organism as denitrification, thereby denitrification can either be reduced to nitrogen with nitre nitrogen and nitrite nitrogen, carries out denitrogenation; Organism in again can oxygenolysis waste water carries out decarburization.Reaction formula is as (7):
In sum: the traditional biological denitrogenation generally comprises nitrifying process and two stages of denitrification process; Nitrification and denitrification are finished by nitrifier and denitrifying bacteria respectively, and two bacterioids are different for the requirement of envrionment conditions, and these two processes can't be carried out simultaneously, can only connect and successively carry out.Nitrifier is aerobic autotrophic bacteria, and nitration reaction is at BOD
5Can carry out smoothly under the lower aerobic condition, and denitrifying bacteria is the amphimicrobian heterotrophic bacterium, can only be as carbon source with organism, so can only certain organic concentration arranged and under anoxic environment, can carry out smoothly.Biological denitrification process under this thought guidance, mostly oxygen-starved area and aerobic zone are separated, form fractionated nitrated-denitrification process, create the control environment condition of nitrifier and denitrifying bacteria growth, so that nitrification and denitrification all can independently be carried out.
The various improvement technologies that the traditional biological denitrogenation is adopted A/O technology and occurred again afterwards are as Bardenpho, Phoredox (A
2O), UCT, JBH, AAA technology etc., these all are typical nitration denitrification technology.
Biological denitrificaion is the process of a more complicated, is subjected to dissolved oxygen, carbon-nitrogen ratio, and influent alkalinity, the influence of factors such as water temperature, biological denitrificaion is difficult to efficient stable to carry out.Be that the removal efficient of A/O technology TN is 60～70% under 200% the situation in reflux ratio.
The synchronous nitration and denitrification technology
(Simultaneous nitrification and denitrification SND) is the microbial reaction phenomenon that nitration reaction and two kinds of biological respinses of denitrification carry out to synchronous nitration and denitrification in same reactor.This phenomenon is called as aerobic denitrification before being found in 20 years, is called as SND subsequently.Many research reports about SND are arranged recent years, as occur in the SND in the SBR technology, occur in the SND in traditional extended aeration technology, A
2SND in the/O technology and the SND in the oxidation ditch process.Former study rests on the observation analysis of SND phenomenon more, and for SND effectively utilize and the research of stable control aspect not many.Realize that synchronous nitration and denitrification can reduce the sewage disposal energy consumption efficiently, reduce water outlet total nitrogen (TN) and ammonia nitrogen (NH
4 +) content, improve effluent quality.
Urban wastewater treatment firm pollutant emission standard (GB18918-2002) is to the ammonia nitrogen in the effluent of municipal sewage plant and total nitrogen discharged higher requirement that proposed, wherein one-level A regulation water outlet ammonia nitrogen is less than 5 (8) mg/L, total nitrogen is less than 15mg/L, ammonia nitrogen up to standard often than being easier to is by extended aeration or increase aeration rate and can realize nitrated fully.And total nitrogen is up to standard difficult relatively, and carbon-nitrogen ratio is low in the part of contaminated water causes the denitrifying carbon source deficiency to cause the TN clearance lower, and dephosphorization need consume the part carbon source in the sewage disposal.The excessive aeration of aerobic zone has also increased the weight of the carbon source deficiency to denitrifying influence in addition, and it is not high to cause total nitrogen to remove efficient.
Because what oxidation ditch process adopted is extended aeration technology, hydraulic detention time is longer, about the phenomenon that has the synchronous nitration and denitrification biological denitrificaion in the oxidation ditch process bibliographical information is arranged more, but major part only rests on the discovery to the synchronous nitration and denitrification phenomenon, and the synchronous nitration and denitrification efficient of report is lower, and is not high to the contribution that total nitrogen is removed.
Research for synchronous nitration and denitrification at present still is in the starting stage, optimal control to synchronous nitration and denitrification is relatively more difficult, its reason is: the environment DO that realizes synchronous nitration and denitrification is lower, often below 0.5mg/L, so the DO variation range is less, and change acutely, thereby be not suitable as controlled variable.And the researchist often thinks in aerobic zone not tangible relation of ORP and biological denitrificaion, thereby caused the ignorance to ORP in the aerobic zone.
Summary of the invention
The purpose of this invention is to provide a kind of A
2/ O oxidation trench technology synchronous nitration denitrification control method and device are to solve A
2The excessive aeration of/O oxidation ditch process causes the biological denitrification process total nitrogen to remove inefficiency, and energy consumption problems of too, and the environment DO that overcomes synchronous nitration and denitrification is low is difficult to control, and the problem of ORP in the secular ignorance aerobic zone, thereby realize the synchronous nitration and denitrification biological denitrification process is carried out efficient, stable control.
(1) A
2The device that/O oxidation trench technology synchronous nitration denitrification control method adopts
A kind of A
2/ O oxidation trench technology synchronous nitration denitrification control device, mainly be in series by water tank 1, oxidation ditch main body 2 and second pond 3 orders, oxidation ditch main body 2 is made up of anaerobic zone 5, oxygen-starved area 6 and the aeration tank 7 that is provided with aerating system, it is characterized in that: described aerating system connects to form by being located at the aeration head 17 in the aeration tank 7 and being located at aeration tank 7 outer frequency conversion gas blowers 14, and frequency conversion gas blower 14 is connected with computer 21; Be provided with DO on-line monitoring instrument 12 and ORP on-line monitoring instrument 13 in the described aeration tank 7, and ORP on-line monitoring instrument 13 is connected with computer 21; Described second pond 3 connects anaerobic zone 5 and oxygen-starved area 6 by sludge reflux pump 11 respectively.
(2) A
2/ O oxidation trench technology synchronous nitration denitrification control method
A kind of A
2/ O oxidation trench technology synchronous nitration denitrification control method is characterized in that this method may further comprise the steps:
1) active sludge that contains polyP bacteria, denitrifying bacteria and nitrifier is added in the oxidation ditch main body 2, carry out the domestication and the cultivation of bacterial classification, make the activated sludge concentration in the oxidation ditch main body 2 maintain 4000mg/L～6000mg/L;
2) with raw waste water from water tank 1 pump to anaerobic zone 5, mix with 30% returned sluge that the sludge reflux pump 11 that is connected anaerobic zone 5 refluxes, after anaerobic zone on average stops 40～60 minutes, enter oxygen-starved area 6;
In anaerobic zone 5, the polyP bacteria in the active sludge absorbs VFA, and carries out the release of phosphorus;
3) after the muddy water of discharging in the above-mentioned anaerobic zone 5 entered oxygen-starved area 6,70% returned sluge that refluxes with the sludge reflux pump 11 that is connected oxygen-starved area 6 mixed, and 6 average stops entered oxidation ditch aeration pond 7 after 60～80 minutes in the oxygen-starved area;
In oxygen-starved area 6, the denitrifying bacteria in the active sludge utilizes that easily biodegradable organics carries out anti-nitration reaction in the water, the NO that returned sluge is brought into
3 -Be reduced to nitrogen;
4) after the muddy water of above-mentioned oxygen-starved area 6 discharges enters in the oxidation ditch aeration pond 7, start frequency conversion gas blower 14 and provide oxygen for the aeration head 17 that is arranged in aeration tank 7, treating water is carried out blast aeration, computer 21 is adjusted the power of frequency conversion gas blower 14 according to the registration of DO on-line monitoring instrument 12 and ORP on-line monitoring instrument 13, the registration of DO on-line monitoring instrument 12 is controlled in 0.8mg/L to the 0.1mg/L scope, and the registration of ORP on-line monitoring instrument 13 is controlled at-30mv～30mv scope in, treating water in oxidation ditch aeration pond 7 average hydraulic detention time after 18 hours draining enter in the second pond 3;
The registration of DO on-line monitoring instrument 12 is illustrated in the dissolved oxygen gradient that forms in the oxidation ditch aeration pond 7, this dissolved oxygen gradient is controlled in 0.8mg/L to the 0.1mg/L scope, just in oxidation ditch aeration pond 7, formed the dissolved oxygen gradient and be the macroscopical aerobic-anaerobic environment in 0.8mg/L to the 0.1mg/L scope, the nitration reaction and the anti-nitration reaction that guarantee macrostate carry out simultaneously, avoid the low excessively too high denitrification that causes of nitrated insufficient and DO that causes of DO to be suppressed;
The registration of ORP on-line monitoring instrument 13 is the redox potential in oxidation ditch aeration pond 7, with the oxidation reduction potential control in the oxidation ditch aeration pond 7 in-30mv～30mv scope, be in order to keep the redox state of microcosmic in the oxidation ditch aeration pond 7, the nitration reaction and the anti-nitration reaction that guarantee microstate carry out simultaneously, be exactly specifically: as ORP＞30mv, the shared whole active sludge flco volume of microcosmic aerobic zone is bigger, the microcosmic aerobic environment accounts for leading, nitrated preponderating, aeration rate be should reduce, active sludge over oxidation and NO in the aeration tank prevented
3 -Accumulation, when ORP＜-30mv, the shared whole active sludge flco volume in microcosmic oxygen-starved area is bigger, the microcosmic anaerobic environment accounts for leading, nitratedly will be affected NH
4 +Because of nitrated the inhibition accumulates, at this moment increase aeration rate, improve nitrification effect;
Mainly carry out following four kinds of reactions in oxidation ditch aeration pond 7: oxidation of coal reaction, nitrifier nitration reaction, denitrifying bacteria anti-nitration reaction, polyP bacteria that heterotrophic bacteria utilizes organism to carry out absorb phosphorus reaction;
5) treating water that overflows from oxidation ditch aeration pond 7 enters second pond 3 and carries out mud-water separation, and supernatant liquor is discharged system, and returned sluge is back to anaerobic zone 5 and oxygen-starved area 6 respectively in 3: 7 ratio.
The beneficial effect of the invention
Macroscopical aerobic-anaerobic environment that the present invention forms in the oxidation ditch aeration pond by the monitoring of DO on-line monitoring instrument, by the microcosmic that ORP on-line monitoring instrument monitoring forms in the oxidation ditch aeration pond aerobic-anaerobic environment, utilize computer control frequency conversion gas blower control aeration rate, guarantee that the nitration reaction and the anti-nitration reaction of both macro and micro state carries out simultaneously.
Method nitration denitrification of the present invention is reflected in the aeration tank and carries out simultaneously, nitrifying process consumes basicity, denitrification process produces basicity, denitrification process has compensated half basicity of nitrifying process, do not need to add in addition alkali and can not influence the nitrated demand of system yet basicity, the contribution that synchronous nitration and denitrification is removed total nitrogen accounts for more than 50% of whole total nitrogens removals, has saved the required carbon source of denitrification, and this municipal sewage treatment to low ratio of carbon to ammonium has more adaptability.Average dissolved oxygen concentration is below 0.5mg/L in the stable synchronous nitration and denitrification aeration tank that the present invention realizes, compare more than 2.0mg/L with the nitrated dissolved oxygen concentration that needs of tradition, greatly reduce aeration energy consumption, realized total nitrogen more than 80% clearance and ammonia nitrogen up to the clearance more than 90%, problem and the sewage water denitrification efficient instability and the low problem of compliance rate of nitrogenous eutrophication sewage disposal have been solved, also solved the water outlet ammonia nitrogen that occurs in the sewage disposal operational process, the unmanageable practical problems of total nitrogen concentration has solved the optimization of oxidation trench technology synchronous nitration denitrification technical parameter and the problem of control.
Description of drawings
Figure 1A
2The device synoptic diagram that/O oxidation trench technology synchronous nitration denitrification control method adopts;
Among the figure: 1-water tank, 2-oxidation ditch main body, 3-second pond, 4-intake pump, 5-anaerobic zone, 6-oxygen-starved area, 7-aeration tank, 8-water-in, 9-returned sluge mouth, 10-agitator, 11-return sludge pump, 12-DO on-line monitoring instrument, 13-ORP on-line monitoring instrument, 14-frequency conversion gas blower, 15-air flowmeter, 16-blast main, 17-aeration head, 18-oxidation ditch overflow weir, 19-active plugboard, 20-residual sludge pump, 21-computer.
Fig. 2 second pond synoptic diagram;
Among the figure: 22-second pond overflow weir, 23-water shoot, 24-second pond stopple coupon, 25-second pond water inlet pipe, 26-second pond central tube, 27-excess sludge pipe, 28-reflux sludge tube.
Embodiment
The present invention is described in detail below in conjunction with drawings and Examples:
(1) A
2The device that/O oxidation trench technology synchronous nitration denitrification control method adopts
A
2The device that/O oxidation trench technology synchronous nitration denitrification control method adopts is a kind of A
2/ O oxidation ditch device as shown in Figure 1, mainly is in series by water tank 1, oxidation ditch main body 2, second pond 3 orders; Oxidation ditch main body 2 is followed successively by anaerobic zone 5 along water (flow) direction, oxygen-starved area 6 and oxidation ditch aeration pond 7, the anaerobic zone 5 of water tank 1 and oxidation ditch main body is connected by intake pump 4, the oxidation ditch aeration pond 7 of oxidation ditch main body 2 is connected with second pond 3 by overflow weir 18 and second pond water inlet pipe 25, anaerobic zone 5 and 6 inside, oxygen-starved area are respectively equipped with agitator 10, anaerobic zone 5 is connected with second pond 3 by a return sludge pump 11 separately with oxygen-starved area 6, oxidation ditch aeration pond 7 makes current form the current oxidation ditch that repeatedly changes direction by the furrow bank that is provided with in it, 7 inside, oxidation ditch aeration pond are provided with agitator 10 in the position of flow direction-changing, 7 inside, oxidation ditch aeration pond also are provided with a plurality of aeration heads 17, each aeration head 17 is connected with frequency conversion gas blower 14 with oxidation ditch aeration pond 5 air outside under meters 15 by blast main 16, second pond 3 is center water inlet peripheral effluent radical sedimentation basin, second pond 3 pool walls are provided with highly different thief hole 24, second pond 3 tops are provided with triangle effluent weir 22, second pond 3 bottoms are provided with 2 mud discharging mouths, one of them returned sluge mouth 28 connects return sludge pump 11, and another excess sludge mouth 27 connects the residual sludge pump 20 of getting rid of excess sludge.
Be provided with active plate 19 between described anaerobic zone 5 and the oxygen-starved area 6, this plate 19 places different position between anaerobic zone 5 and the oxygen-starved area 6, can adjust the volume ratio of anaerobic zone 5 and oxygen-starved area 6.
Be provided with ORP on-line monitoring instrument 13 in 7 exits, described aeration tank, each aeration head 17 front and back is provided with DO on-line monitoring instrument 12 in aeration tank 7, each aeration head 17 is connected by the frequency conversion gas blower 14 of blast main with 7 outsides, oxidation ditch aeration pond, and ORP on-line monitoring instrument 13 is connected with computer 21 by data line respectively with frequency conversion gas blower 14.
(2) A
2/ O oxidation trench technology synchronous nitration denitrification control method
A kind of A
2/ O oxidation trench technology synchronous nitration denitrification control method is characterized in that this method may further comprise the steps:
1) active sludge that contains anaerobism polyP bacteria, denitrifying bacteria and nitrifier is added in the oxidation ditch main body 2, carry out the domestication and the cultivation of bacterial classification, make the activated sludge concentration in the oxidation ditch main body 2 maintain 4000mg/L～6000mg/L;
2) with raw waste water from water tank 1 pump to anaerobic zone 5, mix with 30% returned sluge that the sludge reflux pump 11 that is connected anaerobic zone 5 refluxes, after anaerobic zone on average stops 40～60 minutes, enter oxygen-starved area 6;
3) after the muddy water of discharging in the above-mentioned anaerobic zone 5 entered oxygen-starved area 6,70% returned sluge that refluxes with the sludge reflux pump 11 that is connected oxygen-starved area 6 mixed, and 6 average stops entered oxidation ditch aeration pond 7 after 60～80 minutes in the oxygen-starved area;
4) after the muddy water of above-mentioned oxygen-starved area 6 discharges enters in the oxidation ditch aeration pond 7, start frequency conversion gas blower 14 and provide oxygen for the aeration head 17 that is arranged in aeration tank 7, treating water is carried out blast aeration, computer 21 is adjusted the power of frequency conversion gas blower 15 according to the registration of DO on-line monitoring instrument 12 and ORP on-line monitoring instrument 13, the registration of DO on-line monitoring instrument 12 is controlled in 0.8mg/L to the 0.1mg/L scope, and the registration of ORP on-line monitoring instrument 13 is controlled at-30mv～30mv scope in, treating water in oxidation ditch aeration pond 7 average hydraulic detention time after 18 hours draining enter in the second pond 3;
5) processed water that overflows from oxidation ditch aeration pond 7 enters second pond 3 and carries out mud-water separation, supernatant liquor is discharged from overflow weir 22, part mud is back to anaerobic zone 5 and oxygen-starved area 6 respectively in 3: 7 ratio, and excess sludge is by residual sludge pump 20 discharge systems.
Embodiment one
With the aerated grit chamber water outlet of Beijing sewage work is former water, water inlet COD, ammonia nitrogen, total nitrogen and total phosphorus value (COD=251.2～489.4mg/L, NH
4 +=35.5～51.2mg/L, TN=49.4～65.4mg/L, TP=5.4～8.7mg/L).The hydraulic detention time of oxygen-starved area and anaerobic zone and oxidation ditch (HRT) is respectively 0.5h, 1.5h and 18h, and reflux ratio is 100%, and the mean flow rate in the oxidation ditch aeration pond is about 1cm/s, and circulation primary takes 5～7 minutes.This technology SND is tested as the controlled variable of oxidation ditch process biological denitrificaion synchronous nitration and denitrification (SND) with redox potential (ORP).
Experimental stage COD, BOD
5, NH
4 +, TN average influent concentration be 337.8mg/L, 177.4mg/L, 52.7mg/L and 38.5mg/L, on average going out water concentration is 45.3mg/L, 12.5mg/L, 13.2mg/L, 4.2mg/L, average removal rate are 86.5%, 93.0%, 75.0% and 89%.
ORP is NO more than 95% in the total inorganic nitrogen (TIN) in the water outlet when 30mv is above
3 -, under this situation, be NO more than 80% in the total inorganic nitrogen (TIN) in the water outlet
3 -, the water outlet ammonia nitrogen is energy (less than 5mg/L) up to standard all, and fate TN＞15mg/L of 2/3 is arranged approximately, and nitrification effect is good, and denitrification efficient is lower.ORP-when 30mv is following, fate TN＞5mg/L of 3/4 is arranged approximately, nitrated insufficient, be NH more than 78% in the total inorganic nitrogen (TIN) in the water outlet
4 +, ORP is low more, and is nitrated insufficient more; ORP is when-30～30mv, and the TN clearance is more than 88%, the NO that the SND effect is removed
3 -Account for total NO
3 -More than 90% of removal.The per-cent that the SND effect is removed TN is more than 80%.
Claims (2)
1. A
2/ O oxidation trench technology synchronous nitration denitrification control device, be in series by water tank (1), oxidation ditch main body (2) and second pond (3) order, oxidation ditch main body (2) is made up of anaerobic zone (5), oxygen-starved area (6) and the aeration tank (7) that is provided with aerating system, it is characterized in that:
Described aerating system connects to form by being located at the aeration head (17) in the aeration tank (7) and being located at the outer frequency conversion gas blower (14) in aeration tank (7), and frequency conversion gas blower (14) is connected with computer (21);
Be provided with DO on-line monitoring instrument (12) and ORP on-line monitoring instrument (13) in the described aeration tank (7), and ORP on-line monitoring instrument (13) is connected with computer (21);
Described second pond (3) connects anaerobic zone (5) and oxygen-starved area (6) by sludge reflux pump (11) respectively.
2. A
2/ O oxidation trench technology synchronous nitration denitrification control method is characterized in that this method may further comprise the steps:
1) active sludge that contains polyP bacteria, denitrifying bacteria and nitrifier is added in the oxidation ditch main body (2), carry out the domestication and the cultivation of bacterial classification, make the activated sludge concentration in the oxidation ditch main body (2) maintain 4000mg/L～6000mg/L;
2) with raw waste water from water tank (1) pump to anaerobic zone (5), mix with 30% returned sluge that the sludge reflux pump that is connected anaerobic zone (5) (11) refluxes, after anaerobic zone on average stops 40～60 minutes, enter oxygen-starved area (6);
3) after the muddy water of discharging in the above-mentioned anaerobic zone (5) enters oxygen-starved area (6), mix, after oxygen-starved area (6) on average stop 60～80 minutes, enter oxidation ditch aeration pond (7) with 70% returned sluge that the sludge reflux pump that is connected oxygen-starved area (6) (11) refluxes;
4) after the muddy water of above-mentioned oxygen-starved area (6) discharge enters in the oxidation ditch aeration pond (7), start frequency conversion gas blower (14) and provide oxygen for the aeration head (17) that is arranged in aeration tank (7), treating water is carried out blast aeration, computer (21) is adjusted the power of frequency conversion gas blower (14) according to the registration of DO on-line monitoring instrument (12) and ORP on-line monitoring instrument (13), the registration of DO on-line monitoring instrument (12) is controlled in 0.8mg/L to the 0.1mg/L scope, and the registration of ORP on-line monitoring instrument (13) is controlled at-30mv～30mv scope in, treating water in oxidation ditch aeration pond (7) average hydraulic detention time after 18 hours draining enter in the second pond (3);
5) treating water that overflows from oxidation ditch aeration pond (7) enters second pond (3) and carries out mud-water separation, and supernatant liquor is discharged system, and returned sluge is back to anaerobic zone (5) and oxygen-starved area (6) respectively in 3: 7 ratio.
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