CN104310710A - High-efficiency energy-saving treatment process for coal chemical industry wastewater - Google Patents

High-efficiency energy-saving treatment process for coal chemical industry wastewater Download PDF

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CN104310710A
CN104310710A CN201410584174.7A CN201410584174A CN104310710A CN 104310710 A CN104310710 A CN 104310710A CN 201410584174 A CN201410584174 A CN 201410584174A CN 104310710 A CN104310710 A CN 104310710A
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waste water
aerobic
sludge
low
oxygen
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CN104310710B (en
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陈爱忠
洪卫
刘杰
刘勃
孙淑杰
邹晓凤
刘战修
张涛
王凯
谭心
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YANKUANG LUNAN CHEMICAL FERTILISER PLANT
Shandong Academy of Environmental Science
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YANKUANG LUNAN CHEMICAL FERTILISER PLANT
Shandong Academy of Environmental Science
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Abstract

The invention relates to a high-efficiency energy-saving treatment process for coal chemical industry wastewater. The process comprises the following steps: (1) adding a flocculating agent into coal chemical industry wastewater in a regulating reservoir, performing flocculating settling, thereby preparing coagulating settling wastewater and settling sludge; (2) introducing the coagulating settling wastewater into an air floatation machine, thereby preparing air floatation wastewater and air floatation sludge; (3) respectively introducing the air floatation wastewater into a low oxygenic aeration activated sludge pool and a high oxygenic aeration activated sludge pool for treatment, thereby preparing low oxygenic aeration wastewater and high oxygenic aeration wastewater; (4) introducing the low oxygenic aeration wastewater into a secondary sedimentation tank (I), performing sludge and water separation, preparing aerobic biochemical effluent (I) and aerobic settled sludge (I), and refluxing the aerobic settled sludge (I) back into the low oxygenic aeration activated sludge pool; and (5) mixing the aerobic biochemical effluent (I) with aerobic biochemical effluent (II), treating the effluent in an anaerobic reaction tank, thereby preparing the treated wastewater. According to the process disclosed by the invention, total nitrogen in the wastewater can be efficiently removed, and the aims of saving energy and efficiently treating the wastewater are achieved.

Description

The energy-efficient treatment process of a kind of coal chemical industrial waste water
Technical field
The present invention relates to the energy-efficient treatment process of a kind of coal chemical industrial waste water, belong to industrial waste water treatment.
Background technology
Coal chemical industry enterprises waste discharge, based on high density gas washing wastewater, containing hazardous and noxious substances such as a large amount of phenol, cyanogen, oil, ammonia nitrogens, belongs to that biochemical property is poor, organic pollutant is based on difficult degradation carbon source inferior, difficult degradation wastewater from chemical industry that C/N is lower.
At present, the selection and optimization that China's coal chemical industrial waste water is put into practice through many project, defines the treatment process of taking as the leading factor with biological treatment, as SBR, A/O, A 2/ O, inversion A 2/ O, CASS etc.
Chinese patent literature CN102633359A (application number 201210119771.3) discloses a kind for the treatment of process being applicable to nitrogenous wastewater from chemical industry total nitrogen, and the method comprises preaeration tank process and two-stage A/O treatment process; Waste water processes through preaeration tank, one-level anaerobic pond, one-level Aerobic Pond, secondary anaerobic pond, secondary Aerobic Pond, settling tank successively.Wherein can add denitrogenation microbial inoculum carry out biological reinforced at preaeration tank, one-level Aerobic Pond, two Aerobic Ponds.Present invention process flow process is simple, and leading portion adopts pre-exposure pond, can reduce the impact of organic loading on subsequent biochemical system, improve sewage treatment capacity, make technical process shorten simultaneously, reduces running cost.Adopt two-stage A/O art breading coal chemical industrial waste water, effectively can improve the removal efficiency of total nitrogen.
Chinese patent literature CN102249490A (application number 201110158915.1) discloses a kind of coal gasification wastewater treatment system and treatment process.Described treatment system comprises the grid, equalizing tank, Buffer Pool, EGSB reaction tank, Aerobic Pond and the second pond that connect successively; Described second pond is also connected with Buffer Pool with EGSB reaction tank respectively.
These techniques to some extent solve the pollution problem of COD and ammonia nitrogen in waste water, but it is lower to the removal efficiency of Determination of Total Nitrogen in Waste Water, and tradition " nitrification-denitrification " pattern is removed the mode of total nitrogen and is caused wastewater treatment costly (mainly to comprise the consumption that the power consumption of biochemical treatment and denitrifying carbon source add), traditional Anammox denitrogenation mode need add nitrite in waste water, and this adds the economical load of coal chemical industry enterprises to a certain extent.
Summary of the invention
The present invention is directed to the deficiencies in the prior art, the energy-efficient treatment process of coal chemical industrial waste water that a kind of nitric efficiency is high, working cost is low, energy-saving effect is remarkable, effluent quality is good is provided.
Technical scheme of the present invention is as follows:
The energy-efficient treatment process of a kind of coal chemical industrial waste water, comprises the steps:
(1) coal chemical industrial waste water in equalizing tank to be passed in coagulative precipitation tank and to add flocculation agent, through flocculating settling, obtained coagulating sedimentation waste water and precipitating sludge;
(2) the coagulating sedimentation waste water that step (1) is obtained is passed in air floatation machine, in air floatation machine, add flocculation agent, through flocculating settling, obtained air supporting waste water and air supporting mud;
(3) by air supporting waste water 1:(1.2 ~ 1.5 by volume obtained for step (2)) ratio pass into low-oxygen aeration activated sludge tank respectively and hyperoxia aerating activated sludge pond processes, obtained low-oxygen aeration waste water and hyperoxia aerating waste water;
Described low-oxygen aeration activated sludge tank treatment condition are: be under the condition of 0.5 ~ 0.8mg/L, sludge concentration 3000 ~ 4000mg/L at dissolved oxygen, hydraulic retention 24 ~ 36h;
Described hyperoxia aerating activated sludge pond treatment condition are: be under the condition of 3.0 ~ 4.0mg/L, sludge concentration 3500 ~ 4500mg/L at dissolved oxygen, hydraulic retention 24 ~ 36h;
(4) the low-oxygen aeration waste water that step (3) is obtained is passed into second pond (I), through mud-water separation, obtained aerobic biochemical water outlet (I) is become reconciled oxygen precipitation mud (I), and aerobic precipitating sludge (I) is back to low-oxygen aeration activated sludge tank;
The hyperoxia aerating waste water that step (3) is obtained passes into second pond (II), through mud-water separation, obtained aerobic biochemical water outlet (II) is become reconciled oxygen precipitation mud (II), and aerobic precipitating sludge (II) is back to low-oxygen aeration activated sludge tank;
(5) by after aerobic biochemical water outlet (I) obtained for step (4) and aerobic bio-chemical effluent (II) mixing, after anaerobic reation pool process, then through ultrafiltration, obtained processed waste water.
Preferred according to the present invention, in described step (1), flocculation agent is polymerize aluminum chloride and anionic polyacrylamide, and the add-on of polymerize aluminum chloride is 100 ~ 150mg/L, and the add-on of anionic polyacrylamide is 1 ~ 1.5mg/L; The flocculating settling time is 4 ~ 5h.
Preferred according to the present invention, in described step (2), flocculation agent is polymerize aluminum chloride and anionic polyacrylamide, and the add-on of polymerize aluminum chloride is 50 ~ 100mg/L, and the add-on of anionic polyacrylamide is 1 ~ 1.5mg/L; The flocculating settling time is 5 ~ 6h.
Preferred according to the present invention, in described step (3), the mud in hyperoxia aerating activated sludge pond is on sale in Initial stage of culture inoculation nitrifier BioRemove 5805, nitrifier BioRemove 5805 Novozymes Company of Denmark; Low-oxygen aeration active sludge takes from common municipal sewage plant aeration tank.
Preferred according to the present invention, in described step (3), described low-oxygen aeration activated sludge tank and hyperoxia aerating activated sludge pond are oxidation ditch formula structure, by the oxygen supply of blowing jet aerating system.
Preferred according to the present invention, in described step (3), the COD of low-oxygen aeration waste water and hyperoxia aerating waste water cr≤ 50mg/L.
Preferred according to the present invention, in described step (4), the reflux ratio of aerobic precipitating sludge (I) is 80 ~ 120%; The reflux ratio of aerobic precipitating sludge (II) is 150 ~ 200%.
Preferred according to the present invention, in described step (5), the mud in described anaerobic reation pool is anaerobic ammonia oxidizing bacteria, and hydraulic detention time is 34 ~ 36h.Anaerobic ammonia oxidizing bacteria is common commercially available prod, as: Shandong Huan Ke environmental science and technology company limited is on sale.
Preferred according to the present invention, in described step (5), ultrafiltration carries out ultrafiltration for adopting immersion ultra-filtration technique.
Preferred according to the present invention, also comprise and remaining aerobic precipitating sludge (I) after air supporting mud obtained to precipitating sludge obtained for step (1), step (2), step (4) backflow is become reconciled oxygen precipitation mud (II) after dehydration, dehydration filtrate passes into equalizing tank.
Beneficial effect
1, the present invention adopts low-oxygen aeration and hyperoxia aeration to combine the mode of process effluent part first, the biochemical ability of the biochemical treatment system of inoculation high efficiency nitrification bacterium is utilized in hyperoxia aeration process, be nitrite by the mineralized nitrogen in waste water, the efficient COD removed in waste water simultaneously.By the control to dissolved oxygen in low-oxygen aeration process, realize removing COD in waste water, ammonia nitrogen does not transform simultaneously; Then carry out anaerobic treatment after being mixed by the waste water processed in different ways, the efficient removal of Determination of Total Nitrogen in Waste Water can be realized, reach the object of energy-conservation and efficient process.
2, treatment process of the present invention, the large-minded amplitude of aeration requisite oxygen reduces, without the need to additional carbon or nitrite, power consumption and medicament expense low; By the scientific design to process workshop section, ingeniously achieve under comparatively less energy-consumption condition, to the efficient removal of COD, ammonia nitrogen, total nitrogen in waste water.
3, treatment process of the present invention, by the pretreatment mode that coagulating sedimentation and air supporting combine, the macrobead pollutents such as the coal ash on the one hand in efficient removal waste water, simultaneously to the oily substance efficient removal in waste water, to effectively prevent in waste water inorganic particle and petroleum substance to the impact of subsequent biochemical process, for subsequent biochemical process creates good conditions.
4, utilize anaerobic ammonia oxidizing bacteria as the major microorganisms of anaerobic treatment in treatment process of the present invention, anaerobic ammonia oxidizing bacteria is autotrophic type microorganism, whole reaction process without the need to organic carbon source, without the need to oxygen participate in, do not produce alkali, be a kind of economy, clean total nitrogen removing sulfuldioxide.In anaerobic reation pool, control pH is 7.5 ~ 8.0, and temperature is at 35 ~ 40 DEG C, and outputted aerobic water is processed by immersion filter tank, improves water outlet quality, is beneficial to Treated sewage reusing.
Embodiment
Below in conjunction with embodiment, technical scheme of the present invention is described further, but institute of the present invention protection domain is not limited thereto.
Material source
Low-oxygen aeration active sludge takes from common municipal sewage plant aeration tank.
Nitrifier BioRemove 5805, Novozymes Company of Denmark is on sale.
Anaerobic ammonia oxidizing bacteria, Shandong Huan Ke environmental science and technology company limited is on sale.
Embodiment 1
The coal chemical industrial waste water of Shandong synthetic ammonia coal chemical industry enterprises, index is: COD cr375mg/L, ammonia nitrogen 186mg/L, total nitrogen 213mg/L, SS 136mg/L.
Following treatment process is adopted to process above-mentioned coal chemical industrial waste water:
(1) being passed into by the coal chemical industrial waste water in equalizing tank in coagulative precipitation tank and to add polymerize aluminum chloride and anionic polyacrylamide, the add-on of polymerize aluminum chloride is 100mg/L, and the add-on of anionic polyacrylamide is 1.5mg/L; Through flocculating settling 4h, obtained coagulating sedimentation waste water and precipitating sludge;
(2) the coagulating sedimentation waste water that step (1) is obtained is passed in air floatation machine, polymerize aluminum chloride and anionic polyacrylamide is added in air floatation machine, the add-on of polymerize aluminum chloride is 100mg/L, the add-on of anionic polyacrylamide is 1mg/L, through flocculating settling 5h, obtained air supporting waste water and air supporting mud;
(3) ratio of air supporting waste water obtained for step (2) 1:1.2 is by volume passed into low-oxygen aeration activated sludge tank respectively and hyperoxia aerating activated sludge pond processes, obtained COD crthe low-oxygen aeration waste water of≤50mg/L and hyperoxia aerating waste water;
Described low-oxygen aeration activated sludge tank and hyperoxia aerating activated sludge pond are oxidation ditch formula structure, by the oxygen supply of blowing jet aerating system;
Described low-oxygen aeration activated sludge tank treatment condition are: be under the condition of 0.8mg/L, sludge concentration 4000mg/L at dissolved oxygen, hydraulic retention 36h;
The mud of described low-oxygen aeration activated sludge tank takes from common municipal sewage plant aeration tank.
Described hyperoxia aerating activated sludge pond treatment condition are: be under the condition of 4.0mg/L, sludge concentration 4500mg/L at dissolved oxygen, hydraulic retention 36h;
The mud in described hyperoxia aerating activated sludge pond is at Initial stage of culture inoculation nitrifier BioRemove 5805.
(4) the low-oxygen aeration waste water that step (3) is obtained is passed into second pond (I), through mud-water separation, obtained aerobic biochemical water outlet (I) is become reconciled oxygen precipitation mud (I), and aerobic precipitating sludge (I) is back to low-oxygen aeration activated sludge tank;
The hyperoxia aerating waste water that step (3) is obtained passes into second pond (II), through mud-water separation, obtained aerobic biochemical water outlet (II) is become reconciled oxygen precipitation mud (II), and aerobic precipitating sludge (II) is back to low-oxygen aeration activated sludge tank;
The reflux ratio of aerobic precipitating sludge (I) is 120%; The reflux ratio of aerobic precipitating sludge (II) is 200%;
(5) by after aerobic biochemical water outlet (I) obtained for step (4) and aerobic bio-chemical effluent (II) mixing, anaerobic ammonia oxidizing bacteria process in anaerobic reation pool, hydraulic detention time is 36h, ultrafiltration is carried out again, obtained processed waste water through immersion ultra-filtration technique.
Also comprise and remaining aerobic precipitating sludge (I) after air supporting mud obtained to precipitating sludge obtained for step (1), step (2), step (4) backflow is become reconciled oxygen precipitation mud (II) after dehydration, dehydration filtrate passes into equalizing tank.
According to this coal chemical industrial waste water of art breading that embodiment 1 in Chinese patent literature CN102633359A (application number 201210119771.3) is recorded, treatment effect is as shown in table 1.
As shown in table 1, the waste water quality after testing after the present embodiment process is: COD cr34mg/L, ammonia nitrogen 0.26mg/L, total nitrogen 3.6mg/L, SS can't check, and obvious processing effect is better than Chinese patent literature CN102633359A technique.
Adopt the oxygen depletion amount of air flow quantity metering method check processing technique, after testing, the present embodiment is when obvious processing effect is better than Chinese patent literature CN102633359A technique, oxygen depletion amount comparatively Chinese patent literature CN102633359A technique reduces 30% ~ 40%, and energy-saving effect is remarkable.
Table 1
Embodiment 2
Shandong produces the waste water of alcohol hydrocarbon esters product coal chemical industry enterprises, and index is: COD cr467mg/L, ammonia nitrogen 216mg/L, total nitrogen 264mg/L, SS 237mg/L.
Following treatment process is adopted to process above-mentioned coal chemical industrial waste water:
(1) being passed into by the coal chemical industrial waste water in equalizing tank in coagulative precipitation tank and to add polymerize aluminum chloride and anionic polyacrylamide, the add-on of polymerize aluminum chloride is 150mg/L, and the add-on of anionic polyacrylamide is 1mg/L; Through flocculating settling 5h, obtained coagulating sedimentation waste water and precipitating sludge;
(2) the coagulating sedimentation waste water that step (1) is obtained is passed in air floatation machine, polymerize aluminum chloride and anionic polyacrylamide is added in air floatation machine, the add-on of polymerize aluminum chloride is 50mg/L, the add-on of anionic polyacrylamide is 1.5mg/L, through flocculating settling 6h, obtained air supporting waste water and air supporting mud;
(3) ratio of air supporting waste water obtained for step (2) 1:1.5 is by volume passed into low-oxygen aeration activated sludge tank respectively and hyperoxia aerating activated sludge pond processes, obtained COD crthe low-oxygen aeration waste water of≤50mg/L and hyperoxia aerating waste water;
Described low-oxygen aeration activated sludge tank and hyperoxia aerating activated sludge pond are oxidation ditch formula structure, by the oxygen supply of blowing jet aerating system;
Described low-oxygen aeration activated sludge tank treatment condition are: be under the condition of 0.5mg/L, sludge concentration 3000mg/L at dissolved oxygen, hydraulic retention 24h;
The mud of described low-oxygen aeration activated sludge tank takes from common municipal sewage plant aeration tank.
Described hyperoxia aerating activated sludge pond treatment condition are: be under the condition of 3.0mg/L, sludge concentration 3500mg/L at dissolved oxygen, hydraulic retention 24;
The mud in described hyperoxia aerating activated sludge pond is at Initial stage of culture inoculation nitrifier BioRemove 5805.
(4) the low-oxygen aeration waste water that step (3) is obtained is passed into second pond (I), through mud-water separation, obtained aerobic biochemical water outlet (I) is become reconciled oxygen precipitation mud (I), and aerobic precipitating sludge (I) is back to low-oxygen aeration activated sludge tank;
The hyperoxia aerating waste water that step (3) is obtained passes into second pond (II), through mud-water separation, obtained aerobic biochemical water outlet (II) is become reconciled oxygen precipitation mud (II), and aerobic precipitating sludge (II) is back to low-oxygen aeration activated sludge tank;
The reflux ratio of aerobic precipitating sludge (I) is 80%; The reflux ratio of aerobic precipitating sludge (II) is 150%;
(5) by after aerobic biochemical water outlet (I) obtained for step (4) and aerobic bio-chemical effluent (II) mixing, anaerobic ammonia oxidizing bacteria process in anaerobic reation pool, hydraulic detention time is 34h, ultrafiltration is carried out again, obtained processed waste water through immersion ultra-filtration technique.
Also comprise and remaining aerobic precipitating sludge (I) after air supporting mud obtained to precipitating sludge obtained for step (1), step (2), step (4) backflow is become reconciled oxygen precipitation mud (II) after dehydration, dehydration filtrate passes into equalizing tank.
According to this coal chemical industrial waste water of art breading that embodiment 1 in Chinese patent literature CN102633359A (application number 201210119771.3) is recorded, treatment effect is as shown in table 2.
As shown in table 2, the waste water quality after testing after the present embodiment process is: COD cr42mg/L, ammonia nitrogen 0.45mg/L, total nitrogen 5.8mg/L, SS can't check, and obvious processing effect is better than Chinese patent literature CN102633359A technique.
Adopt the oxygen depletion amount of air flow quantity metering method check processing technique, after testing, the present embodiment is when obvious processing effect is better than Chinese patent literature CN102633359A technique, oxygen depletion amount comparatively Chinese patent literature CN102633359A technique reduces 30% ~ 40%, and energy-saving effect is remarkable.
Table 2
Embodiment 3
The coal chemical industry enterprises waste water of Shandong production coking, index is: COD cr3632mg/L, ammonia nitrogen 469mg/L, total nitrogen 657mg/L, SS 461mg/L.
Following treatment process is adopted to process above-mentioned coal chemical industrial waste water:
(1) being passed into by the coal chemical industrial waste water in equalizing tank in coagulative precipitation tank and to add polymerize aluminum chloride and anionic polyacrylamide, the add-on of polymerize aluminum chloride is 125mg/L, and the add-on of anionic polyacrylamide is 1.25mg/L; Through flocculating settling 4.5h, obtained coagulating sedimentation waste water and precipitating sludge;
(2) the coagulating sedimentation waste water that step (1) is obtained is passed in air floatation machine, polymerize aluminum chloride and anionic polyacrylamide is added in air floatation machine, the add-on of polymerize aluminum chloride is 75mg/L, the add-on of anionic polyacrylamide is 1.25mg/L, through flocculating settling 5.5h, obtained air supporting waste water and air supporting mud;
(3) ratio of air supporting waste water obtained for step (2) 1:1.4 is by volume passed into low-oxygen aeration activated sludge tank respectively and hyperoxia aerating activated sludge pond processes, obtained COD crthe low-oxygen aeration waste water of≤50mg/L and hyperoxia aerating waste water;
Described low-oxygen aeration activated sludge tank and hyperoxia aerating activated sludge pond are oxidation ditch formula structure, by the oxygen supply of blowing jet aerating system;
Described low-oxygen aeration activated sludge tank treatment condition are: be under the condition of 0.65mg/L, sludge concentration 3500mg/L at dissolved oxygen, hydraulic retention 30h;
The mud of described low-oxygen aeration activated sludge tank takes from municipal sewage plant aeration tank.
Described hyperoxia aerating activated sludge pond treatment condition are: be under the condition of 3.5mg/L, sludge concentration 4000mg/L at dissolved oxygen, hydraulic retention 30h;
The mud in described hyperoxia aerating activated sludge pond is at Initial stage of culture inoculation nitrifier BioRemove 5805.
(4) the low-oxygen aeration waste water that step (3) is obtained is passed into second pond (I), through mud-water separation, obtained aerobic biochemical water outlet (I) is become reconciled oxygen precipitation mud (I), and aerobic precipitating sludge (I) is back to low-oxygen aeration activated sludge tank;
The hyperoxia aerating waste water that step (3) is obtained passes into second pond (II), through mud-water separation, obtained aerobic biochemical water outlet (II) is become reconciled oxygen precipitation mud (II), and aerobic precipitating sludge (II) is back to low-oxygen aeration activated sludge tank;
The reflux ratio of aerobic precipitating sludge (I) is 100%; The reflux ratio of aerobic precipitating sludge (II) is 170%;
(5) by after aerobic biochemical water outlet (I) obtained for step (4) and aerobic bio-chemical effluent (II) mixing, anaerobic ammonia oxidizing bacteria process in anaerobic reation pool, hydraulic detention time is 35h, ultrafiltration is carried out again, obtained processed waste water through immersion ultra-filtration technique.
Also comprise and remaining aerobic precipitating sludge (I) after air supporting mud obtained to precipitating sludge obtained for step (1), step (2), step (4) backflow is become reconciled oxygen precipitation mud (II) after dehydration, dehydration filtrate passes into equalizing tank.
According to this coal chemical industrial waste water of art breading that embodiment in Chinese patent literature CN102249490A (application number 201110158915.1) is recorded, treatment effect is as shown in table 3.
As shown in table 3, the waste water quality after testing after the present embodiment process is: COD cr146mg/L, ammonia nitrogen 4.6mg/L, total nitrogen 22.5mg/L, SS can't check, and obvious processing effect is better than Chinese patent literature CN102249490A technique.
Adopt the oxygen depletion amount of air flow quantity metering method check processing technique, after testing, the present embodiment is when obvious processing effect is better than Chinese patent literature CN102249490A technique, oxygen depletion amount comparatively Chinese patent literature CN102249490A technique reduces 30% ~ 40%, and energy-saving effect is remarkable.
Table 3

Claims (10)

1. the energy-efficient treatment process of coal chemical industrial waste water, is characterized in that, comprise the steps:
(1) coal chemical industrial waste water in equalizing tank to be passed in coagulative precipitation tank and to add flocculation agent, through flocculating settling, obtained coagulating sedimentation waste water and precipitating sludge;
(2) the coagulating sedimentation waste water that step (1) is obtained is passed in air floatation machine, in air floatation machine, add flocculation agent, through flocculating settling, obtained air supporting waste water and air supporting mud;
(3) by air supporting waste water 1:(1.2 ~ 1.5 by volume obtained for step (2)) ratio pass into low-oxygen aeration activated sludge tank respectively and hyperoxia aerating activated sludge pond processes, obtained low-oxygen aeration waste water and hyperoxia aerating waste water;
Described low-oxygen aeration activated sludge tank treatment condition are: be under the condition of 0.5 ~ 0.8mg/L, sludge concentration 3000 ~ 4000mg/L at dissolved oxygen, hydraulic retention 24 ~ 36h;
Described hyperoxia aerating activated sludge pond treatment condition are: be under the condition of 3.0 ~ 4.0mg/L, sludge concentration 3500 ~ 4500mg/L at dissolved oxygen, hydraulic retention 24 ~ 36h;
(4) the low-oxygen aeration waste water that step (3) is obtained is passed into second pond (I), through mud-water separation, obtained aerobic biochemical water outlet (I) is become reconciled oxygen precipitation mud (I), and aerobic precipitating sludge (I) is back to low-oxygen aeration activated sludge tank;
The hyperoxia aerating waste water that step (3) is obtained passes into second pond (II), through mud-water separation, obtained aerobic biochemical water outlet (II) is become reconciled oxygen precipitation mud (II), and aerobic precipitating sludge (II) is back to low-oxygen aeration activated sludge tank;
(5) by after aerobic biochemical water outlet (I) obtained for step (4) and aerobic bio-chemical effluent (II) mixing, after anaerobic reation pool process, then through ultrafiltration, obtained processed waste water.
2. technique as claimed in claim 1, it is characterized in that, in described step (1), flocculation agent is polymerize aluminum chloride and anionic polyacrylamide, the add-on of polymerize aluminum chloride is 100 ~ 150mg/L, and the add-on of anionic polyacrylamide is 1 ~ 1.5mg/L; The flocculating settling time is 4 ~ 5h.
3. technique as claimed in claim 1, it is characterized in that, in described step (2), flocculation agent is polymerize aluminum chloride and anionic polyacrylamide, the add-on of polymerize aluminum chloride is 50 ~ 100mg/L, and the add-on of anionic polyacrylamide is 1 ~ 1.5mg/L; The flocculating settling time is 5 ~ 6h.
4. technique as claimed in claim 1, is characterized in that, in described step (3), the mud in hyperoxia aerating activated sludge pond is at Initial stage of culture inoculation nitrifier BioRemove5805, and Novozymes Company of nitrifier BioRemove5805 Denmark is on sale.
5. technique as claimed in claim 1, it is characterized in that, in described step (3), described low-oxygen aeration activated sludge tank and hyperoxia aerating activated sludge pond are oxidation ditch formula structure, by the oxygen supply of blowing jet aerating system.
6. technique as claimed in claim 1, is characterized in that, in described step (3), and the COD of low-oxygen aeration waste water and hyperoxia aerating waste water cr≤ 50mg/L.
7. technique as claimed in claim 1, it is characterized in that, in described step (4), the reflux ratio of aerobic precipitating sludge (I) is 80 ~ 120%; The reflux ratio of aerobic precipitating sludge (II) is 150 ~ 200%.
8. technique as claimed in claim 1, it is characterized in that, in described step (5), the mud in described anaerobic reation pool is anaerobic ammonia oxidizing bacteria, and hydraulic detention time is 34 ~ 36h.
9. technique as claimed in claim 1, is characterized in that, in described step (5), ultrafiltration carries out ultrafiltration for adopting immersion ultra-filtration technique.
10. technique as claimed in claim 1, it is characterized in that, also comprise and remaining aerobic precipitating sludge (I) after air supporting mud obtained to precipitating sludge obtained for step (1), step (2), step (4) backflow is become reconciled oxygen precipitation mud (II) after dehydration, dehydration filtrate passes into equalizing tank.
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CN110104907A (en) * 2019-06-11 2019-08-09 武汉深能环保新沟垃圾发电有限公司 A kind of landfill leachate oil removing system and method

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