CN102730896A - Salt-containing sewage processing method - Google Patents
Salt-containing sewage processing method Download PDFInfo
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- CN102730896A CN102730896A CN2011100819993A CN201110081999A CN102730896A CN 102730896 A CN102730896 A CN 102730896A CN 2011100819993 A CN2011100819993 A CN 2011100819993A CN 201110081999 A CN201110081999 A CN 201110081999A CN 102730896 A CN102730896 A CN 102730896A
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Abstract
The invention relates to an industrial sewage processing method, specifically to a salt-containing sewage processing method. The technical scheme provided by the invention is as follows: the salt-containing processing method comprises the following steps of: (1) preaeration; (2) coagulation sedimentation processing; (3) biological denitrogenation processing; (4) sedimentation separation processing; (5) flocculation filtration processing; and (6) comprehensive adjustment processing. The invention has beneficial effects as follows: the processing method has advantages of less investment, low operation cost and stable and reliable operation effect, can meet increasingly severe environmental protection requirements, can be widely applied in petrochemical (especially alkene, chlor alkali and the like) industrial wastewater processing, and simultaneously can be suitable for sewage processing in municipal, chemical fiber and leather making industries and the like.
Description
Technical field
The present invention relates to a kind of treatment process of industrial sewage, specifically, relate to a kind of treatment process of saline sewage.
Background technology
All can produce a large amount of saline sewages in industries such as oil production, petrochemical complex, printing and dyeing, pharmacy; Salts contg can produce the biology in the Sewage treatment systems and poison, restraining effect; And the destruction sludge settling property, thereby cause conventional activated sludge process to be difficult to realize effective processing of saline sewage.Processing efficiency was low when conventional activated sludge process was handled saline sewage, and anti-salinity impact capacity is poor.At present; Saline sewage is handled the general method of inoculation halophile that adopts and is realized organic effective processing; But the inoculation halophilic bacterium receives the restriction of condition; And right salt bacterium also can receive the competition effect of other mikrobe in the Sewage treatment systems, causes this method processing cost height, treatment effect to be difficult to long-term assurance.The treatment process that is adopted at present adopts sequencing batch reactor mostly, and sequencing batch reactor still is in the laboratory study stage, is not widely used in industrial circle as yet.
Patent CN100443426C discloses the method for wastewater treatment of a kind of saliferous, high organic content.The method that this invention provides has the organic loading of processing height, removes characteristics such as deferrization efficient is high, floor space is little; Accessible former water CODcr concentration is 10000～20000mg/L; Calcium contents is 500～6000mg/L, and iron level is 0～500mg/L, and the waste water COD cr concentration after the processing can be reduced to below the 800mg/L; Calcium contents is reduced to below the 200mg/L, and iron level is reduced to below the 10mg/L.But this method deliming expense is high, and processed waste water COD is difficult to be less than the index of 60mg/L.
Patent CN101054232A discloses and a kind ofly can realize the efficient treatment technology of high slat-containing wastewater.It is through forming aerobic particle mud and adopting certain startup operation method and sludge acclimatization mode in sequencing batch reactor; Under not adding the halophilic bacterium condition, make mud realization gathering growth and formation compound microecological in the reactor drum, thereby realize the efficient processing of high slat-containing wastewater and the anti-salinity impact capacity of improvement system.The sequencing batch reactor that adopts in this patent still is in the laboratory study stage, is not widely used in industrial circle as yet.
For saline sewage, adopt Wastewater Treated by Activated Sludge Process at present mostly, because processing efficiency is not high, the COD clearance is about 70% usually, and the not impact of salt tolerant, water outlet is difficult to reach emission standard.Because salinity suppresses the growth of nitrifier, ammonia nitrogen is difficult to produce nitration reaction under saline environment.
Summary of the invention
It is high that the present invention aims to provide a kind of purification efficiency, and the COD clearance is high, and last effect is stable, and working cost is low, is convenient to the treatment process of the saline sewage of Operation and Maintenance.
Technical scheme of the present invention is: a kind of treatment process of saline sewage may further comprise the steps:
(1) pre-exposure is handled: saline sewage gets into the pre-exposure pond, after fully stirring, through mechanical fine fack the organic pollutant in the saline sewage is fully separated with inorganics, removes the part organic pollutant, and water outlet is promoted to the coagulating sedimentation processing unit; Stir the device that uses and be air stirring pipe; This step COD clearance reaches more than 15%.
(2) coagulating sedimentation is handled: dosing coagulant, and the stirring reaction postprecipitation makes solid-liquid separation, removes part suspended substance and mud in the sewage, and supernatant is from flowing to the biological denitrificaion processing unit.
The device that coagulating sedimentation uses in this step is a reaction tank and a heavy pond, and dosing coagulant in reaction tank precipitates from flowing to a heavy pond behind the stirring reaction.When a heavy pond can not be used, can launch preliminary sedimentation tank and carry out the coagulating sedimentation processing, in preliminary sedimentation tank, directly precipitate behind the dosing coagulant stirring reaction.
Coagulating agent described in this step adopts PAFC, and dosage is 10～30mg/L; Consider that from economy, reasonableness angle consider simultaneously to remove SS and COD simultaneously, best dosage is 10mg/L.
(3) biological denitrificaion is handled: step (2) water outlet is through modification A pond, 0 pond, refluxes and internal reflux carries out biological denitrificaion through mud, reach ammonia nitrogen nitrated with the purpose of removing COD, water outlet entering precipitate and separate processing unit; This step ammonia nitrogen removal frank reaches more than 98%, and the clearance of COD reaches more than 85%.
The main technologic parameters in modification A pond is in this step: hydraulic detention time 11h, mud 50～100d in age, MLSS6000～8000mg/L; MLVSS4000～6000mg/L; Nitrification liquid reflux ratio 200～300%, return sludge ratio 50～100%, volumetric loading 1.10KgCOD/ (m
3D), sludge loading is controlled at 0.20～0.25KgCOD/ (KgVSSd), and the best is 0.22KgCOD/ (KgVSSd); The main technologic parameters in 0 pond is: hydraulic detention time 22.5h, mud 80～100d in age, MLSS6000～8000mg/L; MLVSS4000～6000mg/L; Nitrification liquid reflux ratio 200～300%, return sludge ratio 50～100%, volumetric loading 0.49Kg (COD+NOD)/(m
3D), sludge loading 0.10Kg (COD+NOD)/(KgVSSd).
(4) precipitate and separate is handled: after precipitate and separate, mud is back to the modification A pond of biological denitrificaion processing unit in second pond, and sewage is promoted to the flocculation filtration processing unit.
It is spoke stream that second pond described in this step is provided with form, useful volume 3800m
3, surface load 0.71m
3/ (m
2H), solid flux 170KgVSS/ (m
2D), the mud reflux type is that gas is carried.
(5) flocculation filtration is handled: add flocculation agent, filter through the drift sand strainer reaction back, holds back the SS in the sewage, and in company with removing the COD that part is difficult to degrade, filtered sewage gets into the comprehensive adjustment processing unit; This step COD clearance is about 15%.
The main technologic parameters of the device of running sand filtration described in this step is: hydraulic detention time 1.5～5.5h, the best is 2.0～4.0h, hydraulic load 0.5～1.5m
3/ (m
2H), the best is 0.8～1.2m
3/ (m
2H), organic loading 0.5～1.0KgCOD/ (m
3D), the best is 0.75～0.85KgCOD/ (m
3D), co-substrate dosage 8～15mg/L, the best is 10～12mg/L, and GWR (oxygen) 1.0～3.0: 1, the best are 1.0～1.5: 1, and the filler type is particle diameter 3～6mm light ceramic.
Said running sand filtration device adopts silica sand to load, and loading height is 2.5～4.5m, and best loading height is 2.8m.
(6) comprehensive adjustment is handled: be used to make the sewage mixing and buffering, qualified discharge.
Beneficial effect of the present invention is: invest little; Working cost is low; Last effect is reliable and stable; Can satisfy the environmental protection demand of increasingly stringent, and can comparatively be widely used in petrochemical industry (especially alkene, chlor-alkali etc.) Industrial Wastewater Treatment, also can be fit to the processing of industry sewage such as municipal administration, chemical fibre, process hides simultaneously.
Description of drawings
Fig. 1 is a schema of the present invention.
Embodiment
Embodiment 1:
Saltiness (TDS) is 1.0% saline sewage (COD624mg/L, NH
3-N25.6mg/L) getting into treatment scheme shown in Figure 1, the main technologic parameters of each processing unit is: pre-exposure pond reaction settling time 1h; The one heavy pond residence time was 3.8 hours, surface load 1.43m
3/ (m
2H); Modification A tank waterpower residence time 11h, mud 50～80d in age, MLSS6000～8000mg/L, MLVSS4000～6000mg/L, nitrification liquid reflux ratio 200～300%, return sludge ratio 50～100%; 0 tank waterpower residence time 22.5h, mud 80～100d in age, MLSS6000～8000mg/L, MLVSS4000～6000mg/L, nitrification liquid reflux ratio 280%, return sludge ratio 80%.Running sand filtration device effluent quality parameter is: COD46.7mg/L, NH
3-N＜0.2mg/L, suspended substance 5.0mg/L.
Embodiment 2:
Saltiness (TDS) is 0.8% saline sewage (COD587mg/L, NH
3-N31.2mg/L) getting into treatment scheme shown in Figure 1, the main technologic parameters of each processing unit is: pre-exposure pond reaction settling time 1h; The one heavy pond residence time was 3.8 hours, surface load 1.43m
3/ (m
2.h); Modification A tank waterpower residence time 11h, mud 60～80d in age, MLSS7000～8000mg/L, MLVSS5000～6000mg/L, nitrification liquid reflux ratio 260%, return sludge ratio 75%; O tank waterpower residence time 22.5h, mud 80～90d in age, MLSS7000～8000mg/L, MLVSS5000～6000mg/L, nitrification liquid reflux ratio 270%, return sludge ratio 75%; Running sand filtration device effluent quality parameter is: COD52.1mg/L, NH
3-N＜0.2mg/L, suspended substance 4.5mg/L.
Embodiment 3:
Saltiness (TDS) is 0.8% saline sewage (COD526mg/L, NH
3-N 28.5mg/L) get into treatment scheme shown in Figure 1, the main technologic parameters of each processing unit is: pre-exposure pond reaction settling time 1h; The one heavy pond residence time was 3.8 hours, surface load 1.43m
3/ m
2/ h; Modification A tank waterpower residence time 11h, mud 60～80d in age, MLSS7000～8000mg/L, MLVSS5000～6000mg/L; Nitrification liquid reflux ratio 240%, return sludge ratio 70～80%, O tank waterpower residence time 22.5h; Mud 60-85d in age, MLSS7000～8000mg/L, MLVSS5000～6000mg/L; Nitrification liquid reflux ratio 240～280%, return sludge ratio 65～85%, the running sand filtration device: packing height is 4.2 meters; The COD clearance is 15%, and running sand filtration device effluent quality parameter is: COD38.9mg/L (less than 50mg/L), NH
3-N＜0.2mg/L, suspended substance＜4.5mg/L.
Claims (13)
1. the treatment process of a saline sewage is characterized in that, may further comprise the steps:
(1) pre-exposure is handled: saline sewage gets into the pre-exposure pond, after fully stirring, through mechanical fine fack the organic pollutant in the saline sewage is fully separated with inorganics, removes the part organic pollutant, and water outlet is promoted to the coagulating sedimentation processing unit;
(2) coagulating sedimentation is handled: dosing coagulant, and the stirring reaction postprecipitation makes solid-liquid separation, removes part suspended substance and mud in the sewage, and supernatant is from flowing to the biological denitrificaion processing unit;
(3) biological denitrificaion is handled: step (2) water outlet is through modification A pond, 0 pond, refluxes and internal reflux carries out biological denitrificaion through mud, reach ammonia nitrogen nitrated with the purpose of removing COD, water outlet entering precipitate and separate processing unit;
(4) precipitate and separate is handled: after precipitate and separate, mud is back to the modification A pond of biological denitrificaion processing unit in second pond, and sewage is promoted to the flocculation filtration processing unit;
(5) flocculation filtration is handled: add flocculation agent, filter through the drift sand strainer reaction back, holds back the SS in the sewage, and in company with removing the COD that part is difficult to degrade, filtered sewage gets into the comprehensive adjustment processing unit;
(6) comprehensive adjustment is handled: be used to make the sewage mixing and buffering, qualified discharge.
2. the treatment process of saline sewage according to claim 1 is characterized in that, in said step (1) the pre-exposure treatment step, stirs the device that uses and is air stirring pipe.
3. the treatment process of saline sewage according to claim 1 is characterized in that, in said step (2) the coagulating sedimentation treatment step, the device of coagulating sedimentation is a preliminary sedimentation tank, dosing coagulant stirring reaction postprecipitation in preliminary sedimentation tank.
4. the treatment process of saline sewage according to claim 1; It is characterized in that in said step (2) the coagulating sedimentation treatment step, the device of coagulating sedimentation is a reaction tank and a heavy pond; Dosing coagulant in reaction tank precipitates from flowing to a heavy pond behind the stirring reaction.
5. the treatment process of saline sewage according to claim 1 is characterized in that, in said step (2) the coagulating sedimentation treatment step, said coagulating agent adopts PAFC, and dosage is 10～30mg/L.
6. the treatment process of saline sewage according to claim 4 is characterized in that, said coagulant charging quantity is 10mg/L.
7. the treatment process of saline sewage according to claim 1 is characterized in that, in said step (3) the biological denitrificaion treatment step; The main technologic parameters in modification A pond is: hydraulic detention time 11h, mud 50～100d in age, MLSS6000～8000mg/L; MLVSS4000～6000mg/L; Nitrification liquid reflux ratio 200～300%, return sludge ratio 50～100%, volumetric loading 1.10KgCOD/ (m
3D), sludge loading is controlled at 0.20～0.25KgCOD/ (KgVSSd); The main technologic parameters in 0 pond is: hydraulic detention time 22.5h, mud 80～100d in age, MLSS6000～8000mg/L; MLVSS4000～6000mg/L; Nitrification liquid reflux ratio 200～300%, return sludge ratio 50～100%, volumetric loading 0.49Kg (COD+NOD)/(m
3D), sludge loading 0.10Kg (COD+NOD)/(KgVSSd).
8. the treatment process of saline sewage according to claim 5 is characterized in that, the sludge loading in said modification A pond is 0.22KgCOD/ (KgVSSd).
9. the treatment process of saline sewage according to claim 1 is characterized in that, in said step (4) the precipitate and separate treatment step, it is spoke stream that said second pond is provided with form, useful volume 3800m
3, surface load 0.71m
3/ (m
2H), solid flux 170KgVSS/ (m
2D), the mud reflux type is that gas is carried.
10. the treatment process of saline sewage according to claim 1 is characterized in that, in said step (5) the flocculation filtration treatment step, the main technologic parameters of said running sand filtration device is: hydraulic detention time 1.5～5.5h, hydraulic load 0.5～1.5m
3/ (m
2H), organic loading 0.50～1.0KgCOD/ (m
3D), co-substrate dosage 8～15mg/L, GWR (oxygen) 1.0～3.0: 1, filler type are particle diameter 3～6mm light ceramic.
11. the treatment process of saline sewage according to claim 10 is characterized in that, the main technologic parameters of said running sand filtration device is: hydraulic detention time 2.0～4h, hydraulic load 0.8～1.2m
3/ (m
2H), organic loading 0.75～0.85KgCOD/ (m
3D), co-substrate dosage 10～12mg/L, GWR (oxygen) 1.0～1.5: 1, filler type are particle diameter 3～6mm light ceramic.
12. the treatment process of saline sewage according to claim 10 is characterized in that, said running sand filtration device adopts silica sand to load, and loading height is 2.5～4.5m.
13. the treatment process of saline sewage according to claim 11 is characterized in that, the loading height of said running sand filtration device is 2.8m.
Priority Applications (1)
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|---|---|---|---|
| CN2011100819993A CN102730896A (en) | 2011-04-01 | 2011-04-01 | Salt-containing sewage processing method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100819993A CN102730896A (en) | 2011-04-01 | 2011-04-01 | Salt-containing sewage processing method |
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| Publication Number | Publication Date |
|---|---|
| CN102730896A true CN102730896A (en) | 2012-10-17 |
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ID=46987300
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104276729A (en) * | 2014-10-16 | 2015-01-14 | 滁州友林科技发展有限公司 | High-oil-content sewage treatment technique |
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| CN101607777A (en) * | 2009-07-30 | 2009-12-23 | 达斯玛环境科技（北京）有限公司 | A kind of Lurgi furnace coal gasification wastewater treatment and reuse technology |
| CN101700948A (en) * | 2009-11-20 | 2010-05-05 | 上海应用技术学院 | Wastewater treatment technology for textile dyeing and finishing industry |
| KR100960015B1 (en) * | 2009-08-28 | 2010-05-28 | 주식회사 부강테크 | Waste water treatment apparatus for processing early rain effectively and the method thereof |
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2011
- 2011-04-01 CN CN2011100819993A patent/CN102730896A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101525202A (en) * | 2009-04-14 | 2009-09-09 | 东华大学 | Advanced dyeing wastewater treatment and reclaimed water reuse system and method thereof |
| CN101607777A (en) * | 2009-07-30 | 2009-12-23 | 达斯玛环境科技（北京）有限公司 | A kind of Lurgi furnace coal gasification wastewater treatment and reuse technology |
| KR100960015B1 (en) * | 2009-08-28 | 2010-05-28 | 주식회사 부강테크 | Waste water treatment apparatus for processing early rain effectively and the method thereof |
| CN101700948A (en) * | 2009-11-20 | 2010-05-05 | 上海应用技术学院 | Wastewater treatment technology for textile dyeing and finishing industry |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104276729A (en) * | 2014-10-16 | 2015-01-14 | 滁州友林科技发展有限公司 | High-oil-content sewage treatment technique |
| CN104276729B (en) * | 2014-10-16 | 2016-04-13 | 滁州友林科技发展有限公司 | The sewage treatment process that a kind of oleaginousness is high |
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Application publication date: 20121017 |