CN204779236U - Coking wastewater's high -efficient low -cost processing system - Google Patents
Coking wastewater's high -efficient low -cost processing system Download PDFInfo
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- CN204779236U CN204779236U CN201520351003.XU CN201520351003U CN204779236U CN 204779236 U CN204779236 U CN 204779236U CN 201520351003 U CN201520351003 U CN 201520351003U CN 204779236 U CN204779236 U CN 204779236U
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Abstract
The utility model relates to a coking wastewater's high -efficient low -cost processing system, including pretreatment systems, biochemical treatment system and the degree of depth processing system who connects gradually, pretreatment systems comprises equalizing basin and the little electrolytic reaction ware of iron fillings fly ash, and the biochemical treatment system criticizes formula membrane bioreactor for the preface, and degree of depth processing system is the fine coke adsorption tower, electric mixer and membrane module are established in criticizing the formula membrane reactor to the preface, and the bottom is established the micropore aeration head and is had the aeration pump through the pipe connection. The utility model discloses a method that oxidation, biochemistry and physical absorption combined together is handled coking wastewater, reinforces the getting rid of of difficult degradation polluting substances in the waste water, makes the play water quality of water after handling can reach the requirement that emission standard (DB 211627 -2008) is synthesized to liaoning province's sewage, have the characteristics of effectual, the high -efficient economy of integrated treatment, and realized the recycle of multiple industry by -product, finally realize the zero release and have important realistic meaning to ecological environment's protection coking wastewater.
Description
Technical field
The utility model relates to industrial waste water treatment, particularly relates to a kind of high efficiency, low cost treatment system of coking chemical waste water.
Background technology
Coking chemical waste water is in High T-emperature Carbonization process and gas purification, the waste water that formed in Chemicals treating process, complicated component, Pollutant levels are high, colourity is high, toxicity is large, character is highly stable, biodegradability is poor, except inorganic pollution beyond the region of objective existences such as ammonia nitrogen, cyanogen and thiocyanates, also containing heterocycle and polycyclc aromatic compounds (PAHs) such as phenols, naphthalene, pyridine, quinoline, be one of unmanageable trade effluent of a kind of composition and complexity thereof.
At present, the treatment process of coking chemical waste water can be divided into physico-chemical process and biochemical process substantially.Physico-chemical process has coagulating sedimentation, coagulation air-float, absorption, light electrolysis, wet air oxidation technology etc.Coking chemical waste water belongs to high concentrated organic wastewater, and adopt materializing strategy cost high completely, most enterprise cannot bear.In practical application, materializing strategy technique is used for Wastewater Pretreatment to improve the influent quality of biochemical treatment section and to make waste water reach emission standard for advanced treatment.Adopt biochemical processing method running cost relatively low, most domestic coke-oven plant adopts biochemical processing process.General employing A/O front establishment method and establish the pretreated A of anaerobic hydrolysis
2o technique, these technical process are long and very complicated, and floor space is also larger.Because nitrated, denitrification realize in two reactors, need mixed-liquor return be carried out, and the more difficult control of reflux ratio, control improperly not reach fine treatment effect.In addition, in coking chemical waste water, hardly degraded organic substance concentration is high, and bio-toxicity is large, and above-mentioned technique capacity of resisting impact load is also undesirable.
The Chinese patent of application number 201010130326.8 (applying date is on March 23rd, 2010) discloses one " treatment process of coking chemical waste water ", by coking chemical waste water by oil trap, equalizing tank, iron carbon-Fenton oxidation pond, up flow anaerobic sludge blanket reactor, hydrolysis multi-function pool, anoxic pond, complex enzyme/activated sludge pond and second pond, then discharge water outlet.This kind of method required process structures are more, and complex process, floor space is large, and running cost is also higher.
2006 " water resources and Hydraulic Projects journal " upper paper " integral type film biological reactor Treatment of Wastewater in Coking " (Pei Liang etc.) published, discuss the feasibility by integral type film biological reactor Treatment of Wastewater in Coking, by Adjustment Tests operating parameters, to COD, NH3-N and turbidity all achieve good treatment effect, but it is comparatively large to there is sludge volume, and unit capacity is little, the problem that fouling membrane is more serious, and ammonia nitrogen removal effect is undesirable.
The Chinese patent of application number 200810234318.0 (applying date is on November 18th, 2008) discloses " a kind of process method for treating coking wastewater ", treatment system is made up of physicochemical treatment unit and biochemical treatment unit, wherein physicochemical treatment unit is made up of micro-electrolysis reactor, settling tank, micro-electrolysis reactor with waste iron filing, copper scrap bits and lightweight bulk material for filler.Biochemical treatment unit is made up of inside circulation triphase fluidized bed reactor, utilizes immobilized active mud bead to realize removal of carbon and nitrogen simultaneously.Although water outlet volatile phenol, ammonia nitrogen, colourity can reach integrated wastewater discharge standard primary standard, COD treatment effect is unsatisfactory, only can reach integrated wastewater discharge standard secondary standard.
Application number be 201410478681.2 Chinese patent disclose the treatment process of coking chemical waste water " after a kind of oil removing ", the method is for the pretreated coking chemical waste water of oil removing, light sorbent is added in sequencing batch membrane bioreactor, and regularly refluxing portion Fenton reacts the ferric hydroxide precipitate produced, utilize the adsorption and sedimentation performance of light sorbent and the throwing out of ironic hydroxide, enhance the Biochemical Treatment of waste water.Shortcoming to set up reflux line, ironic hydroxide flco has corrosive nature to pipeline, ironic hydroxide flco some hazardous and noxious substances of complexing in Fenton oxidation process of backflow, such as prussiate, is back in membrane bioreactor the steady running being unfavorable for biochemical system.
Application number be 201410339214.1 Chinese patent disclose " a kind for the treatment of process of coking chemical waste water ", the method is for pretreated coking chemical waste water, light sorbent is added in sequencing batch membrane bioreactor, and regularly refluxing portion Fenton reacts the ferric hydroxide precipitate produced, utilize the adsorption and sedimentation performance of light sorbent and the throwing out of ironic hydroxide, enhance the Biochemical Treatment of waste water.Shortcoming is that the ironic hydroxide flco of backflow has corrosive nature to pipeline, and ironic hydroxide flco some hazardous and noxious substances of complexing in Fenton oxidation process of backflow, be back in membrane bioreactor and can produce toxic action to microorganism, affect Biochemical Treatment.
The Chinese patent of application number 201110400207.4 (applying date is on December 5th, 2011) discloses " a kind for the treatment of process of coking distilled ammonia wastewater ", for coking distilled ammonia wastewater, successively Inner electrolysis and Fenton oxidation process distilled ammonia wastewater is adopted at pretreatment stage, enter biochemical system after improving the biodegradability of waste water to process, effluent quality reaches Wastewater Of Steel Industry first discharge standard, but need in Fenton oxidation process to add a large amount of Fe2+ catalyzer and oxygenant H2O2, cause cost for wastewater treatment higher, be unfavorable for the application of Practical Project.
In sum, because coking chemical waste water complicated component is changeable, long-chain containing multiple difficult degradation and ring-type organic species, wastewater biodegradability is poor, depends merely on a kind for the treatment of process and is difficult to reach desirable effect, and the materialization mostly adopted at present and biochemical coupling technique carry out Treatment of Wastewater in Coking, but it is undesirable to there is treatment effect in processes, the present situation that technical process is complicated and running cost is higher, does not play respective advantage, causes process effluent quality to be difficult to meet existing emission standard.Be necessary to develop a kind for the treatment of effect for above problem good; technical process is simple; and all more rational treatment process of the operation of equipment and investment cost, will coking chemical waste water finally be realized to zero release and the protection of ecotope and the Sustainable development of coal chemical enterprise be had important practical significance.
Utility model content
The utility model provides a kind of high efficiency, low cost treatment system of coking chemical waste water, adopt the method that oxidation, biochemistry and physical adsorption combine, coking chemical waste water is processed, the removal of strengthening to Recalcitrant chemicals matter in waste water, makes the effluent quality after process can reach the requirement of Liaoning Province's integrated wastewater discharge standard (DB21/1627-2008); Have that comprehensive treatment effect is good, the feature of efficient economy, and achieve the recycling of multiple industry byproduct.
In order to achieve the above object, the utility model realizes by the following technical solutions:
A kind of high efficiency, low cost treatment system of coking chemical waste water, comprise the pretreatment system, biochemical treatment system and the advanced treatment system that connect successively, described pretreatment system is made up of the equalizing tank be connected and iron filings flyash micro-electrolysis reactor, biochemical treatment system is sequencing batch membrane bioreactor, and advanced treatment system is coke powder adsorption tower; Establish electric mixer and membrane module in batched membrane reactor, bottom is established micro porous aeration head and is connected with aeration pump by pipeline.
Force (forcing) pump established by the outlet conduit of described equalizing tank, vacuum pump established by the outlet conduit of batched membrane reactor.
In described iron filings flyash micro-electrolysis reactor, the volume ratio of flyash and iron filings is 2:1 ~ 3:1.
The ceramic grain filter particle diameter of described sequencing batch membrane bioreactor filling is 3-5mm, and add-on is 1/7 ~ 1/5 of reactor effective volume.
Dry quenched coke powder footpath in described coke powder adsorption tower is 90 ~ 110 orders.
Compared with prior art, the beneficial effects of the utility model are:
1) method adopting oxidation, biochemistry and physical adsorption to combine processes coking chemical waste water, pollutant each in coking chemical waste water is effectively removed, the removal of strengthening to Recalcitrant chemicals matter in waste water, makes the effluent quality after process can reach the requirement of Liaoning Province's integrated wastewater discharge standard (DB21/1627-2008);
2) in sequencing batch membrane bioreactor, spherical haydite filtrate is added as granular filler, give full play to the large feature also can adhering to a large amount of microorganism of ceramic grain filter specific surface area, ironic hydroxide flco add the character greatly improving mud mixed liquid, enhance the Biochemical Treatment of waste water;
3) gac that micro-electrolysis reaction coal ash instead is traditional, greatly reduces pretreated expense;
4) physical adsorption dry coke quenching coke powder used is the byproduct of metallurgical process, be applied to field of waste water treatment and improve final effluent quality greatly, achieve the object of waste recycling, and the coke powder after absorption can be directly used in SINTERING PRODUCTION without regeneration, meet the policy guidance of developing a circular economy that country advocates;
5) comprehensive treatment effect is good, and technical process is simple, and the operation of equipment and investment cost economical rationality, finally realize zero release to coking chemical waste water and have important practical significance to the protection of ecotope and the Sustainable development of coal chemical enterprise.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
In figure: 1. equalizing tank 2. micro-electrolysis reactor 3. sequencing batch membrane bioreactor 4. coke powder adsorption tower 5. agitator 6. membrane module 7. aeration head 8. force (forcing) pump 9. aeration pump 10. vacuum pump
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described further:
See Fig. 1, it is structural representation of the present utility model, the high efficiency, low cost treatment system of a kind of coking chemical waste water of the utility model, comprise the pretreatment system, biochemical treatment system and the advanced treatment system that connect successively, described pretreatment system is made up of the equalizing tank 1 be connected and iron filings flyash micro-electrolysis reactor 2, biochemical treatment system is sequencing batch membrane bioreactor 3, and advanced treatment system is coke powder adsorption tower 4; Establish electric mixer 5 and membrane module 6 in batched membrane reactor 3, bottom is established micro porous aeration head 7 and is connected with aeration pump 9 by pipeline.
Force (forcing) pump 8 established by the outlet conduit of described equalizing tank 1, the outlet conduit of batched membrane reactor 3 established vacuum pump 10,
In described iron filings flyash micro-electrolysis reactor 2, the volume ratio of flyash and iron filings is 2:1 ~ 3:1.
The ceramic grain filter particle diameter that described sequencing batch membrane bioreactor 3 loads is 3-5mm, and add-on is 1/7 ~ 1/5 of reactor 3 effective volume.
Dry quenched coke powder footpath in described coke powder adsorption tower 4 is 90 ~ 110 orders.
The working process of the high efficiency, low cost treatment system of a kind of coking chemical waste water of the utility model comprises pre-treatment, biochemical treatment and advanced treatment process, specifically comprises the steps:
1) preprocessing process of coking chemical waste water:
The coking chemical waste water collected is passed into equalizing tank 1, adds the vitriol oil and its pH value is regulated, control the pH value of waste water between 3.0 ~ 4.0; Then waste water is introduced in micro-electrolysis reactor 2, take flyash as negative electrode, iron filings are anode, under the combined action of electrochemical reaction, redox reaction, coagulant precipitation and physical adsorption process, make useless Organic substance in water generation oxidizing reaction, destroy its organic polymer structure; Waste water is upper entering and lower leaving in micro-electrolysis reactor 2, and the residence time is 1.0 ~ 2.0h, and the water outlet of micro-electrolysis reactor 2 is pretreated coking chemical waste water;
2) the biochemical treatment process of coking chemical waste water:
Pretreated coking chemical waste water enters into sequencing batch membrane bioreactor 3, ceramic grain filter is filled with in sequencing batch membrane bioreactor 3, and according to sludge concentration in reactor and survey iron concentration in mud, in sequencing batch membrane bioreactor 3, add the ironic hydroxide flco configured, make iron level be the 4%-6% of mud weight; The mode mutually switched by agitator 5 and aeration pump 9 carries out anoxic denitrification and aerobic nitration reaction respectively;
First turn on agitator 5, close aeration pump 9, the anoxia stirring time is 9 ~ 10h, waste water ph controls at 8.0-9.0, active sludge microorganism now in reactor 3 remains the environment of anoxic, utilize water inlet high-enriched organics to carry out anti-nitration reaction as denitrifying carbon source, make nitrate-nitrogen reduction become nitrogen;
Close agitator 5, open aeration pump 9 pairs of sewage and carry out aeration, for the active sludge in reactor 3 provides sufficient oxygen, make it be in oxygen condition, the residue carbonaceous organic material in sewage is effectively degraded; Meanwhile, the ammonium oxidation in waste water is become nitrite nitrogen and nitrate nitrogen by nitrifier, for anoxic phases provides sufficient electron acceptor(EA); The aerobic aeration time is 18 ~ 20h, and pH value controls at 7.0-8.0, and the gas-water ratio of aeration rate and flooding quantity controls at 40 ~ 50:1;
After aerobic aeration, under the suction function of vacuum pump 10, waste water discharges the water outlet as biochemical treatment process after membrane module 6, in exiting water process, macromolecular substance, active sludge microorganism and inorganic particle are all trapped in reactor 3 by membrane module 6, and a wastewater discharge is 1/3 of reactor 3 volume;
3) advanced treatment process of coking chemical waste water:
The water outlet of biochemical treatment process enters into coke powder adsorption tower 4, adopt dry coke quenching coke powder as sorbent material, intake by the top of coke powder adsorption tower 4, bottom water outlet, utilize the adsorptive power of coke powder to remove organic and inorganic suspended particles small in waste water, reduce the colourity of waste water and the content of solvability COD class material further; Waste water ph controls 3.0 ~ 4.0, and the residence time of waste water in coke powder adsorption tower 4 is 2 ~ 3h, and the water outlet of coke powder adsorption tower 4 is the coking chemical waste water after advanced treatment.
Following examples are implemented under premised on technical solutions of the utility model, give detailed embodiment and concrete operating process, but protection domain of the present utility model are not limited to following embodiment.In following embodiment, method therefor is ordinary method if no special instructions.
[embodiment 1]
1) preprocessing process of coking chemical waste water:
Coking chemical waste water in equalizing tank 1 slowly adds the vitriol oil under the state stirred, and the pH value controlling waste water is 3.0, becomes acidic solution, to meet the requirement of follow-up micro-electrolysis reaction; Then coking chemical waste water is injected iron filings flyash micro-electrolysis reactor 2 by force (forcing) pump 8 from top and carry out micro-electrolysis reaction.Keep the residence time of waste water in micro-electrolysis reactor 2 to be 1.0h, the volume ratio of flyash and iron filings is 2:1.The water outlet of iron filings flyash micro-electrolysis reactor 2 is pretreated coking chemical waste water.
2) the biochemical treatment process of coking chemical waste water:
The water outlet of iron filings flyash micro-electrolysis reactor 2 enters into sequencing batch membrane bioreactor 3, in sequencing batch membrane bioreactor 3, load particle diameter is the ceramic grain filter of 3mm, add-on is 1/7 of reactor 3 effective volume, in sequencing batch membrane bioreactor 3, add the ironic hydroxide flco configured, make iron level be 4% of mud weight.First turn on agitator 5, close aeration pump 9, controlling the anoxia stirring time is 9h, and waste water ph controls 8.0, active sludge microorganism now in reactor 3 remains the environment of anoxic, can make full use of and carry out anti-nitration reaction into water high-enriched organics as denitrifying carbon source.Close agitator 5 subsequently, open aeration pump 9 pairs of sewage and carry out aeration, make the active sludge in reactor 3 be in oxygen condition, carry out nitration reaction.Controlling aerobic aeration time is 18h, and pH value controls 7.0, and the gas-water ratio of aeration rate and flooding quantity controls at 40:1.After aerobic aeration, under the suction function of vacuum pump 10, the water after process becomes the water outlet of biochemical system through outlet pipeline, wastewater discharge of each cycle controls for reactor 3 volume 1/3, after draining terminates, close vacuum pump 10, start the circulation of next cycle.Whole process passes through NaHCO
3solution and the vitriol oil control the pH value of waste water.The water outlet of sequencing batch membrane bioreactor 3 is the coking chemical waste water after biochemical treatment.
3) advanced treatment process of coking chemical waste water:
The water outlet of sequencing batch membrane bioreactor 3 enters into coke powder adsorption tower 4.Select dry coke quenching coke powder as sorbent material, coke powder particle diameter is 90 orders, and waste water is upper entering and lower leaving, and controlling waste water ph is 3, and the residence time is 2h, and the water outlet after coke powder adsorption is the coking chemical waste water after final process.
[embodiment 2]
1) preprocessing process of coking chemical waste water:
Coking chemical waste water in equalizing tank 1 slowly adds the vitriol oil under the state stirred, and the pH value controlling waste water is 3.5, becomes acidic solution, to meet the requirement of follow-up micro-electrolysis reaction; Then coking chemical waste water is injected iron filings flyash micro-electrolysis reactor 2 by force (forcing) pump 8 by top and carry out micro-electrolysis reaction.Keep the residence time of waste water in micro-electrolysis reactor 2 to be 1.5h, the volume ratio of flyash and iron filings is 2.5:1.The water outlet of iron filings flyash micro-electrolysis reactor 2 is pretreated coking chemical waste water.
2) the biochemical treatment process of coking chemical waste water:
The water outlet of iron filings flyash micro-electrolysis reactor 2 enters into sequencing batch membrane bioreactor 3, in sequencing batch membrane bioreactor 3, load particle diameter is the ceramic grain filter of 4mm, add-on is 1/6 of reactor effective volume, in sequencing batch membrane bioreactor 3, add the ironic hydroxide flco configured, make iron level be 5% of mud weight.First turn on agitator 5, close aeration pump 9, controlling the anoxia stirring time is 9.5h, and waste water ph controls 8.5, active sludge microorganism now in reactor 3 remains the environment of anoxic, can make full use of and carry out anti-nitration reaction into water high-enriched organics as denitrifying carbon source.Close agitator 5 subsequently, open aeration pump 9 pairs of sewage and carry out aeration, make the active sludge in reactor 3 be in oxygen condition, carry out nitration reaction.Controlling aerobic aeration time is 19h, and pH value controls 7.5, and the gas-water ratio of aeration rate and flooding quantity controls at 45:1.After aerobic aeration, under the suction function of vacuum pump 10, the water after process becomes the water outlet of biochemical system through outlet pipeline, wastewater discharge of each cycle controls for reactor 3 volume 1/3, after draining terminates, close vacuum pump 10, start the circulation of next cycle.Whole process passes through NaHCO
3solution and the vitriol oil control the pH value of waste water.The water outlet of sequencing batch membrane bioreactor 3 is the coking chemical waste water after biochemical treatment.
3) advanced treatment process of coking chemical waste water:
The water outlet of sequencing batch membrane bioreactor 3 enters into coke powder adsorption tower 4.Select dry coke quenching coke powder as sorbent material, coke powder particle diameter is 100 orders, and waste water is upper entering and lower leaving, and controlling waste water ph is 3.5, and the residence time is 2.5h, and the water outlet after coke powder adsorption is the coking chemical waste water after final process.
[embodiment 3]
1) preprocessing process of coking chemical waste water:
Coking chemical waste water in equalizing tank 1 slowly adds the vitriol oil under the state stirred, and the pH value controlling waste water is 4.0, becomes acidic solution, to meet the requirement of follow-up micro-electrolysis reaction; Then coking chemical waste water is injected iron filings flyash micro-electrolysis reactor 2 by force (forcing) pump 8 by top and carry out micro-electrolysis reaction.Keep the residence time of waste water in micro-electrolysis reactor 2 to be 2.0h, the volume ratio of flyash and iron filings is 3:1.The water outlet of iron filings flyash micro-electrolysis reactor 2 is pretreated coking chemical waste water.
2) the biochemical treatment process of coking chemical waste water:
The water outlet of iron filings flyash micro-electrolysis reactor 2 enters into sequencing batch membrane bioreactor 3, in sequencing batch membrane bioreactor 3, load particle diameter is the ceramic grain filter of 5mm, add-on is 1/5 of reactor 3 effective volume, in sequencing batch membrane bioreactor 3, add the ironic hydroxide flco configured, make iron level be 6% of mud weight.First turn on agitator 5, closes aeration pump 9, and controlling the anoxia stirring time is 10h, waste water ph controls 9.0, active sludge microorganism now in reactor 3 remains the environment of anoxic, can make full use of into water high-enriched organics as denitrifying carbon source, carry out anti-nitration reaction.Close agitator 5 subsequently, open aeration pump 9 pairs of sewage and carry out aeration, make the active sludge in reactor 3 be in oxygen condition, carry out nitration reaction.Controlling aerobic aeration time is 20h, and pH value controls 8.0, and the gas-water ratio of aeration rate and flooding quantity controls at 50:1.After aerobic aeration, under the suction function of vacuum pump 10, the water after process becomes the water outlet of biochemical system through outlet pipeline, wastewater discharge of each cycle controls for reactor 3 volume 1/3, after draining terminates, close vacuum pump 10, start the circulation of next cycle.Whole process passes through NaHCO
3solution and the vitriol oil control the pH value of waste water.The water outlet of sequencing batch membrane bioreactor 3 is the coking chemical waste water after biochemical treatment.
3) advanced treatment process of coking chemical waste water:
The water outlet of sequencing batch membrane bioreactor 3 enters into coke powder adsorption tower 4.Select dry coke quenching coke powder as sorbent material, coke powder particle diameter is 110 orders, and waste water is upper entering and lower leaving, and controlling waste water ph is 4.0, and the residence time is 3h, and the water outlet after coke powder adsorption is the coking chemical waste water after final process.
The main water-quality guideline of coking chemical waste water water inlet is COD:3321.7mg/L, ammonia nitrogen: 125.2mg/L, total nitrogen: 172.8mg/L, volatile phenol: 630.2mg/L, total cyanogen: 12.7mg/L, oil: 35.6mg/L.
After comprehensive treating process, the leading indicator of each embodiment water outlet is as shown in table 1:
Pollutant load (unit: mg/L) in each embodiment water outlet of table 1
| COD | Ammonia nitrogen | Total nitrogen | Oil | Volatile phenol | Total cyanogen | |
| Embodiment 1 | 43.2 | 4.1 | 10.4 | 2.1 | 0.13 | 0.12 |
| Embodiment 2 | 36.4 | 3.4 | 8.7 | 1.7 | 0.11 | 0.09 |
| Embodiment 3 | 41.7 | 2.5 | 9.2 | 1.9 | 0.08 | 0.11 |
From result in table 1, coking chemical waste water after the utility model process, COD≤50mg/L, ammonia nitrogen≤8mg/L, total nitrogen≤15mg/L, oil≤3mg/L, volatile phenol≤0.3mg/L, total cyanogen≤0.2mg/L, Process for Effluent water conditioning, reaches the requirement of Liaoning Province's integrated wastewater discharge standard (DB21/1627-2008).
Claims (5)
1. the high efficiency, low cost treatment system of a coking chemical waste water, it is characterized in that, comprise the pretreatment system, biochemical treatment system and the advanced treatment system that connect successively, described pretreatment system is made up of the equalizing tank be connected and iron filings flyash micro-electrolysis reactor, biochemical treatment system is sequencing batch membrane bioreactor, and advanced treatment system is coke powder adsorption tower; Establish electric mixer and membrane module in batched membrane reactor, bottom is established micro porous aeration head and is connected with aeration pump by pipeline.
2. the high efficiency, low cost treatment system of a kind of coking chemical waste water according to claim 1, is characterized in that, force (forcing) pump established by the outlet conduit of described equalizing tank, and vacuum pump established by the outlet conduit of batched membrane reactor.
3. the high efficiency, low cost treatment system of a kind of coking chemical waste water according to claim 1, is characterized in that, in described iron filings flyash micro-electrolysis reactor, the volume ratio of flyash and iron filings is 2:1 ~ 3:1.
4. the high efficiency, low cost treatment system of a kind of coking chemical waste water according to claim 1, is characterized in that, the ceramic grain filter particle diameter of described sequencing batch membrane bioreactor filling is 3-5mm, and add-on is 1/7 ~ 1/5 of reactor effective volume.
5. the high efficiency, low cost treatment system of a kind of coking chemical waste water according to claim 1, is characterized in that, the dry quenched coke powder footpath in described coke powder adsorption tower is 90 ~ 110 orders.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107129040A (en) * | 2016-02-29 | 2017-09-05 | 鞍钢股份有限公司 | A kind of method and device for extending sequencing batch membrane bioreactor film service life |
| CN107555701A (en) * | 2016-06-30 | 2018-01-09 | 鞍钢股份有限公司 | A kind of method of low-cost processes coking chemical waste water |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107129040A (en) * | 2016-02-29 | 2017-09-05 | 鞍钢股份有限公司 | A kind of method and device for extending sequencing batch membrane bioreactor film service life |
| CN107555701A (en) * | 2016-06-30 | 2018-01-09 | 鞍钢股份有限公司 | A kind of method of low-cost processes coking chemical waste water |
| CN107555701B (en) * | 2016-06-30 | 2020-09-29 | 鞍钢股份有限公司 | Low-cost coking wastewater treatment method |
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Granted publication date: 20151118 Termination date: 20210527 |