CN104724888A - Decarbonization and total nitrogen removal treating process for semi-coking wastewater - Google Patents
Decarbonization and total nitrogen removal treating process for semi-coking wastewater Download PDFInfo
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- CN104724888A CN104724888A CN201510129478.9A CN201510129478A CN104724888A CN 104724888 A CN104724888 A CN 104724888A CN 201510129478 A CN201510129478 A CN 201510129478A CN 104724888 A CN104724888 A CN 104724888A
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Abstract
The invention discloses a decarbonization and total nitrogen removal treating process for semi-coking wastewater. The process sequentially comprises a pretreatment system, a biochemical treatment system and a deep treatment system, wherein the pretreatment system comprises an oil separation tank and cavitation air flotation tanks of two stages; the biochemical treatment system at least comprises an aerobic pool, a facultative tank and a precipitation tank; the deep treatment system at least comprises a photocatalytic ozone oxidation reaction tower, and ozone enters water through a microporous aeration disc from the lower end of the photocatalytic ozone oxidation reaction tower; a gas collecting pipe is arranged at the top of the photocatalytic ozone oxidation reaction tower and is used for collecting residual ozone overflowing from a water surface and then leading the collected residual ozone into a first-stage cavitation air flotation tank. The residual ozone is introduced to an air flotation section of the first-stage cavitation air flotation tank, so that the ozone is recycled, the deoiling effect of the air flotation section is improved, meanwhile, the removal amount of harmful substances is increased, and the load of treatment of a biochemical end is reduced. Aiming at the semi-coking wastewater, the process is good in treatment effect, strong in adaptability and convenient in operation and is stable and reliable.
Description
Technical field
The present invention relates to industrial waste water treatment, particularly relate to a kind of blue charcoal waste water decarburization removing total nitrogen treatment process.
Background technology
Blue charcoal also known as semicoke, it be with low-temperature pyrolysis (600 ~ 800 DEG C) pyrolysis in the processes such as long-flame coal, non-caking coal and weakly caking coal obtain compared with the solid carbonaceous product of low volatile, its waste water quality composition is similar to coking chemical waste water.In coke production, pyrolysis temperature is about 1000 DEG C, and in the production of blue charcoal, pyrolysis temperature is low.Therefore containing a large amount of not by low molecule pollutent in high temperature oxidation in blue charcoal waste water, its concentration exceeds about 10 times than coking chemical waste water.Blue charcoal waste water, mainly containing high-enriched organics and inorganics, is the pollutent that toxicity is very strong, is generally difficult to treatment for reuse.It is mainly containing coal tar oily substance, as methyl alcohol, ethanol, formic acid, acetic acid, toluene, benzene, phenol type substances, naphthalene, anthracene, quinone etc., and a large amount of loop chain organism, nitrine class mineral compound and ammonia nitrogens etc., wherein COD is up to 30000-40000mg/L, and ammonia nitrogen is up to 2500-3000mg/L; Inorganic pollutant, mainly based on ammonium salt, also contains the objectionable impuritiess such as sulfide, thiocyanide, prussiate, if unprocessed direct discharge will cause severe contamination to water surrounding.At present, blue charcoal waste water has become one of used water difficult to degradate of generally acknowledging both at home and abroad.
Existing blue charcoal scale wastewater treatment system many employings Physical, chemical method and biological process: its main process method has absorption method, flue gas treatment method, activated sludge process, burning method, catalyzed oxidation-biochemical process, ammonia still process dephenolize-SBR method and emulsion liquid membrane etc., their Problems existing: cost of investment is high, processing cost is high, suitability is not strong, difficult treatment or generation secondary pollution problems, as high in absorption method processing cost, absorption regeneration difficulty, inapplicable high concentration wastewater treatment, flue gas method requires that in waste water, ammonia content must balance with ammonia amount needed for stack gas, use restricted, burning method process investment is large, and require high to water quality treatment, suitability is not strong, catalytic oxidation will carry out under high-temperature and high-pressure conditions, and processing cost is high, scale of investment and working cost large, ammonia still process dephenolize-SBR method needs to use organic solvent dephenolize, secondary pollution can be produced, and affect NH_3-N treating efficiency after first carrying out phenol removal, add the difficulty of subsequent disposal, these all may make water outlet can not reach table 2 directly emission standard in " coking chemistry emission of industrial pollutants standard " GB16171-2012.
Summary of the invention
Proposition of the present invention is to overcome above treatment process Problems existing, proposes that a kind for the treatment of effect for blue charcoal waste water is good, suitability is strong, the treatment process of reliable and stable and easy to operate, process working cost is lower decarburization removing total nitrogen.
To achieve these goals, the technical solution used in the present invention is:
A kind of blue charcoal waste water decarburization removing total nitrogen treatment process, comprises pretreatment system, biochemical treatment system, advanced treatment system successively;
Described pretreatment system comprises an oil trap and secondary cavitation air flotation pond; Described biochemical treatment system at least comprises an Aerobic Pond, oxygen compatibility pool, a settling tank; Described advanced treatment system at least comprises a photocatalytic ozonation reaction tower, and ozone enters water body from photocatalytic ozonation reaction tower lower end by microporous aeration disc;
It is characterized in that: photocatalytic ozonation reaction tower top is provided with effuser, cause in described first step cavitation air flotation pond after collecting the residual ozone overflowed from the water surface.
Further, be provided with loose gas impeller in described cavitation air flotation pond, and add emulsion splitter.
Described advanced treatment system also comprises the advanced treatment system of inner circulating aerating biological filtering tank, BAF, more medium filter, UF/RO membranous system, finally reaches the function of reuse.
Preprocessing process of the present invention is that first blue charcoal waste water enter oil trap, remove most heavy oil and part light oil, connect after water outlet enters equalizing tank homogenization treatment and enter the process of secondary cavitation air flotation, by loose gas impeller, " microbubble " is distributed in sewage uniformly, add emulsion splitter simultaneously, remove most oil in water emulsion and oil slick and most of undissolved suspended matter, as added quaternary amine multipolymer, dosage about 20mg/L, obviously reduces (conventional P AC adds more than 100mg/L) than dosages such as traditional medicament PAC, scum silica frost generation is only 1/3 of PAC in addition, accessed residual ozone at the cavitation air flotation pond air supporting section ullage of the first step simultaneously, it is made to pass in water body with the form of microbubble, recycling ozone, ozone oxidation is very capable, it has been generally acknowledged that (under alkaline condition, ozone produces the intermediate products such as the very strong hydroxyl radical free radical of oxidisability after decomposing in water body to ozone by direct reaction (ozone carries out direct reaction with the organism in oxygen molecule form and water body) and indirect reaction, there is indirect oxidation reaction) two kinds of approach and many organism or functional group react, as C=C, C ≡ C, aromatic compound, heterogeneous ring compound, N=N, C=N,-OH,-SH,-NH
2,-CHO etc., also apolar substance can be changed into polar material, change macromolecule organic into low molecule organic matter, change organic for wetting ability micelle into inorganics that hydrophobicity easily condenses filtration, thus, air supporting section in first step cavitation air flotation pond introduces residual ozone, not only recycling ozone, and improve air supporting section deoiling effect, add the removal amount of objectionable impurities simultaneously, alleviate the processing load of biochemical end, reduce the running cost of system, the processing cost of rear end residual ozone when avoiding system cloud gray model, raising system pre-treatment efficiency, reduce the advantages such as the processing cost of biochemical system and advanced treatment system.Therefore, pretreatment stage petroleum-type, total oil removing rate reach respectively 93.3% and 90%(do not utilize residual ozone reach 85.3% and 76%); Have good removal effect to COD, clearance reaches more than 20% (the pretreatment stage COD clearance of unreferenced residual ozone is 11%), also has certain removal effect to volatile phenol, ammonia nitrogen and total nitrogen simultaneously.
Described inner circulating aerating biological filtering tank (RBAF) is arranged and water inlet aeration mode by the filter material layer in adjustment filter tank, realize the internal recycle of water inlet in filter tank, thus improving decomposition and the separating effect of BAF, the organism for bio-chemical effluent is effectively removed.Described photocatalytic ozonation bear decomposing organic matter be can be biochemical small-molecule substance and remove part COD, remove the function of prussiate and decolouring, and the unnecessary ozone in photocatalytic ozonation reaction tower guides to first step cavitation air flotation pond air supporting section ullage, as one of air supporting section source of the gas, recycling residual ozone removes part objectionable impurities, saving resource and cost.Photocatalytic ozonation water outlet flows through BAF, more medium filter, the process of UF/RO film again, table 3 directly emission standard in effluent quality reaches " coking chemistry emission of industrial pollutants standard " GB16171-2012.
Accompanying drawing explanation
Fig. 1 is embodiment of the present invention process flow sheet.
Fig. 2 is photocatalytic ozonation reaction unit schematic diagram.
Embodiment
See accompanying drawing.In Fig. 1, A is blue charcoal waste water; B is residual ozone; C is excess sludge; D is sludge reflux; E is mixed-liquor return; F is water outlet or reuse.
Blue charcoal waste water in this engineering from certain Lan Tan factory via the waste water after ammonia still process, dephenolize, oil removing pre-treatment, be made up of phenolic wastewater and oily(waste)water two portions (flooding quantity with 4:6), water-quality guideline is as shown in table 1, is 1m by the process design flooding quantity of Fig. 1
3the plant running of/h.Wherein in photocatalytic ozonation reaction tower, 51 is water inlet, and 53 is water outlet, and 52 is ozone entrance, and 23 is microporous aeration disc, and 22 is ultraviolet source, and 24 is effuser.Water enters photocatalysis and ozone reaction tower from water inlet 51, ozone enters water body by microporous aeration disc 23, react under ultraviolet catalytic, water after having reacted flows out from water outlet 53, and remaining ozone overflows the water surface, after effuser 24 is collected, cause first step cavitation air flotation pond air supporting section ullage.
The present embodiment overall process process is as follows.
1) pretreatment system:
Blue charcoal waste water enters oil trap, remove most heavy oil and part light oil, the process of secondary cavitation air flotation is entered after entering equalizing tank homogenization treatment, every grade adds quaternary amine multipolymer and is about 10mg/L, remove most oil in water emulsion and oil slick, remove most of undissolved suspended matter simultaneously, and utilize residual ozone as one of source of the gas in first step cavitation air flotation pond air supporting section, recycling ozone, oxide treatment moieties, reduce the objectionable impurities such as COD, ammonia nitrogen, volatile phenol in waste water, air supporting water outlet access biochemical system.With regard to the effect of water outlet after pre-treatment ozone introduced to air supporting section in following table 2 and utilize air source and be described (under the condition that other controling parameters are the same), the pre-treatment water outlet petroleum-type of recycling residual ozone, always oil removing rate reach respectively 93.3% and 90%(do not utilize residual ozone reach 85.3% and 76%); Have good removal effect to COD, clearance reaches more than 20% (the pretreatment stage COD clearance of unreferenced residual ozone is 11%), also has certain removal effect to volatile phenol, ammonia nitrogen and total nitrogen simultaneously.
2) biochemical system:
Pre-treatment water outlet enters sludge absorption bed bioreactor (PASAB), fully mix with excess sludge, simultaneously according to practical situation, add carrier and biological enzyme inducible factor, choosing mixture concentration is control different mixed liquid concentrations in 5000mg/L(PASAB pond, its effluent quality situation is as shown in table 3), hydraulic retention 60min, enter the first settling tank afterwards and realize mud-water separation, water outlet enters HLA+ first Aerobic Pond, multiple refluxing opening is set in the gallery of the first Aerobic Pond, reflux and its reflux ratio 60% and 40% in 2/3 gallery position of the first Aerobic Pond and end simultaneously, mud-water separation is carried out again through the second settling tank, after enter the further denitrification and decarburization of A/O system, the qualified discharge of the water outlet total nitrogen of safeguards system.Draw in this process of the test, biochemical stage water outlet COD is down to below 120mg/L, ammonia nitrogen < 0.5mg/L, total nitrogen < 20mg/L, volatile phenol < 0.2mg/L, petroleum-type < 1mg/L, colourity is down to less than 140 times; And only end backflow, water outlet total nitrogen near 40-60mg/L in, add advanced treatment load, also may cause final outflow water total nitrogen (in GB16171-2012, table 2 directly discharges) not up to standard.In whole biochemical treatment process, the second clarifier sludge is back to HLA pond, and the second clarifier sludge is back to anoxic pond; Simultaneously also according to water quality and system disposition spoil disposal, excess sludge enters PASAB reactor or sludge thickener.
3) advanced treatment:
Bio-chemical effluent is introduced into RBAF, filter material layer in adjustment filter tank is arranged and water inlet aeration mode, realize the internal recycle of water inlet in filter tank, thus improve decomposition and the separating effect of BAF, organism for bio-chemical effluent is effectively removed, afterwards through photocatalytic ozonation, macromolecular substance is degraded to material that intermediate state or small molecules can be biochemical, be conducive to the process of follow-up BAF, the colourity of water outlet is down to less than 15 times, after BAF process, water outlet is through more medium filter, the process of UF/RO film, final outflow water index is made to meet table 3 directly emission standard in " coking chemistry emission of industrial pollutants standard " GB16171-2012, simultaneously index of correlation to be better than in GB50335-2002 reuse water as the water quality standard of recirculated cooling water supplementary feed.Result is as shown in table 4 below:
As can be seen from above-described embodiment, the present invention can reduce every pollutent index effectively, completes goal of the invention.Especially the simultaneous test of table 2, demonstrates core of the present invention difference technical characteristic well and has significant progress.
Claims (3)
1. a blue charcoal waste water decarburization removing total nitrogen treatment process, comprises pretreatment system, biochemical treatment system, advanced treatment system successively;
Described pretreatment system comprises an oil trap and secondary cavitation air flotation pond; Described biochemical treatment system at least comprises an Aerobic Pond, oxygen compatibility pool, a settling tank; Described advanced treatment system at least comprises a photocatalytic ozonation reaction tower, and ozone enters water body from photocatalytic ozonation reaction tower lower end by microporous aeration disc; It is characterized in that: photocatalytic ozonation reaction tower top is provided with effuser, cause in described first step cavitation air flotation pond after collecting the residual ozone overflowed from the water surface.
2., according to the blue charcoal waste water of the one described in claim 1 decarburization removing total nitrogen treatment process, it is characterized in that: be provided with loose gas impeller in described cavitation air flotation pond, and add emulsion splitter.
3. according to the blue charcoal waste water of the one described in claim 2 decarburization removing total nitrogen treatment process, it is characterized in that: described advanced treatment system also comprises the advanced treatment system of inner circulating aerating biological filtering tank, BAF, more medium filter, UF/RO membranous system, finally reaches the function of reuse.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439323A (en) * | 2015-12-23 | 2016-03-30 | 云南润玖环境工程有限公司 | Ozone gas floatation circular processing apparatus |
| CN107902835A (en) * | 2016-08-24 | 2018-04-13 | 南京万德斯环保科技股份有限公司 | A kind of device for handling high solids content high-salt wastewater |
| CN113912237A (en) * | 2021-10-29 | 2022-01-11 | 山东亚泰国宇环保科技有限公司 | Heavy-pollution semi-coke wastewater treatment process |
| CN115304216A (en) * | 2022-08-03 | 2022-11-08 | 上海扉悦环保科技有限公司 | Semi-coke wastewater treatment process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103102040A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Method for treating refinery sewage organic matter |
| CN103553269A (en) * | 2013-10-31 | 2014-02-05 | 北京清大国华环保科技有限公司 | Method and device for treating and recycling semi-coke wastewater |
-
2015
- 2015-03-24 CN CN201510129478.9A patent/CN104724888A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103102040A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Method for treating refinery sewage organic matter |
| CN103553269A (en) * | 2013-10-31 | 2014-02-05 | 北京清大国华环保科技有限公司 | Method and device for treating and recycling semi-coke wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 水工业市场杂志: "《"十一五"水处理关键技术与工程应用案例大全》", 31 October 2010, 中国环境科学出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439323A (en) * | 2015-12-23 | 2016-03-30 | 云南润玖环境工程有限公司 | Ozone gas floatation circular processing apparatus |
| CN107902835A (en) * | 2016-08-24 | 2018-04-13 | 南京万德斯环保科技股份有限公司 | A kind of device for handling high solids content high-salt wastewater |
| CN113912237A (en) * | 2021-10-29 | 2022-01-11 | 山东亚泰国宇环保科技有限公司 | Heavy-pollution semi-coke wastewater treatment process |
| CN115304216A (en) * | 2022-08-03 | 2022-11-08 | 上海扉悦环保科技有限公司 | Semi-coke wastewater treatment process |
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