CN101863597B - High ammonia nitrogen sewage processing method - Google Patents
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- CN101863597B CN101863597B CN 201010210946 CN201010210946A CN101863597B CN 101863597 B CN101863597 B CN 101863597B CN 201010210946 CN201010210946 CN 201010210946 CN 201010210946 A CN201010210946 A CN 201010210946A CN 101863597 B CN101863597 B CN 101863597B
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- 239000010865 sewage Substances 0.000 title claims abstract description 78
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 238000003672 processing method Methods 0.000 title claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000010802 sludge Substances 0.000 claims abstract description 32
- 238000000034 method Methods 0.000 claims abstract description 19
- 238000001914 filtration Methods 0.000 claims abstract description 15
- 230000015556 catabolic process Effects 0.000 claims abstract description 12
- 238000006731 degradation reaction Methods 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 11
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 27
- 239000012528 membrane Substances 0.000 claims description 26
- 238000012545 processing Methods 0.000 claims description 25
- 239000000945 filler Substances 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 17
- 238000001223 reverse osmosis Methods 0.000 claims description 15
- 239000002689 soil Substances 0.000 claims description 15
- 239000000377 silicon dioxide Substances 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical group OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 230000029087 digestion Effects 0.000 claims description 7
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 claims description 6
- 238000006396 nitration reaction Methods 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 6
- 238000009287 sand filtration Methods 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 6
- 206010002660 Anoxia Diseases 0.000 claims description 3
- 241000976983 Anoxia Species 0.000 claims description 3
- 206010021143 Hypoxia Diseases 0.000 claims description 3
- 239000006004 Quartz sand Substances 0.000 claims description 3
- 238000005273 aeration Methods 0.000 claims description 3
- 230000007953 anoxia Effects 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 3
- 230000001376 precipitating effect Effects 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 6
- 239000003344 environmental pollutant Substances 0.000 abstract description 5
- 231100000719 pollutant Toxicity 0.000 abstract description 5
- 238000005189 flocculation Methods 0.000 abstract description 2
- 230000016615 flocculation Effects 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 238000003911 water pollution Methods 0.000 abstract description 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000004062 sedimentation Methods 0.000 abstract 1
- 238000013461 design Methods 0.000 description 42
- 239000000126 substance Substances 0.000 description 14
- 239000000463 material Substances 0.000 description 12
- 238000000746 purification Methods 0.000 description 12
- 238000002360 preparation method Methods 0.000 description 8
- 239000002033 PVDF binder Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 230000003203 everyday effect Effects 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 210000002249 digestive system Anatomy 0.000 description 2
- -1 COD Chemical compound 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000002054 inoculum Substances 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
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- 230000002459 sustained effect Effects 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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Abstract
The invention discloses a high ammonia nitrogen sewage processing method, which mainly comprises the following steps: (1) storing and homogenizing the ammonia nitrogen sewage; (2) utilizing the prepared active sludge to biologically degrade COD, BOD and NH3-N pollutants in the sewage; (3) separating sludge from water in the sewage; (4) film separating the sewage. The method has the advantages that: (1) the active sludge prepared in a culture pond has the advantages of easy flocculation, easy block formation and good sedimentation, so the sludge-water separation speed is fast; (2) the prepared active sludge is utilized to biologically degrade the sewage, so the degradation effect on the ammonia nitrogen, COD and BOD is good; (3) film filtering treatment on the sewage is performed, so the pollutants and partial ion in the sewage can be further removed, the sewage after the film treatment can reach the standard and also can be recycled, the recycling of the resource can be realized, and the water pollution can be reduced.
Description
Technical field
The invention belongs to environmental technology field, specifically a kind for the treatment of process of high-ammonia-nitrogen sewage.
Background technology
High-ammonia-nitrogen sewage is that a kind of ammonia nitrogen concentration that modern industry produces is higher than municipal wastewater, it is generally acknowledged that ammonia nitrogen concentration is higher than the above sewage of 300mg/l.The ammonia composition volatilizees easily and causes the pollution of ambient air in the high-ammonia-nitrogen sewage, when adopting the routine biochemistry technical finesse, can produce restraining effect to biological inoculum because ammonia-nitrogen content is too high, has a strong impact on Biochemical Treatment; When adopting the ammonia stripping process, the stripping effect is unstable, blows out waste gas and does not do secondary treatment and will pollute atmospheric environment; Adopt the flash evaporation technology working cost high; Outer displacement hull can cause eutrophication, and water body sense organ shape is worsened, thereby reduces the water body aesthetic values; And the normal dissolved oxygen balance of water body is disturbed, and further impel water body to worsen; Reduce quality of water supply, increase the water treatment burden, thereby efflux the water treatment plant water factory can not be run well; Destroy the water ecology balance, the water body economic worth is reduced.Thereby anti-water-stop body high-ammonia-nitrogen sewage pollutes most important to social economy's sustained and coordinated development.
Summary of the invention
The objective of the invention is to solve problems of the prior art, the treatment process of the good high-ammonia-nitrogen sewage of a kind for the treatment of effect is provided.
Technical scheme of the present invention is: a kind of high ammonia nitrogen sewage processing method comprises the steps:
(1) ammonia-nitrogen sewage is pooled to equalizing tank, and the storage of carrying out the water yield reaches all closes;
(2) COD, BOD and the NH in the biological degradation sewage
3-N pollutent, its concrete operation method is: the sewage in the equalizing tank is mixed with return digestion liquid, carbon source, active sludge introduce denitrification tank, under anoxia condition, carry out anti-nitration reaction, sludge concentration is 5000mg/l～13000mg/l, hydraulic detention time is 1d～10d, then the returned sluge in the sewage after denitrification is processed and the settling tank is introduced digester and carry out nitration treatment, digester bottom continuous aeration, hydraulic detention time is 3d～20d;
(3) will carry out mud-water separation in the sewage introducing settling tank after the biological degradation processing, make a part of supernatant liquor after the precipitation be back to denitrification tank as the Digestive system in the step (2), part supernatant liquor enters intermediate pool and transfers pH to 6.1～6.5, a mud part that precipitates is sent into digester and is done the returned sluge use, a part is sent into cultivation pool and is used for the preparation of active sludge, and excess sludge is discharged;
(4) sewage in the intermediate pool is carried out membrane separation, sewage is made further filtration treatment.
Preferably, described carbon source is methyl alcohol.
The add-on of carbon source is decided according to the carbon-nitrogen ratio in the system in the described step (2), and the carbon-nitrogen ratio in the system is 100: 15 by weight.
The quantity of reflux of the middle return digestion liquid of described step (2) is 5～10 times of sewage load.
The quantity of reflux of returned sluge is 50～100% of sewage load in the described step (2).
The preparation method of described active sludge is: the middle partly precipitated mud of described step (3) is entered in the reactor of cultivation pool, establish filler in the described reactor, described filler is divided into two-layer, the upper strata is described soil ulmin, lower floor is silica, the mass ratio of soil ulmin and silica is 1: 2 in the filler, the dosage of filler is decided according to the amount of disposing of sewage, the filler total mass is for processing 30～50% of water total mass, and the introducing denitrification tank carries out the biological degradation processing to sewage described precipitating sludge is cultivated 10d～60d in reactor after.
The COD of sewage is≤2000mg/1 in the described intermediate pool, BOD≤900mg/l.
Described step (4) membrane separation comprises pretreatment system, first step reverse osmosis membrane treatment system and second stage reverse osmosis membrane treatment system, pretreatment system comprises sand filtration and filter element filtering, sand filtration adopts quartz sand to filter, filter core aperture in the filter element filtering system is 2-10 μ m, liquid by the two steps ro film processing system is to see through liquid, and the liquid by the two steps ro film processing system is not concentrated solution.
Selected film in the described step (4) is high pollution-resistant membrane.
The invention has the beneficial effects as follows: the active sludge that (1) prepares in cultivation pool has easy flocculation, easy consolidated block and the good characteristics of settleability, so mud-water separation speed is fast; (2) utilize the active sludge of preparation that sewage is carried out biological degradation, it is to the good degrading effect of ammonia nitrogen, COD, BOD; (3) sewage carries out the membrane filtration processing, and further except pollution substance and part ion in the decontaminated water, but the sewage qualified discharge after film is processed is also recyclable, realizes the recycling of resource, has reduced water pollution.
Description of drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
Fig. 1 is high-ammonia-nitrogen sewage processing technological flow figure of the present invention, and it comprises the steps:
(1) ammonia-nitrogen sewage is pooled to equalizing tank, and the storage of carrying out the water yield reaches all closes;
(2) COD, BOD and the NH in the biological degradation sewage
3-N pollutent, its concrete operation method is: with the sewage in the equalizing tank and return digestion liquid, carbon source, active sludge mixes introduces denitrification tank, under anoxia condition, carry out anti-nitration reaction, sludge concentration is 5000mg/l～13000mg/l, hydraulic detention time is 1d～10d, described carbon source is preferably methyl alcohol, the add-on of carbon source is decided according to the carbon-nitrogen ratio in the system, carbon-nitrogen ratio in the system is 100: 15 by weight, the quantity of reflux of return digestion liquid is 5～10 times of sewage load, then the returned sluge in the sewage after denitrification is processed and the settling tank is introduced digester and carry out nitration treatment, digester bottom continuous aeration, hydraulic detention time is 3d～20d, and the quantity of reflux of returned sluge is 50～100% of sewage load; The preparation method of described active sludge is: the middle partly precipitated mud of described step (3) is entered in the reactor of cultivation pool, establish filler in the described reactor, described filler is divided into two-layer, the upper strata is described soil ulmin, lower floor is silica, the mass ratio of soil ulmin and silica is 1: 2 in the filler, the dosage of filler is decided according to the amount of disposing of sewage, the filler total mass is for processing 30～50% of water total mass, and the introducing denitrification tank carries out the biological degradation processing to sewage described precipitating sludge is cultivated 10d～60d in reactor after.
(3) will carry out mud-water separation in the sewage introducing settling tank after the biological degradation processing, make a part of supernatant liquor after the precipitation be back to denitrification tank as the Digestive system in the step (2), part supernatant liquor enters intermediate pool and transfers pH to 6.1～6.5, a mud part that precipitates is sent into digester and is done the returned sluge use, a part is sent into cultivation pool and is used for the preparation of active sludge, and excess sludge is discharged; Sewage can't reach direct emission standard after carrying out above-mentioned degradation treatment, the general water outlet COD that processes is in 100～1000mg/l, for running cost and the cost that reduces integrated artistic, subsequent film is processed born certain load, reduce the hydraulic detention time that DeR is processed, so that being controlled at COD, the processing water outlet is≤2000mg/l BOD≤900mg/l.
(4) sewage in the intermediate pool is carried out membrane separation, sewage is done further to filter degraded, membrane separation comprises pretreatment system, first step reverse osmosis membrane treatment system and second stage reverse osmosis membrane treatment system, pretreatment system comprises sand filtration and filter element filtering, sand filtration adopts quartz sand to filter, filter core aperture in the filter element filtering system is 2～10 μ m, liquid by the two steps ro film processing system is to see through liquid, and the liquid by the two steps ro film processing system is not concentrated solution.See through liquid and can directly discharge or recycle processing, concentrated solution can carry out landfill or process.
Embodiment 1
The high-ammonia-nitrogen sewage that certain paper mill produces adopts the inventive method, and the designing treatment Total Water is 800t/d, and every day was by continuously operation design in 24 hours; Film processing unit flooding velocity is 33.3m
3/ h; Soil ulmin model in the present embodiment in the used filler of preparation active sludge is SH350, and the soil ulmin of this model is bought from the clear auspicious Co., Ltd. of Japan, and the particle diameter of the silica in the filler is 1mm～4mm.
1. influent quality
Table 1 high-ammonia-nitrogen sewage influent quality (unit: mg/l; PH value zero dimension)
| The pollutent index | COD Cr | BOD 5 | NH 3-N | SS | TN | Specific conductivity (μ S/cm) | pH |
| Pollutant levels | 15000 | 3750 | 2300 | 1200 | 2500 | 25000 | 6～8 |
2. membrane treatment process section design variable
800t/d high-ammonia-nitrogen sewage membrane treatment process adopts two-stage DTRO disc tube reverse osmosis (dt-ro) film processing system, and the part operating parameter is as follows:
Table 2 first step reverse osmosis membrane treatment system design variable
| Mould material | PVDF and PES material |
| The design Homes Using TV | 90％ |
| The design water purification rate of recovery | Q RO＝80％ |
| Design flooding velocity Qd | Qd＝800m 3/d |
| Design water purification production Q p | Qp＝640m 3/d |
| Film post quantity n RO | n RO=440 |
| Single the long-pending SRO of film cylinder | S RO＝9.405m 2 |
| The total filtration area SRO of film, t | S RO，t＝4326.3m 2 |
| Routine operating pressure | P Max＝55bar |
| The design maximum operating pressure | P Max＝75bar |
| The high-pressure pump number of units | 8 |
| Built-in online pump number of units | 2 |
Table 3 second stage reverse osmosis membrane treatment system design variable
| Mould material | PVDF and PES material |
| The design Homes Using TV | 90％ |
| The design water purification rate of recovery | Q RO＝90％ |
| Design flooding velocity Qd | Qd＝870m 3/d |
| Design water purification production Q p | Qp＝640m 3/d |
| Film post quantity n RO | n RO=100 |
| Single the long-pending SRO of film cylinder | S RO＝9.405m 2 |
| The total filtration area SRO of film, t | S RO，t＝940.5m 2 |
| Routine operating pressure | P Max＝40bar |
| The design maximum operating pressure | P Max＝70bar |
| The high-pressure pump number of units | 6 |
3. clearance situation
Among this embodiment in the denitrification tank sludge concentration be 7500mg/l～9620mg/l, the hydraulic detention time in the denitrification tank is 2.1d, the hydraulic detention time in the digester is 9d; Filler total amount in the cultivation pool is 15 tons, and wherein soil ulmin is 5 tons, and silica is 10 tons, and mud is cultivated in reactor after 29 days and made active sludge.
Table 4 high-ammonia-nitrogen sewage is processed the clearance effect
4. beneficial effect
Present embodiment can be processed 26.4 ten thousand tons of high-ammonia-nitrogen sewages every year, clears up chemical oxygen demand (COD) (CODcr): 3950 ton/years; Clear up five-day BOD (BOD
5): 987 ton/years; Clear up the NH3-N amount: 600 ton/years; Clear up suspended substance (SS): 315.2 ton/years.
Embodiment 2
The high-ammonia-nitrogen sewage that certain textile printing and dyeing factory produces adopts the inventive method, and the designing treatment Total Water is 400t/d, and every day was by continuously operation design in 24 hours; Film processing unit flooding velocity is 16.6m
3/ h; Soil ulmin model in the present embodiment in the used filler of preparation active sludge is SH350, and the soil ulmin of this model is bought from the clear auspicious Co., Ltd. of Japan, and the particle diameter of the silica in the filler is 1mm～4mm.
1. influent quality
Table 5 high-ammonia-nitrogen sewage influent quality (unit: mg/l; PH value zero dimension)
| The pollutent index | COD Cr | BOD 5 | NH 3-N | SS | TN | Specific conductivity (μ S/cm) | pH |
| Pollutant levels | 12340 | 3113 | 1893 | 786 | 2114 | 18790 | 7～8 |
2. membrane treatment process section design variable
400t/d high-ammonia-nitrogen sewage membrane treatment process adopts two-stage DTRO disc tube reverse osmosis (dt-ro) film processing system, and the part operating parameter is as follows:
Table 6 first step reverse osmosis membrane treatment system design variable
| Mould material | PVDF and PES material |
| The design Homes Using TV | 90％ |
| The design water purification rate of recovery | Q RO＝80％ |
| Design flooding velocity Qd | Qd＝400m 3/d |
| Design water purification production Q p | Qp＝320m 3/d |
| Film post quantity n RO | n RO=220 |
| Single the long-pending SRO of film cylinder | S RO＝9.405m 2 |
| The total filtration area SRO of film, t | S RO，t＝2165.2m 2 |
| Routine operating pressure | P Max＝45bar |
| The design maximum operating pressure | P Max＝55bar |
| The high-pressure pump number of units | 4 |
| Built-in online pump number of units | 2 |
Table 7 second stage reverse osmosis membrane treatment system design variable
| Mould material | PVDF and PES material |
| The design Homes Using TV | 90％ |
| The design water purification rate of recovery | Q RO＝90％ |
| Design flooding velocity Qd | Qd＝400m 3/d |
| Design water purification production Q p | Qp＝360m 3/d |
| Film post quantity n RO | n RO=50 |
| Single the long-pending SRO of film cylinder | S RO＝9.405m 2 |
| The total filtration area SRO of film, t | S RO，t＝480.3m 2 |
| Routine operating pressure | P Max＝30bar |
| The design maximum operating pressure | P Max＝40bar |
| The high-pressure pump number of units | 3 |
3. clearance situation
Among this embodiment in the denitrification tank sludge concentration be 6500mg/l～8500mg/l, the hydraulic detention time in the denitrification tank is 2.5d, the hydraulic detention time in the digester is 10.5d; Filler total amount in the cultivation pool is 9 tons, and wherein soil ulmin is 3 tons, and silica is 6 tons, and mud is cultivated in reactor after 35 days and made active sludge.
Table 8 high-ammonia-nitrogen sewage is processed the clearance effect
4. beneficial effect
Present embodiment can be processed 14.6 ten thousand tons of high-ammonia-nitrogen sewages every year, clears up chemical oxygen demand (COD) (CODcr): 1800 ton/years; Clear up five-day BOD (BOD
5): 454 ton/years; Clear up NH
3-N amount: 276 ton/years; Clear up suspended substance (SS): 270 ton/years.
Embodiment 3
The high-ammonia-nitrogen sewage that certain chemical plant produces adopts the inventive method, and the designing treatment Total Water is 200t/d, and every day was by continuously operation design in 24 hours; Film processing unit flooding velocity is 8.3m
3/ h; Soil ulmin model in the present embodiment in the used filler of preparation active sludge is SH350, and the soil ulmin of this model is bought from the clear auspicious Co., Ltd. of Japan, and the particle diameter of the silica in the filler is 1mm～4mm.
1. influent quality
Table 9 high-ammonia-nitrogen sewage influent quality (unit: mg/l; PH value zero dimension)
| The pollutent index | COD Cr | BOD 5 | NH 3-N | SS | TN | Specific conductivity (μ S/cm) | pH |
| Pollutant levels | 24603 | 4756 | 3378 | 634 | 3667 | 19800 | 6～7 |
2. membrane treatment process section design variable
200t/d high-ammonia-nitrogen sewage membrane treatment process adopts two-stage DTRO disc tube reverse osmosis (dt-ro) film processing system, and the part operating parameter is as follows:
Table 10 first step reverse osmosis membrane treatment system design variable
| Mould material | PVDF and PES material |
| The design Homes Using TV | 90％ |
| The design water purification rate of recovery | Q RO＝80％ |
| Design flooding velocity Qd | Qd＝200m 3/d |
| Design water purification production Q p | Qp＝180m 3/d |
| Film post quantity n RO | n RO=120 |
| Single the long-pending SRO of film cylinder | S RO＝9.405m 2 |
| The total filtration area SRO of film, t | S RO，t＝1128.6m 2 |
| Routine operating pressure | P Max＝45bar |
| The design maximum operating pressure | P Max＝55bar |
| The high-pressure pump number of units | 2 |
| Built-in online pump number of units | 2 |
Table 11 second stage reverse osmosis membrane treatment system design variable
| Mould material | PVDF and PES material |
| The design Homes Using TV | 90％ |
| The design water purification rate of recovery | Q RO＝90％ |
| Design flooding velocity Qd | Qd＝200m 3/d |
| Design water purification production Q p | Qp＝180m 3/d |
| Film post quantity n RO | n RO=25 |
| Single the long-pending SRO of film cylinder | S RO＝9.405m 2 |
| The total filtration area SRO of film, t | S RO，t＝235.5m 2 |
| Routine operating pressure | P Max＝40bar |
| The design maximum operating pressure | P Max＝70bar |
| The high-pressure pump number of units | 2 |
3. clearance situation
In the present embodiment in the denitrification tank sludge concentration be 9000mg/l～1000mg/l, the hydraulic detention time in the denitrification tank is 3.3d, the hydraulic detention time in the digester is 16d; Filler total amount in the cultivation pool is 6 tons, and wherein soil ulmin is 2 tons, and silica is 4 tons, and mud is cultivated in reactor after 45 days and made active sludge.
Table 12 high-ammonia-nitrogen sewage is processed the clearance effect
4. beneficial effect
Present embodiment can be processed 7.3 ten thousand tons of high-ammonia-nitrogen sewages every year, clears up chemical oxygen demand (COD) (CODcr): 1796 ton/years; Clear up five-day BOD (BOD
5): 340 ton/years; Clear up NH
3-N amount: 245 ton/years; Clear up suspended substance (SS): 46.28 ton/years.
Claims (8)
1. a high ammonia nitrogen sewage processing method is characterized in that: comprise the steps:
(1) ammonia-nitrogen sewage is pooled to equalizing tank, and the storage of carrying out the water yield reaches all closes;
(2) COD, BOD and the NH in the biological degradation sewage
3-N pollutent, its concrete operation method is: the sewage in the equalizing tank is mixed with return digestion liquid, carbon source, active sludge introduce denitrification tank, under anoxia condition, carry out anti-nitration reaction, sludge concentration is 5000mg/l～13000mg/l, hydraulic detention time is 1d～10d, then the returned sluge in the sewage after denitrification is processed and the settling tank is introduced digester and carry out nitration treatment, digester bottom continuous aeration, hydraulic detention time is 3d～20d;
(3) will carry out mud-water separation in the sewage introducing settling tank after the biological degradation processing, make a part of supernatant liquor after the precipitation be back to denitrification tank as the return digestion liquid in the step (2), part supernatant liquor enters intermediate pool and transfers pH to 6.1～6.5, a mud part that precipitates is sent into digester and is done the returned sluge use, a part enters in the reactor of cultivation pool and prepares active sludge, establish filler in the described reactor, described filler is divided into two-layer, the upper strata is described soil ulmin, lower floor is silica, the mass ratio of soil ulmin and silica is 1: 2 in the filler, the dosage of filler is decided according to the amount of disposing of sewage, the filler total mass is for processing 30～50% of water total mass, and the introducing denitrification tank carries out the biological degradation processing to sewage described precipitating sludge is cultivated 10d～60d in reactor after; Excess sludge is discharged;
(4) sewage in the intermediate pool is carried out membrane separation, sewage is made further filtration treatment.
2. high ammonia nitrogen sewage processing method according to claim 1, it is characterized in that: described carbon source is methyl alcohol.
3. high ammonia nitrogen sewage processing method according to claim 1 is characterized in that: the add-on of carbon source is decided according to the carbon-nitrogen ratio in the system in the described step (2), and the carbon-nitrogen ratio in the system is 100: 15 by weight.
4. high ammonia nitrogen sewage processing method according to claim 1 is characterized in that: the quantity of reflux of return digestion liquid is 5～10 times of sewage load in the described step (2).
5. high ammonia nitrogen sewage processing method according to claim 1 is characterized in that: the quantity of reflux of returned sluge is 50～100% of sewage load in the described step (2).
6. high ammonia nitrogen sewage processing method according to claim 1 is characterized in that: the COD of sewage is≤2000mg/l, BOD≤900mg/l in the described intermediate pool.
7. high ammonia nitrogen sewage processing method according to claim 1, it is characterized in that: described step (4) membrane separation comprises pretreatment system, first step reverse osmosis membrane treatment system and second stage reverse osmosis membrane treatment system, pretreatment system comprises sand filtration and filter element filtering, sand filtration adopts quartz sand to filter, filter core aperture in the filter element filtering system is 2-10 μ m, liquid by the two steps ro film processing system is to see through liquid, and the liquid by the two steps ro film processing system is not concentrated solution.
8. high ammonia nitrogen sewage processing method according to claim 7, it is characterized in that: selected film is high pollution-resistant membrane in the described step (4).
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| CN 201010210946 CN101863597B (en) | 2010-06-28 | 2010-06-28 | High ammonia nitrogen sewage processing method |
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| CN101863597B true CN101863597B (en) | 2013-04-03 |
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| CN106430811A (en) * | 2016-08-30 | 2017-02-22 | 陈亚松 | Highly toxic waste water pre-treatment device and use method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1159429A (en) * | 1995-07-20 | 1997-09-17 | 东洋生物反应株式会社 | Sewage treating method |
| JP2006255548A (en) * | 2005-03-16 | 2006-09-28 | Mitsui Eng & Shipbuild Co Ltd | Treatment apparatus for nitrogen-containing sewage |
| CN1935697A (en) * | 2006-10-13 | 2007-03-28 | 东南大学 | Integrated membrane biological fluidized bed sewage treating method and apparatus |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPH10296288A (en) * | 1997-04-22 | 1998-11-10 | Toyo Bio Reactor Kk | Sludge reforming method in batch type and oxidation ditch type waste water treatment method |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1159429A (en) * | 1995-07-20 | 1997-09-17 | 东洋生物反应株式会社 | Sewage treating method |
| JP2006255548A (en) * | 2005-03-16 | 2006-09-28 | Mitsui Eng & Shipbuild Co Ltd | Treatment apparatus for nitrogen-containing sewage |
| CN1935697A (en) * | 2006-10-13 | 2007-03-28 | 东南大学 | Integrated membrane biological fluidized bed sewage treating method and apparatus |
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