CN104944676A - Method for treating coking nanofiltration concentrated water - Google Patents
Method for treating coking nanofiltration concentrated water Download PDFInfo
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Abstract
The invention discloses a method for treating coking nanofiltration concentrated water and especially high-conductivity wastewater. Coking nanofiltration concentrated water is sequentially treated by a pH regulation aeration tank, treated by an anoxic SBR (sequencing batch reactor) bioreactor process, treated by an aerobic-anoxic-aerobic SBR bioreactor process, and finally subjected to a coagulative precipitation process. The SBR main reaction tank in the anoxic SBR bioreactor process mainly adopts an influent-anoxic-precipitation drainage-idling operating mode, and the aerobic-anoxic-aerobic SBR bioreactor main reaction tank mainly adopts an influent-aerobic aeration-anoxic stirring-aerobic aeration-precipitation drainage-idling operating mode. The coking nanofiltration concentrated water treatment system has the advantages of low on-time investment, stable wastewater treatment effect, low production operating cost and high automation degree, and is simple to operate. The quality of the nanofiltration concentrated water effluent completely reaches the requirements for national discharge standard.
Description
Technical field
The invention belongs to water-treatment technology field, be specifically related to the process system that the dense water of a kind of coking nanofiltration removes COD and total nitrogen.
Background technology
China is a coke big country.Coking is typical case's " two high money " industry of high energy consumption, high pollution, resource.Produce in the process of coke and can discharge a large amount of waste water, 100,000,000 tons of coking chemical waste waters about discharge every year in China.
The coking chemical waste water waste water that to be coal formed in high temperature carbonization and gas purification, chemical products treating process, wherein containing tens kinds of pollutents such as phenol, ammonia nitrogen, cyanogen, benzene, pyridine, indoles and quinoline, complicated component, organic contamination substrate concentration and Colority of Sewage Water is high, toxicity is large, character is highly stable, is a kind of typical organic wastewater with difficult degradation thereby.
Current country just progressively improves the emission standard of waste water and relevant " energy-saving and emission-reduction " policy, rose on October 1, upper 2012 and promulgated new " Iron And Steel Industry pollution discharge standard " (GB13456-2012) and " coking chemistry emission of industrial pollutants standard " (GB16171-2012), wherein " coking chemistry emission of industrial pollutants standard " required from 1 day January in 2015, the standard C OD that existing enterprise performs is 80mg/L, BOD is 20mg/L, ammonia nitrogen is 10mg/L, total nitrogen is 20mg/L, total cyanide is 0.2mg/L, and to petroleum-type, volatile phenol, sulfide, polycyclic aromatic hydrocarbons (PAHs), benzo (a) Bi etc. all has strict requirement.
Waste water recycling is the ultimate aim of wastewater treatment, is the enforcement means that industry energy conservation reduces discharging.At present simple coking waste water reuse technology cannot meet enterprise requirements, and after the coking chemical waste water after biochemical treatment is carried out advanced treatment, reuse is inevitable trend.
Domestic coking wastewater deep treatment technology adopts nanofiltration and reverse osmosis technology using reuse after coking wastewater deep treatment as iron and steel enterprise's Municipal Sewage for Circulating, but the subject matter existed is the process of the dense water that nanofiltration and reverse osmosis produce.Baosteel is only had to adopt ultrafiltration+nanofiltration+reverse osmosis advanced Treatment of Wastewater in Coking at present.
Therefore, the qualified discharge of the dense water of coking nanofiltration of nanofiltration technique generation is problem demanding prompt solution.The dense water of coking nanofiltration, except saltiness height, also containing high COD and nitre nitrogen, if unprocessed and directly discharge, will certainly produce harm greatly to water body environment.
Summary of the invention
Therefore, the technical problem to be solved in the present invention is the water quality and quantity situation for the dense water of coking nanofiltration, develops the treatment process of economy, the dense water removal COD of coking nanofiltration efficiently and total nitrogen, realizes the qualified discharge of waste water, promote the service efficiency of trade effluent, reduce the quantity discharged of ton steel waste water.
Technical scheme of the present invention is, the treatment process of the dense water of a kind of coking nanofiltration, comprise the process of pH regulator aeration tank, the dense water of described coking nanofiltration is after the process of pH regulator aeration tank, enter anoxic SBR bio-reactor operation, enter aerobic-anaerobic-aerobic SBR bio-reactor operation again, eventually pass coagulating sedimentation operation;
The dense water of nanofiltration behind pH regulator pond enters anoxic SBR bio-reactor.The major function of anoxic SBR bio-reactor is that denitrification removes nitre nitrogen.
The operation scheme of SBR main reaction pond water inlet-anoxic-sedimentation and drawing-idle,
Described anoxic SBR bio-reactor operation comprises:
(1) intake: enter anoxic SBR pond from the dense water of the nanofiltration in pH regulator pond according to setting flooding quantity, setting flooding time, i.e. flooding quantity=flooding velocity × flooding time; Described flooding quantity is anoxic sbr reactor device actual capacity, and system controls flooding time and flooding quantity by PLC;
(2) the anoxia stirring phase: after water inlet end, turn on agitator carries out anoxia stirring, adds organic carbon source simultaneously, described organic carbon source is selected from one or more of propionic acid, sherwood oil and lignocellulose; Agitator stirs and makes the mixed solution in whole anoxic SBR main reaction pond be in anoxic condition, and hypoxic exposure is 360min ~ 1200min;
The anoxia stirring stage keeps the dense water of nanofiltration to mix with mud, and denitrifying bacteria carries out digestion denitration nitrogen.By additional carbon, denitrifying bacterium carries out external source denitrification, and nitre nitrogen is reduced to N
2.
Biological denitrification reaction is under the condition of anoxic, and the nitrate produced in nitrifying process or nitrate reductase are become gaseous nitrogen or N
2the process of O, NO comprises Rhodopseudomonas, denitrification Bacillaceae, spiral Pseudomonas and achromobacter etc. by there being a group heterotrophic bacterium to work in coordination with " microorganism participating in this biochemical reaction is denitrifying bacteria " common denitrifying bacteria.They mostly are facultative bacteria, and when there being molecular oxygen to exist, denitrifying bacteria decomposing organic matter, utilizes molecular oxygen as final electron acceptor(EA).Without in molecular oxygen situation, denitrifying bacteria utilizes the nitrogen in NO3-N and NO2-N to make electron acceptor(EA), O
2-generate H as hydrogen acceptor
2o and OH-basicity, organism then provides energy as carbon source and electron donor and obtains oxidation-stabilized.
(3) the sedimentation and drawing phase: after anoxic denitrification, stop, mud-water separation is carried out in SBR main reaction pond, arrive after below the liquid level half of SBR main reaction pond until sludge settling, draining enters alternately aerobic SBR bio-reactor, and after draining terminates, the sedimentation and drawing time is 30min ~ 60min;
(4) the spoil disposal phase: discharge excess sludge, control in the reactor activated sludge concentration (MLSS) at 2800 ~ 4200mg/L; Prevent sludge aging phenomenon, also regularly must discharge excess sludge, for fresh sludge provides enough Growth In Space breedings;
(5) lay-up period: idle mixing time is 60min ~ 180min, makes microorganism activity recovery, for next cycle creates good condition by stirring or leaving standstill; By lay-up period, active sludge is in nutrition starvation, thus enters next cycle and effectively plays its initial effect;
The dense water of nanofiltration of a upper operation drainage period discharge enters aerobic-anaerobic-aerobic SBR bio-reactor.Aerobic-anaerobic-aerobic SBR bio-reactor major function removes COD and organonitrogen.
Described aerobic-anaerobic-aerobic SBR bio-reactor flow process: the operation scheme of main reaction pond water inlet-aerobic aeration-anoxia stirring-aerobic aeration-sedimentation and drawing-idle, the volume capacity of aerobic-anaerobic-aerobic SBR bio-reactor is consistent with anoxic SBR bio-reactor, is controlled the processes such as stirring, aeration, water inlet, draining by PLC.
Described aerobic-anaerobic-aerobic SBR bio-reactor operation comprises:
(1) intake the phase: the dense water of anoxic SBR drainage period discharge enters aerobic-anaerobic-aerobic SBR bio-reactor according to setting flooding quantity, and system controls flooding time and flooding quantity by PLC;
(2) aerobic aeration I phase: after water inlet reaches the liquid level of setting, start aeration, adopt complete mixed aeration mode, make the organism in waste water and the microorganism in pond fully absorb oxygen, dissolved oxygen (DO) in water reaches maximum value, and COD, organonitrogen and ammonia nitrogen constantly reduce; The time of reaction is 120min ~ 360min; Dissolved oxygen solubility is 1.5 ~ 3mg/L; Water outlet COD is 200 ~ 400mg/L, and organonitrogen is 1 ~ 10mg/L, and ammonia nitrogen is 0 ~ 3mg/L.In this step, the clearance of aerobic aeration phase COD is about 50%, and the clearance of organonitrogen and ammonia nitrogen is more than 85%.
(3) the anoxia stirring phase: carry out slow anoxia stirring after aerobic aeration terminates; Agitator stirs and makes the mixed solution in whole SBR main reaction pond be in anoxic condition, and hypoxic exposure is 60min ~ 360min; Utilize bacterial nitrification effect to make ammonia nitrogen convert nitre nitrogen in aerobic aeration process, guarantee that the total nitrogen of water outlet is lower than 15mg/L.Anaerobic phase is that this part nitre nitrogen of removal and anoxic SBR bio-reactor remain the nitre nitrogen do not removed.
(4) aerobic aeration II phase: anoxia stirring terminates rear continuation aeration, the hardly degraded organic substance that degraded front-end-of-line is not removed, effluent quality COD is lower than 60mg/L; The dosage of Black Liquor with Efficient Bacteria is 0 ~ 0.2g/kg; The aerobic aeration time is 120min ~ 720min;
(5) the sedimentation and drawing phase: after anoxic denitrification, stop, mud-water separation is carried out in SBR main reaction pond, arrive after below the liquid level half of SBR main reaction pond until sludge settling, draining enters alternately aerobic SBR bio-reactor, and after draining terminates, the sedimentation and drawing time is 30min ~ 60min;
(6) the spoil disposal phase: regularly discharge excess sludge, control in the reactor activated sludge concentration (MLSS) at 3500 ~ 4500mg/L;
(7) lay-up period: idle mixing time is 60min ~ 180min, by stir, aeration or leave standstill make Microbial Communities in Activated Sludge fully rest activity recovery, for next cycle creates good condition.
According to the treatment process of the dense water of a kind of coking nanofiltration of the present invention, preferably, in the treatment process of described pH regulator aeration tank, add acidic substance adjust ph in pH regulator pond, pH value is controlled at 7.0-9.0.
According to the treatment process of the dense water of a kind of coking nanofiltration of the present invention, preferably, described acidic substance are one or both in industrial waste sulfuric acid, waste hydrochloric acid; More preferably, described acidic substance are the Waste Sulfuric Acid of 10%-80%.
Preferably, in described equalizing tank, pH meter and robot control system(RCS) are housed.
According to the treatment process of the dense water of a kind of coking nanofiltration of the present invention, preferably, the dense water water quality of coking nanofiltration in pH regulator pond is entered described in: pH is 8 ~ 11; Specific conductivity is 8000 ~ 18000 μ s/cm; COD is 100 ~ 600mg/L; Total nitrogen: 50 ~ 300mg/L.The principal character of the dense water of coking nanofiltration is high conductivity, high COD, the waste water of high total nitrogen.The main component of total nitrogen is nitre nitrogen and organonitrogen.
According to the treatment process of the dense water of a kind of coking nanofiltration of the present invention, preferably, in described anoxic SBR bio-reactor operation in step (2), when independent a kind of organic carbon source, dosage is propionic acid is 150 ~ 900mg/L; Sherwood oil is 300 ~ 1300mg/L; Lignocellulose is 600 ~ 2200mg/L.
Or, in described anoxic SBR bio-reactor operation in step (2), when adding three kinds of organic carbon sources, propionic acid: sherwood oil: the mass percent of lignocellulose is 1 ~ 80%:1 ~ 70%:1 ~ 60%.Also can any two kinds of carbon sources used in combination.Further, propionic acid: sherwood oil: the mass percent of lignocellulose is 40%:40%:20% or 3:1:1.
Preferably, in described aerobic-anaerobic-aerobic SBR bio-reactor process (4), anoxia stirring can add denitrification biological inoculum after terminating rear continuation aeration.This denitrification biological inoculum is commercially available bacterial classification.Add biological inoculum and can make better effects if.
According to the treatment process of the dense water of a kind of coking nanofiltration of the present invention, preferably, described coagulating sedimentation operation is carried out in coagulative precipitation tank; The coagulating agent adopted in described coagulating sedimentation operation is the one in Tai-Ace S 150, iron trichloride, ferrous sulfate, potassium aluminium sulfate (alum), sodium aluminate and ferric sulfate, and the flocculation agent adopted in described coagulating sedimentation operation is Polyacrylamide (PAM).
Further, described coagulant charging quantity is 100mg/L ~ 800mg/L; Described polyacrylamide dosage is 0.1-1mg/L, and optimizing polyacrylamide dosage is 0.5mg/L.
Coagulating agent and flocculation agent with the use of the colourity and the COD that remove nanofiltration waste water in, short period of time, guarantee that water outlet COD is lower than 50mg/L in reaction tank.After coagulating sedimentation, particulate matter precipitation enters bucket bottom settling tank, the mud periodic cleaning in bucket and outward transport.
SBR biochemical system adopts variable volume batch reactor, eliminate returned sluge system and settling apparatus, aeration completes with being deposited in same container, utilize the growth velocity of microorganism under different flco loading condiction and biological carbon and phosphorous removal mechanism, bio-reactor is combined with variable volume reactor, forms the Sludge System of one-period operation sexual refractoriness.SBR biochemical system composition is simple, and without the need to establishing sludge reflux equipment, do not establish second pond, aeration tank volume is also less than continous way, and construction cost and working cost are all lower.In addition SBR system also has following characteristics: (1) in most of the cases (comprises Industrial Wastewater Treatment), without the necessity arranging equalizing tank.(2) SVI value is lower, and mud is easy to precipitation, generally, does not produce sludge bulking phenomenon.(3) by the adjustment to operation scheme, denitrogenation can be carried out and remove phosphorus reaction in single aeration tank.(4) apply the automatic instrument(s)s such as motorized valve, liquidometer, timing register and programmable controller, this technological process may be made to realize whole automatization, and controlled by master control room.(5) operational management is proper, and process water water quality is better than continous way.
The invention has the beneficial effects as follows:
The present invention proposes the technical scheme of the dense water of coking chemical waste water nanofiltration, the dense water of exploitation coking nanofiltration removes the technique of COD and total nitrogen, and with environment protection main task, decreasing pollution, responds actively the legislations of environmental protection of increasingly stringent.Technical scheme system of the present invention solves the problem of COD and the direct exhaust emission environment of total nitrogen in the dense water of coking nanofiltration, and the COD in the dense water of the nanofiltration after the technical program process and total nitrogen can reach the emission standard of national requirements.
Adopt the dense water technology of coking chemical waste water nanofiltration of the present invention, treatment effect is stablized, and production run cost is low, and operation runs easy, and level of automation is high.Therefore the invention belongs to iron and steel environmental protection production-process systems.
Through process program process of the present invention, the dense water effluent quality of nanofiltration: PH is 7 ~ 9; Specific conductivity is 8000 ~ 18000 μ s/cm; COD is less than 50mg/L; Total nitrogen is less than 10mg/L, reaches the requirement of discharging standards completely.
Accompanying drawing explanation
The dense water treatment technological process of Fig. 1 coking nanofiltration.
Embodiment
Certainly, those skilled in the art in the art will be appreciated that, above-described embodiment is only used to the present invention is described, but not is used as limitation of the invention, as long as in spirit of the present invention, the conversion of above-described embodiment, distortion all will be dropped in the scope of the claims in the present invention.
Embodiment 1:
The dense water inlet flow-patterm of coking nanofiltration is 10; Specific conductivity is 15000 μ s/cm; COD is 450mg/L; Total nitrogen: 150mg/L.
The dense water of coking chemical waste water nanofiltration enters pH regulator aeration tank, and pH value controls 7.0.The time that waste water stops in equalizing tank is 1h.The industrial waste acid added is 30% Waste Sulfuric Acid.
The dense water of nanofiltration behind pH regulator pond enters anoxic SBR bio-reactor.Rear sbr reactor device of having intake controls to start anoxia stirring according to PLC.Add 300mg/L propionic acid, 300mg/L sherwood oil, 150mg/L lignocellulose is as additional carbon, and agitator stirs and makes the mixed solution in whole anoxic SBR main reaction pond be in anoxic condition, and hypoxic exposure is 600min, and the sedimentation and drawing time is 30min.In reactor, activated sludge concentration (MLSS) is at 3200mg/L.After draining spoil disposal, idle mixing time is 120min.
Then the dense water of nanofiltration enters aerobic-anaerobic-aerobic SBR bio-reactor.The time of reaction aerobic aeration (I) phase is 200min.Dissolved oxygen solubility is 3mg/L.Anoxia stirring phase hypoxic exposure is 300min.The dosage of aerobic aeration (II) phase Black Liquor with Efficient Bacteria is 0.2g/kg.The aerobic aeration time is 500min.The sedimentation and drawing time is 30min; Activated sludge concentration (MLSS) is at 3500mg/L.Idle mixing time is 60min.
The water outlet of SBR bio-reactor enters coagulative precipitation tank.Tai-Ace S 150 dosage is 300mg/L, and polyacrylamide dosage is 0.5mg/L.
Through process program process of the present invention, the dense water effluent quality of nanofiltration: pH is 8.3; Specific conductivity is 16000 μ s/cm; COD is 35mg/L; Total nitrogen is 6.4mg/L.
Embodiment 2:
The dense water inlet flow-patterm of coking nanofiltration is 11; Specific conductivity is 17000 μ s/cm; COD is 550mg/L; Total nitrogen: 280mg/L.
The dense water of coking chemical waste water nanofiltration enters pH regulator aeration tank, and pH value controls 7.5.The time that waste water stops in equalizing tank is 3h.The industrial waste acid added is 75% Waste Sulfuric Acid.
The dense water of nanofiltration behind pH regulator pond enters anoxic SBR bio-reactor.Rear sbr reactor device of having intake controls to start anoxia stirring according to PLC.Add 300mg/L propionic acid, 400mg/L lignocellulose is as additional carbon, and agitator stirs and makes the mixed solution in whole anoxic SBR main reaction pond be in anoxic condition, and hypoxic exposure is 1000min, and the sedimentation and drawing time is 60min.In reactor, activated sludge concentration (MLSS) is at 3900mg/L.After draining spoil disposal, idle mixing time is 180min.
Then the dense water of nanofiltration enters aerobic-anaerobic-aerobic SBR bio-reactor.The time of reaction aerobic aeration (I) phase is 300min.Dissolved oxygen solubility is 2.5mg/L.Anoxia stirring phase hypoxic exposure is 360min.The dosage of aerobic aeration (II) phase Black Liquor with Efficient Bacteria is 0.2g/kg.The aerobic aeration time is 500min.The sedimentation and drawing time is 30min; Activated sludge concentration (MLSS) is at 3500mg/L.Idle mixing time is 60min.
The water outlet of SBR bio-reactor enters coagulative precipitation tank.Iron trichloride dosage is 500mg/L, and polyacrylamide dosage is 0.5mg/L.
Through process program process of the present invention, the dense water effluent quality of nanofiltration: pH is 8.1; Specific conductivity is 18000 μ s/cm; COD is 31mg/L; Total nitrogen is 7.3mg/L.
Embodiment 3:
The dense water inlet flow-patterm of coking nanofiltration is 9; Specific conductivity is 18000 μ s/cm; COD is 500mg/L; Total nitrogen: 300mg/L.
The dense water of coking chemical waste water nanofiltration enters pH regulator aeration tank, and pH value controls 9.0.The time that waste water stops in equalizing tank is 2h.The industrial waste acid added is 60% Waste Sulfuric Acid.
The dense water of nanofiltration behind pH regulator pond enters anoxic SBR bio-reactor.Rear sbr reactor device of having intake controls to start anoxia stirring according to PLC.Add 400mg/L propionic acid, 200mg/L sherwood oil, 200mg/L lignocellulose is as additional carbon, and agitator stirs and makes the mixed solution in whole anoxic SBR main reaction pond be in anoxic condition, and hypoxic exposure is 1200min, and the sedimentation and drawing time is 50min.In reactor, activated sludge concentration (MLSS) is at 4200mg/L.After draining spoil disposal, idle mixing time is 160min.
Then the dense water of nanofiltration enters aerobic-anaerobic-aerobic SBR bio-reactor.The time of reaction aerobic aeration (I) phase is 360min.Dissolved oxygen solubility is 1.5mg/L.Anoxia stirring phase hypoxic exposure is 360min.The dosage of aerobic aeration (II) phase Black Liquor with Efficient Bacteria is 0.1g/kg.The aerobic aeration time is 700min.The sedimentation and drawing time is 60min; Activated sludge concentration (MLSS) is at 4200mg/L.Idle mixing time is 180min.
The water outlet of SBR bio-reactor enters coagulative precipitation tank.Ferrous sulfate dosage is 600mg/L, and polyacrylamide dosage is 0.5mg/L.
Through process program process of the present invention, the dense water effluent quality of nanofiltration: pH is 7.9; Specific conductivity is 18000 μ s/cm; COD is 42mg/L; Total nitrogen is 8.6mg/L.
Embodiment 4:
The dense water inlet flow-patterm of coking nanofiltration is 8.6; Specific conductivity is 17800 μ s/cm; COD is 420mg/L; Total nitrogen: 225mg/L.
The dense water of coking chemical waste water nanofiltration enters pH regulator aeration tank, and pH value controls 8.8.The time that waste water stops in equalizing tank is 2h.The industrial waste acid added is 57% Waste Sulfuric Acid.
The dense water of nanofiltration behind pH regulator pond enters anoxic SBR bio-reactor.Rear sbr reactor device of having intake controls to start anoxia stirring according to PLC.Add 350mg/L propionic acid, 180mg/L sherwood oil, 140mg/L lignocellulose is as additional carbon, and agitator stirs and makes the mixed solution in whole anoxic SBR main reaction pond be in anoxic condition, and hypoxic exposure is 1000min, and the sedimentation and drawing time is 50min.In reactor, activated sludge concentration (MLSS) is at 3950mg/L.After draining spoil disposal, idle mixing time is 140min.
Then the dense water of nanofiltration enters aerobic-anaerobic-aerobic SBR bio-reactor.The time of reaction aerobic aeration (I) phase is 360min.Dissolved oxygen solubility is 1.6mg/L.Anoxia stirring phase hypoxic exposure is 360min.The dosage of aerobic aeration (II) phase Black Liquor with Efficient Bacteria is 0.1g/kg.The aerobic aeration time is 700min.The sedimentation and drawing time is 60min; Activated sludge concentration (MLSS) is at 3800mg/L.Idle mixing time is 180min.
The water outlet of SBR bio-reactor enters coagulative precipitation tank.Ferric sulfate dosage is 600mg/L, and polyacrylamide dosage is 0.5mg/L.
Through process program process of the present invention, the dense water effluent quality of nanofiltration: pH is 8.1; Specific conductivity is 17800 μ s/cm; COD is 37mg/L; Total nitrogen is 8.1mg/L.
Steel industry one is directly subordinate to waste water consumption and discharge rich and influential family, and energy-saving and emission-reduction are developing directions.The present invention proposes the systems technology solution of the dense water of coking chemical waste water nanofiltration of low cost first.Therefore the present invention not only has economy and environmental protection double effects, but also has good social benefit and environmental benefit.Coking nanofiltration of the present invention dense water treatment system one-time investment is low; Liquid waste disposal effect stability; Production run cost is low; Level of automation is high, simple to operate.The present invention has fully demonstrated the effect of energy-saving and emission-reduction, is environmentally friendly green process for producing steel and iron.
Claims (9)
1. the treatment process of the dense water of coking nanofiltration, comprise the process of pH regulator aeration tank, it is characterized in that: the dense water of described coking nanofiltration is after the process of pH regulator aeration tank, enter anoxic SBR bio-reactor operation, enter aerobic-anaerobic-aerobic SBR bio-reactor operation again, eventually pass coagulating sedimentation operation;
Described anoxic SBR bio-reactor operation comprises:
(1) intake: enter anoxic SBR pond from the dense water of the nanofiltration in pH regulator pond according to setting flooding quantity, setting flooding time, i.e. flooding quantity=flooding velocity × flooding time; Described flooding quantity is anoxic sbr reactor device actual capacity, and system controls flooding time and flooding quantity by PLC;
(2) the anoxia stirring phase: after water inlet end, turn on agitator carries out anoxia stirring, adds organic carbon source simultaneously, described organic carbon source is selected from one or more of propionic acid, sherwood oil and lignocellulose; Agitator stirs and makes the mixed solution in whole anoxic SBR main reaction pond be in anoxic condition, and hypoxic exposure is 360min ~ 1200min;
(3) the sedimentation and drawing phase: after anoxic denitrification, stop, mud-water separation is carried out in SBR main reaction pond, arrive after below the liquid level half of SBR main reaction pond until sludge settling, draining enters alternately aerobic SBR bio-reactor, and after draining terminates, the sedimentation and drawing time is 30min ~ 60min;
(4) the spoil disposal phase: discharge excess sludge, control in the reactor activated sludge concentration (MLSS) at 2800 ~ 4200mg/L;
(5) lay-up period: idle mixing time is 60min ~ 180min, makes microorganism activity recovery, for next cycle creates good condition by stirring or leaving standstill;
Described aerobic-anaerobic-aerobic SBR bio-reactor operation comprises:
(1) intake the phase: the dense water of anoxic SBR drainage period discharge enters aerobic-anaerobic-aerobic SBR bio-reactor according to setting flooding quantity, and system controls flooding time and flooding quantity by PLC;
(2) aerobic aeration I phase: after water inlet reaches the liquid level of setting, start aeration, adopt complete mixed aeration mode, make the organism in waste water and the microorganism in pond fully absorb oxygen, dissolved oxygen (DO) in water reaches maximum value, and COD, organonitrogen and ammonia nitrogen constantly reduce; The time of reaction is 120min ~ 360min; Dissolved oxygen solubility is 1.5 ~ 3mg/L; Water outlet COD is 200 ~ 400mg/L, and organonitrogen is 1 ~ 10mg/L, and ammonia nitrogen is 0 ~ 3mg/L;
(3) the anoxia stirring phase: carry out slow anoxia stirring after aerobic aeration terminates; Agitator stirs and makes the mixed solution in whole SBR main reaction pond be in anoxic condition, and hypoxic exposure is 60min ~ 360min; Utilize bacterial nitrification effect to make ammonia nitrogen convert nitre nitrogen in aerobic aeration process, guarantee that the total nitrogen of water outlet is lower than 15mg/L;
(4) aerobic aeration II phase: anoxia stirring terminates rear continuation aeration, the hardly degraded organic substance that degraded front-end-of-line is not removed, effluent quality COD is lower than 60mg/L; The dosage of Black Liquor with Efficient Bacteria is 0 ~ 0.2g/kg; The aerobic aeration time is 120min ~ 720min;
(5) the sedimentation and drawing phase: after anoxic denitrification, stop, mud-water separation is carried out in SBR main reaction pond, arrive after below the liquid level half of SBR main reaction pond until sludge settling, draining enters alternately aerobic SBR bio-reactor, and after draining terminates, the sedimentation and drawing time is 30min ~ 60min;
(6) the spoil disposal phase: regularly discharge excess sludge, control in the reactor activated sludge concentration (MLSS) at 3500 ~ 4500mg/L;
(7) lay-up period: idle mixing time is 60min ~ 180min, by stir, aeration or leave standstill make Microbial Communities in Activated Sludge fully rest activity recovery, for next cycle creates good condition.
2. the treatment process of the dense water of a kind of coking nanofiltration according to claim 1, is characterized in that, in the treatment process of described pH regulator aeration tank, adds acidic substance adjust ph, pH value is controlled at 7.0-9.0 in pH regulator pond.
3. the treatment process of the dense water of a kind of coking nanofiltration according to claim 2, is characterized in that, described acidic substance are one or both in industrial waste sulfuric acid, waste hydrochloric acid; PH meter and robot control system(RCS) are housed in described equalizing tank.
4. the treatment process of the dense water of a kind of coking nanofiltration according to claim 1, is characterized in that, described in enter the dense water water quality of nanofiltration in pH regulator pond: pH is 8 ~ 11; Specific conductivity is 8000 ~ 18000 μ s/cm; COD is 100 ~ 600mg/L; Total nitrogen: 50 ~ 300mg/L.
5. the treatment process of the dense water of a kind of coking nanofiltration according to claim 1, is characterized in that, in described anoxic SBR bio-reactor operation in step (2), when independent a kind of organic carbon source, dosage is propionic acid is 150 ~ 900mg/L; Sherwood oil is 300 ~ 1300mg/L; Lignocellulose is 600 ~ 2200mg/L.
6. the treatment process of the dense water of a kind of coking nanofiltration according to claim 1, is characterized in that, when adding three kinds of organic carbon sources, and propionic acid: sherwood oil: the mass percent of lignocellulose is 1 ~ 80%:1 ~ 70%:1 ~ 60%.
7. the treatment process of the dense water of a kind of coking nanofiltration according to claim 1, is characterized in that, in described aerobic-anaerobic-aerobic SBR bio-reactor process (4), anoxia stirring adds denitrification biological inoculum after terminating rear continuation aeration.
8. the treatment process of the dense water of a kind of coking nanofiltration according to claim 1, is characterized in that, described coagulating sedimentation operation is carried out in coagulative precipitation tank; The coagulating agent adopted in described coagulating sedimentation operation is the one in Tai-Ace S 150, iron trichloride, ferrous sulfate, potassium aluminium sulfate, sodium aluminate and ferric sulfate, and the flocculation agent adopted in described coagulating sedimentation operation is Polyacrylamide (PAM).
9. the treatment process of the dense water of a kind of coking nanofiltration according to claim 8, it is characterized in that, described coagulant charging quantity is 100mg/L ~ 800mg/L; Described polyacrylamide dosage is 0.1-1mg/L.
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| CN106630243A (en) * | 2015-10-29 | 2017-05-10 | 宝山钢铁股份有限公司 | Method and apparatus for removing COD and cyanion from coked nano-filtration concentrated water |
| CN107758865A (en) * | 2016-08-19 | 2018-03-06 | 宝山钢铁股份有限公司 | A kind of synchronous method for removing nitrate nitrogen, ammonia nitrogen and COD in coking reverse osmosis concentrated water |
| CN109607965A (en) * | 2019-01-09 | 2019-04-12 | 湖北君集水处理有限公司 | A kind of system and method for sewage treatment plant tail water advanced nitrogen dephosphorization |
| CN109626746A (en) * | 2019-01-14 | 2019-04-16 | 中原环保郑州设备工程科技有限公司 | The middle-size and small-size multipoint water feeding advanced nitrogen dephosphorization sewage disposal system of integration and processing method |
| CN109704514A (en) * | 2019-01-21 | 2019-05-03 | 湖北君集水处理有限公司 | A kind of system and method for advanced treatment of wastewater and concentrated water disposition |
| CN111423059A (en) * | 2020-04-07 | 2020-07-17 | 水艺控股集团股份有限公司 | Improved SBR sewage treatment device and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106630243A (en) * | 2015-10-29 | 2017-05-10 | 宝山钢铁股份有限公司 | Method and apparatus for removing COD and cyanion from coked nano-filtration concentrated water |
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| CN109626746A (en) * | 2019-01-14 | 2019-04-16 | 中原环保郑州设备工程科技有限公司 | The middle-size and small-size multipoint water feeding advanced nitrogen dephosphorization sewage disposal system of integration and processing method |
| CN109704514A (en) * | 2019-01-21 | 2019-05-03 | 湖北君集水处理有限公司 | A kind of system and method for advanced treatment of wastewater and concentrated water disposition |
| CN111423059A (en) * | 2020-04-07 | 2020-07-17 | 水艺控股集团股份有限公司 | Improved SBR sewage treatment device and method |
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