CN101723554B - Chemical fertilizer waste water treatment method - Google Patents
Chemical fertilizer waste water treatment method Download PDFInfo
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- CN101723554B CN101723554B CN2009102144783A CN200910214478A CN101723554B CN 101723554 B CN101723554 B CN 101723554B CN 2009102144783 A CN2009102144783 A CN 2009102144783A CN 200910214478 A CN200910214478 A CN 200910214478A CN 101723554 B CN101723554 B CN 101723554B
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- 239000003337 fertilizer Substances 0.000 title claims abstract description 28
- 239000000126 substance Substances 0.000 title claims abstract description 17
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000002351 wastewater Substances 0.000 claims abstract description 49
- 238000005273 aeration Methods 0.000 claims abstract description 40
- 239000001301 oxygen Substances 0.000 claims abstract description 33
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 33
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 238000004062 sedimentation Methods 0.000 claims abstract description 25
- 238000010992 reflux Methods 0.000 claims abstract description 21
- 230000001105 regulatory Effects 0.000 claims abstract description 9
- 229920002401 polyacrylamide Polymers 0.000 claims abstract description 7
- 238000001556 precipitation Methods 0.000 claims abstract description 5
- 239000010802 sludge Substances 0.000 claims description 58
- 241000276438 Gadus morhua Species 0.000 claims description 40
- 235000019516 cod Nutrition 0.000 claims description 40
- 230000000694 effects Effects 0.000 claims description 36
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound [N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 claims description 25
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 24
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 20
- 229910052757 nitrogen Inorganic materials 0.000 claims description 12
- 206010042602 Supraventricular extrasystoles Diseases 0.000 claims description 9
- 238000005189 flocculation Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 230000016615 flocculation Effects 0.000 claims description 8
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- FGIUAXJPYTZDNR-UHFFFAOYSA-N Potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000006396 nitration reaction Methods 0.000 abstract description 5
- 238000000034 method Methods 0.000 abstract description 3
- 206010002660 Anoxia Diseases 0.000 abstract description 2
- 241000976983 Anoxia Species 0.000 abstract description 2
- 238000004886 process control Methods 0.000 abstract description 2
- 239000010865 sewage Substances 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 abstract 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract 1
- 239000008394 flocculating agent Substances 0.000 abstract 1
- 238000005086 pumping Methods 0.000 abstract 1
- 231100000486 side effect Toxicity 0.000 abstract 1
- 231100000331 toxic Toxicity 0.000 abstract 1
- 238000011068 load Methods 0.000 description 11
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 8
- 150000002989 phenols Chemical class 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 239000012535 impurity Substances 0.000 description 5
- 230000001473 noxious Effects 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000010815 organic waste Substances 0.000 description 4
- 150000001299 aldehydes Chemical class 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- NRADCUWKNUKPHY-UHFFFAOYSA-N oxalonitrile;phenol Chemical class N#CC#N.OC1=CC=CC=C1 NRADCUWKNUKPHY-UHFFFAOYSA-N 0.000 description 3
- 230000002093 peripheral Effects 0.000 description 3
- -1 carbon nitrogen Chemical compound 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 239000000618 nitrogen fertilizer Substances 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 230000037250 Clearance Effects 0.000 description 1
- JMANVNJQNLATNU-UHFFFAOYSA-N Cyanogen Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 1
- 241000108664 Nitrobacteria Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000035512 clearance Effects 0.000 description 1
- 230000001351 cycling Effects 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000003311 flocculating Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 231100000224 toxic side effect Toxicity 0.000 description 1
Abstract
The invention provides a chemical fertilizer waste water treatment process control method. The process comprises the following steps of: homogenizing chemical fertilizer waste water through a regulating pool; then pumping the waste water in the regulating pool into a primary aeration tank by utilizing a sewage pump so as to primarily remove COD (chemical oxygen demand) and relieve toxic and side effects for a subsequent biological and chemical system; after the waste water is treated by a primary sedimentation tank, ensuring that the waste water enters an A/O (anacrobic/oxic) biological denitrification system and a subsequent materialization deep treatment system; keeping DO (dissolved oxygen) of a pool A (anoxia pool) being below 0.5mg/L and the water flow of nitration liquid refluxing from a pool O (oxic pool) being 3-5 times of that of inlet water; maintaining the pH of the pool O to be 6.5-8.5 and the DO to be 2-3mg/L; and regulating to a proper mud reflux ratio so as to ensure that the biological and chemical system can be efficiently and stably operated. The materialization deep treatment system is used for adding flocculating agents PAC (polyaluminium chloride) and PAM (polyacrylamide), and after reaction and precipitation, outlet water can reach the national first-level discharge standard.
Description
Technical field
The present invention relates to a kind of chemical fertilizer waste water treatment method, relate in particular to a kind of treatment process control method that is used for the ammonia nitrogen in high density fertilizer waste water.
Background technology
In the fertilizer waste water, ammonia nitrogen concentration superelevation, carbon source relative deficiency are the technical barriers to its processing.For denitride technology, generally believe that at present biochemical treatment is the most cost-effective technology.Traditional bio-denitrification technology mainly contains the A/O method, A/A/O method etc., and these technologies all can be removed COD and ammonia nitrogen, but relatively are fit to municipal effluent, for high-concentration fertilizer waste water poor effect then., the influent load restriction long etc. of tracing it to its cause for nitrobacteria growth condition restriction, sludge age.Nitrifier is long generation time, is subject to into restrictions such as water pH, COD load, so most important to the operating parameter control of actual sewage factory.Waste water treatment process regulatory limits condition is more, and different quality, different technical parameters control differ bigger, cause many technologies not move in the best condition.
Summary of the invention
In order to overcome above-mentioned prior art restriction, it is low to the invention provides a kind of sludge treatment cost, and nitration denitrification carries out simultaneously, and the decarburization denitrification effect is good, and waste water can reach the chemical fertilizer waste water treatment method of reuse water standard.
The object of the invention is achieved through the following technical solutions:
Optimize the growing environment of nitrifier, the present invention adopts following technical matters and condition control:
Operational path of the present invention is: equalizing tank-elementary aeration tank-preliminary sedimentation tank-A/O biological denitrificaion unit (anoxic pond-Aerobic Pond 1-Aerobic Pond 2-second pond)-flocculation sedimentation tank)-and water outlet.In elementary aeration tank and A/O biological denitrificaion unit use active sludge, active sludge removes materials such as carbon nitrogen in the water by its vital movement.High ammonia nitrogen fertilizer waste water stopped 3-5 hour mixing fully in the equalizing tank, by the even water quality of blast aeration.Evenly the waste water after the water quality is removed the hazardous and noxious substances in the water inlet, and is tentatively removed about COD50% through the strong aeration effect of elementary aerating apparatus.Aeration tank dissolved oxygen is suitably adjusted according to the water inlet condition, when the COD load surpasses 1200mg/L dissolved oxygen is controlled at 1.5mg/L; Dissolved oxygen was controlled at about 1mg/L when the COD load was low.
Operation control comprises: elementary aeration tank dissolved oxygen level, pH, temperature; Dissolved oxygen in anoxic tank, COD; Aerobic Pond dissolved oxygen, COD, pH; Under water outlet state still not up to standard, use flocculation tank, add flocculation agent PAC, mix adding PAC and PAM when flocculating effect is not good.
The operational conditions control of elementary aeration tank: the effect of elementary aeration tank is to remove objectionable impurities such as phenol, cyanogen etc. in the waste water, and pH is controlled in the 6.5-8.5 active sludge normal growth scope, and dissolved oxygen is controlled at 1-2mg/L.Control parameter adjustment when influent load changes: because the fluctuation of producing, when water inlet COD was lower than 500mg/L, dissolved oxygen was controlled at 1-2mg/L; When water inlet COD was lower than 200mg/L, dissolved oxygen was controlled at 0.8-1mg/L, and pH is controlled at 6.0-7.5, can just expose to the sun the accumulation of pond realization nitrite nitrogen to save follow-up denitrifying carbon source.Mud is back to elementary aeration tank by preliminary sedimentation tank, and control of reflux ratio guarantees that at 1: 1 just the aeration tank sludge concentration is at 2000-3000mg/L; Winter the active sludge poor growth, in order to guarantee the COD removal effect, the mud quantity of reflux is transferred to 1.5: 1-2: 1, suitably increase activated sludge concentration, excess sludge drains into mud-collecting well.
The control of anoxic pond operational conditions: nitrification liquid is back to anoxic pond through Aerobic Pond and carries out denitrification, and the nitrification liquid control of reflux ratio can reach denitrification effect preferably at 3: 1.Denitrifying limiting factor comprises COD and dissolved oxygen levels.Control dissolved oxygen in anoxic tank level is below the 0.5mg/L, and this condition is easier to control, and common stirring draw can reach requirement; COD is the limiting factor of anoxic pond denitrification effect often, and especially for high ammonia nitrogen fertilizer waste water, carbon source lacks relatively.In conjunction with field condition, effectively utilization can utilize carbon source, adds COD directly to the anoxic pond origin or beginning, guarantees that the C/N ratio reaches 3-5 in the pond.
The control of Aerobic Pond operational conditions: Aerobic Pond mainly carries out nitrification, and its limiting factor comprises COD, pH, dissolved oxygen, return sludge ratio etc.No. 1 Aerobic Pond COD is no more than 300mg/L, otherwise will suppress the growth of nitrifier; PH is controlled at 7-8.5, and conventional active sludge need add yellow soda ash and regulate basicity, this process using active sludge, and after domestication, tolerance is stronger, can add the caustic soda waste liquid in order to save cost; Dissolved oxygen is adjusted in real time according to operational conditions, and the higher time control dissolved oxygen of loading is in the relative higher level of 3-4mg/L, and dissolved oxygen maintains about 2mg/L during underrun; Return sludge ratio is controlled at 1.5: 1-2: 1, and the maintenance sludge concentration is 3000-4000mg/L, winter temperature can suitably improve return sludge ratio when low, to guarantee sludge concentration and treatment effect.
Flocculation tank operational conditions control: come into operation under the situations that exceed standard such as water outlet COD, SS, add flocculation agent PAC and PAM, dosage adds according to the ratio of PAC100ppm/ ton waste water and PAM1ppm/ ton waste water, suitably increases and decreases the dosage of PAC according to the water outlet effect.Because PAM is an objectionable impurities, under the situation that water outlet allows, can only add PAC.
Among the present invention, waste water passes through elementary aerating system, A/O biological denitrificaion unit, materialization advanced treatment unit successively, by parameters such as optimal control dissolved oxygen, pH, dosage, return sludge ratio and nitrification liquid reflux ratios, water outlet is reached even be better than emission standard.Can reach more than 90% for high ammonia-nitrogen wastewater COD clearance, ammonia nitrogen removal frank can reach more than 99%.
The present invention has following advantage and beneficial effect with respect to prior art:
(1) the generation surplus sludge volume is few, saves the sludge treatment cost;
(2) select active sludge for use, anti impulsion load more, anti-hazardous and noxious substances effectively improves the stability of biochemical system;
(3) control Aerobic Pond dissolved oxygen content can make nitration denitrification carry out simultaneously, improves denitrification effect;
(4) use the caustic soda waste liquid to regulate Aerobic Pond pH value, effectively save cost.
(5) waste water after the materialization advanced treatment can reach the reuse water standard, is used for the cycling use of water in the fertilizer plant, reaches the purpose of resource utilization and energy-saving and emission-reduction.
Description of drawings
Fig. 1 is embodiment 1 each pond COD concentration curve figure;
Fig. 2 is embodiment 1 each pond ammonia nitrogen concentration change curve;
Fig. 3 is embodiment 2 each pond COD concentration curve figure;
Fig. 4 is embodiment 2 each pond ammonia nitrogen concentration change curve;
Fig. 5 is embodiment 3 each pond COD concentration curve figure;
Fig. 6 is that embodiment 3 each pond ammonia nitrogen concentration change histogram;
Fig. 7 is system's aldehydes matter change in concentration figure among the embodiment 3.
Embodiment
The present invention is further illustrated below in conjunction with drawings and Examples, but embodiment does not constitute the restriction to the claimed scope of the present invention.
Embodiment 1
After blast aeration mixes in equalizing tank, fertilizer plant's waste water index: CODcr=1000-1200mg/L, SS=200mg/L, NH
3-N=200-300mg/L, pH=6～9.Equalizing tank comes water to comprise high content of ammonia and nitrogen in fertilizer factory fertilizer waste water and organic waster-water, and according to treatment capacity and factory effluent water displacement configuration adjustment pond load, unnecessary waste water is enabled accident pool and temporarily stored.Adopt continuous water distribution mode, allocate ammonia nitrogen waste water and organic waste water into equalizing tank according to 4: 1 flowrate proportioning, treatment capacity is 120m
3/ h.
Waste water behind the homogeneous pumps into blast aeration hybrid elementary aeration tank fully, keep dissolved oxygen about 1.5mg/L, can tentatively remove COD, make rest COD maintain 300-500mg/L, mixed liquid concentration 2000-3000mg/L, pH maintains 6.5-8.5, return sludge ratio 1.5: 1, hydraulic detention time 2h is in this pond, by strong aeration effect, and the phenol cyanogen class hazardous and noxious substances that contains in the vital movement removal waste water by active sludge.Operation result: elementary aeration tank water outlet CODcr=300-500mg/L, NH
3-N=100-200mg/L, SS=50-80mg/L.Waste water enters preliminary sedimentation tank after through the pond of just exposing to the sun, and preliminary sedimentation tank is back to through precipitation part mud and just exposes to the sun the pond to keep the sludge concentration in the pond, and excess sludge drains into mud-collecting well.
Through behind the preliminary sedimentation tank, waste water enters A/O biological denitrificaion unit.In the A/O biological denitrificaion unit, anoxic pond is installed two QJB type diving mixers, to guarantee that mud is in suspended state, simultaneously can keep dissolved oxygen levels below 0.5mg/L, thereby active sludge carries out denitrification vital movement deviate to reflux nitrogen in the nitrification liquid in anoxic pond, this pond utilizes the preliminary sedimentation tank rest COD, and the C/N mol ratio is generally more than 3.Active sludge carries out nitrification in Aerobic Pond, ammonia nitrogen is converted into nitre nitrogen for follow-up denitrification, and Aerobic Pond adopts ARE190 type roots blower air blast micro-pore aeration, and the micro-pore aeration gas distribution is even, can satisfy the vital movement of active sludge.Wherein, No. 1 Aerobic Pond is regulated dissolved oxygen to 3-5mg/L by adding caustic soda waste liquid (concentration is 32%) control pH value in the 7-8.5 scope; Mixed liquid concentration is controlled at 3000-4000mg/L (realizing by spoil disposal and daily control).No. 2 the Aerobic Pond dissolved oxygen levels transfers to 2mg/L, the nitrification liquid reflux ratio of Aerobic Pond after nitrated 3: 1, and to guarantee the denitrification effect of water outlet, the big more denitrification effect of nitrification liquid reflux ratio is good more in theory, considers that simultaneously economic factors adopted reflux ratio 3: 1; Return sludge ratio adopted 1.5: 1, with sludge concentration and the nitrification effect of keeping Aerobic Pond; The nitrification liquid of Aerobic Pond after nitrated is back to anoxic pond by No. 2 Aerobic Ponds, and mud is back to anoxic pond and No. 1 Aerobic Pond by second pond.The radical sedimentation basin of second pond employing center water inlet peripheral effluent, sludge part is back to anoxic pond and No. 1 Aerobic Pond, and excess sludge drains into mud-collecting well.Through after the above art breading, water outlet COD=30-80mg/L, NH
3-N＜10mg/L can reach national grade one discharge standard (GB8978-1996).Need not to use the materialization advanced treatment system.
Fig. 1 is under the higher relatively running status of equalizing tank COD level, the treatment effect figure in each pond in the treatment system.Through behind the pond of just exposing to the sun, COD removes about 50% substantially as seen from the figure, passes through the further removal of denitrogenation unit activity mud effect again, and water outlet COD is stabilized in below the 100mg/L.
Fig. 2 is the ammonia nitrogen removal design sketch in each pond in the treatment system.As seen from the figure, ammonia nitrogen does not have removal substantially at preliminary sedimentation tank.Mainly from water, remove through follow-up nitration denitrification effect.
Embodiment 2
After blast aeration mixes in equalizing tank, fertilizer plant's waste water index: COD=100-300mg/L, SS=50-100mg/L, NH
3-N=100-200mg/L.Equalizing tank comes water to comprise high content of ammonia and nitrogen in fertilizer factory fertilizer waste water and organic waster-water, and organic waste water concentration is ultralow under the accidental state, and the organic loading of total system reduces.Adopt continuous water distribution mode, allocate ammonia nitrogen waste water and organic waste water into equalizing tank respectively, treatment capacity is 150m
3/ h.
In equalizing tank, it is mixed the high content of ammonia and nitrogen in fertilizer factory fertilizer waste water, 3 hours residence time by blast aeration.Waste water behind the homogeneous pumps into elementary aeration tank, regulate dissolved oxygen to 0.8mg/L, mixed liquid concentration 2000mg/L, pH maintains 6.5-8.5, return sludge ratio 1: 1, hydraulic detention time 2h removes the phenol cyanogen class hazardous and noxious substances that contains in the waste water by strong aeration effect by the vital movement of active sludge in this pond.Operation result: elementary aeration tank water outlet CODcr=100-150mg/L, NH
3-N=50-100mg/L, SS=50-80mg/L.Waste water enters preliminary sedimentation tank after through the pond of just exposing to the sun, and preliminary sedimentation tank is back to through precipitation part mud and just exposes to the sun the pond to keep the sludge concentration in the pond, and excess sludge drains into mud-collecting well.Through behind the preliminary sedimentation tank, waste water enters A/O biological denitrificaion unit.Because water inlet COD concentration can't reach processing requirements, need the people for adding carbon source to the anoxic pond origin or beginning, guarantee that anoxic pond C/N mol ratio reaches more than 3, this pond dissolved oxygen levels is controlled at 0.5mg/L following (realizing by the diving mixer effect), thereby active sludge carries out denitrification vital movement deviate to reflux nitrogen in the nitrification liquid in this pond.Active sludge carries out nitrated activity in Aerobic Pond, ammonia nitrogen is converted into nitre nitrogen for follow-up denitrification, and Aerobic Pond adopts ARE190 type roots blower air blast micro-pore aeration, and the micro-pore aeration gas distribution is even, can satisfy the vital movement of active sludge.No. 1 Aerobic Pond is regulated dissolved oxygen to 2-4mg/L by adding caustic soda waste liquid (concentration is 32%) control pH value in the 7-8.5 scope; Mixed liquid concentration is controlled at 3000mg/L (realizing by spoil disposal and daily control).No. 2 the Aerobic Pond dissolved oxygen levels transfers to 2mg/L, nitrification liquid reflux ratio 3: 1, and to guarantee the denitrification effect of water outlet, the big more denitrification effect of nitrification liquid reflux ratio is good more in theory, considers that simultaneously economic factors adopted reflux ratio 3: 1; Return sludge ratio adopted 1.0: 1, with sludge concentration and the nitrification effect of keeping Aerobic Pond; Nitrification liquid is back to anoxic pond by No. 2 Aerobic Ponds, and mud is back to anoxic pond and No. 1 Aerobic Pond by second pond.The radical sedimentation basin of second pond employing center water inlet peripheral effluent, sludge part is back to anoxic pond and No. 1 Aerobic Pond, and excess sludge drains into mud-collecting well.Through after the above art breading, water outlet COD＜50mg/L, NH
3-N＜10mg/L can reach national grade one discharge standard (GB8978-1996).Need not to use the materialization advanced treatment system.
Fig. 3 is under the relatively low running status of equalizing tank COD level, the treatment effect figure in each pond in the treatment system.Through behind the pond of just exposing to the sun, COD has been in low-level as seen from the figure, can't satisfy denitrifying needs, thus the anoxic pond people for adding carbon source for follow-up denitrification.Under the underload treated state, water outlet COD is below the 50mg/L substantially.
Fig. 4 is the ammonia nitrogen removal design sketch in each pond in the treatment system.As seen from the figure, ammonia nitrogen does not have removal substantially at preliminary sedimentation tank.Mainly remove from water through follow-up nitration denitrification effect, underload does not cause intensive to impact to system.
Embodiment 3
After blast aeration mixes in equalizing tank, fertilizer plant's waste water index: COD=600-1000mg/L, SS=50-100mg/L, NH
3-N=100-200mg/L, phenols=50mg/L.Equalizing tank comes water to comprise high content of ammonia and nitrogen in fertilizer factory fertilizer waste water and organic waster-water, and according to treatment capacity and factory effluent water displacement configuration adjustment pond load, unnecessary waste water is enabled accident pool and temporarily stored.Adopt continuous water distribution mode, allocate ammonia nitrogen waste water and organic waste water into equalizing tank respectively, treatment capacity is 120m
3/ h.
Waste water behind the homogeneous pumps into elementary aeration tank, in order effectively to remove aldehydes matter is that toxic side effect is removed in follow-up biological denitrificaion unit, regulate dissolved oxygen to 2mg/L, mixed liquid concentration 3000mg/L, pH maintains 6.5-8.5, return sludge ratio 1.5: 1, hydraulic detention time 2h removes the phenol cyanogen class hazardous and noxious substances that contains in the waste water by strong aeration effect by the vital movement of active sludge in this pond.Operation result: elementary aeration tank water outlet CODcr=300-400mg/L, NH
3-N=50-100mg/L, SS=50-80mg/L, phenols＜10mg/L.Waste water enters preliminary sedimentation tank after through the pond of just exposing to the sun, and preliminary sedimentation tank is back to through precipitation part mud and just exposes to the sun the pond to keep the sludge concentration in the pond, and excess sludge drains into mud-collecting well.Through behind the preliminary sedimentation tank, waste water enters A/O biological denitrificaion unit.Anoxic pond adopts two QJB type agitators under water, guarantee to keep when mud is in suspended state dissolved oxygen levels below 0.5mg/L, remove nitrogen in the nitrated phegma thereby denitrifying bacteria carries out denitrification under organic carbon source and anoxia condition in this pond; Thereby active sludge carries out denitrification vital movement deviate to reflux nitrogen in the nitrification liquid in this pond, this pond utilizes the preliminary sedimentation tank rest COD, and the C/N mol ratio maintains more than 3 substantially.Active sludge carries out nitrated activity in Aerobic Pond, ammonia nitrogen is converted into nitre nitrogen for follow-up denitrification, and Aerobic Pond adopts ARE190 type roots blower air blast micro-pore aeration, and the micro-pore aeration gas distribution is even, can satisfy the vital movement of active sludge.No. 1 Aerobic Pond is regulated dissolved oxygen to 2-4mg/L by adding caustic soda waste liquid (concentration is 32%) control pH value in the 7-8.5 scope; Mixed liquid concentration is controlled at 3000mg/L (realizing by spoil disposal and daily control).No. 2 the Aerobic Pond dissolved oxygen levels transfers to 2mg/L, nitrification liquid reflux ratio 3: 1, and to guarantee the denitrification effect of water outlet, the big more denitrification effect of nitrification liquid reflux ratio is good more in theory, considers that simultaneously economic factors adopted reflux ratio 3: 1; Return sludge ratio adopted 1.0: 1, with sludge concentration and the nitrification effect of keeping Aerobic Pond; Nitrification liquid is back to anoxic pond by No. 2 Aerobic Ponds, and mud is back to anoxic pond and No. 1 Aerobic Pond by second pond.The radical sedimentation basin of second pond employing center water inlet peripheral effluent, sludge part is back to anoxic pond and No. 1 Aerobic Pond, and excess sludge drains into mud-collecting well.The second pond water outlet enters the materialization advanced treatment system, adds flocculation agent PAC 100ppm/ ton waste water, behind the grid flocculation sloping plate deposition, and water outlet COD＜50mg/L, NH
3-N＜10mg/L, SS＜10mg/L, phenols does not detect, and can reach national grade one discharge standard (GB8978-1996).
Fig. 5 when in the water of source, containing objectionable impurities such as phenols system to the ability that removes of COD.As seen from the figure, under the obvious state of source water quality fluctuation, elementary aeration tank can reduce load variations to the unitary influence of follow-up biological denitrificaion, and COD is controlled at reasonable level with the preliminary sedimentation tank water outlet.
Fig. 6 ammonia nitrogen concentration change curve in the system when in the water of source, containing objectionable impurities such as phenols.As seen from the figure, obviously, illustrate that strong aeration effect has certain effect to the removal of ammonia nitrogen before ammonia nitrogen changes in elementary aerating system.
Fig. 7 is the change in concentration histogram of objectionable impurities in system such as phenols in the water of source.As seen from the figure, removing most of aldehydes matter substantially, make the level that its concentration is reduced to does not influence follow-up biological denitrification system through after the strong aeration effect of elementary aerating system.
Claims (3)
1. chemical fertilizer waste water treatment method is characterized in that comprising the steps and processing condition:
(1) equalizing tank is regulated: the blast aeration facility of fertilizer plant's ammonia nitrogen in high density fertilizer waste water at the bottom of by equalizing tank mixes it, and COD concentration is 500-1200mg/L in the equalizing tank, and ammonia nitrogen concentration is 100-300mg/L;
(2) handle elementary aeration tank: the fertilizer waste water after equalizing tank is regulated pumps into elementary aeration tank, regulate DO to 1-1.5mg/L, tentatively remove COD, and to make rest COD content be 300-500mg/L, to satisfy the needs of follow-up biochemical system, regulate pH to 6.5-8.5 with waste lye;
(3) preliminary sedimentation tank is handled: waste water enters preliminary sedimentation tank through behind the elementary aeration tank, preliminary sedimentation tank is back to elementary aeration tank to keep the sludge concentration in the pond through precipitation part mud, excess sludge drains into mud-collecting well, quantity of reflux is controlled at 1-2: 1, guarantee that elementary aeration tank sludge concentration is at 2000-3000mg/L;
(4) the A/O biological denitrificaion is handled: waste water is converted into nitrification liquid based on nitre nitrogen in the nitrification of Aerobic Pond by nitrifier, nitrification liquid is back to anoxic pond through No. 2 Aerobic Ponds and carries out denitrification, adjust nitrification liquid reflux ratio 3-5 according to the denitrification effect: 1, control dissolved oxygen in anoxic tank level is below the 0.5mg/L, mud is back to anoxic pond and No. 1 Aerobic Pond by second pond, and reflux ratio was respectively 1: 1 and 1.5: 1; Control C/N mol ratio is more than 3, needs the people for adding carbon source to the anoxic pond origin or beginning when source water can't satisfy the demands; Control No. 1 Aerobic Pond COD and be no more than 300mg/L, pH is controlled at 7-8.5, and the control dissolved oxygen is at 2-4mg/L; Return sludge ratio is controlled at 1.5: 1-2: 1, and the maintenance sludge concentration is 3000-4000mg/L; Fertilizer waste water after No. 2 Aerobic Pond is handled is discharged through second pond.
2. chemical fertilizer waste water treatment method according to claim 1, it is characterized in that: if water COD and SS that second pond is discharged exceed standard, water outlet enters flocculation sedimentation tank and handles, add flocculation agent PAC, or adding PAC and PAM, the PAC dosage adds according to 100ppm/ ton waste water, and the PAM dosage adds according to 1ppm/ ton waste water.
3. chemical fertilizer waste water treatment method according to claim 1 is characterized in that: the pH value of described step (3) is controlled at 7-8.5 by adding the caustic soda waste liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102144783A CN101723554B (en) | 2009-12-31 | 2009-12-31 | Chemical fertilizer waste water treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102144783A CN101723554B (en) | 2009-12-31 | 2009-12-31 | Chemical fertilizer waste water treatment method |
Publications (2)
| Publication Number | Publication Date |
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| CN101723554A CN101723554A (en) | 2010-06-09 |
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| CN102225828B (en) * | 2011-05-25 | 2013-02-13 | 华南理工大学 | Optimization method for fertilizer wastewater treatment process |
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