CN106219885A - Coking waste water treatment method based on jet biochemical reactor - Google Patents
Coking waste water treatment method based on jet biochemical reactor Download PDFInfo
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- CN106219885A CN106219885A CN201610755788.6A CN201610755788A CN106219885A CN 106219885 A CN106219885 A CN 106219885A CN 201610755788 A CN201610755788 A CN 201610755788A CN 106219885 A CN106219885 A CN 106219885A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/121—Multistep treatment
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
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Abstract
The present invention relates to a kind of coking waste water treatment method based on jet biochemical reactor, including air supporting pretreatment, Prepositive denitrification process, biochemical reactor process, degassing process, rear-mounted denitrification processes and hyperfiltration treatment, reverse osmosis/nanofiltration process.Overall flow of the present invention is reasonable in design, biochemical processing process and film advanced treatment process is used to combine, activated sludge is retained by external ultrafiltration, process technique A/O/A with Prepositive denitrification process, biochemical reactor and rear-mounted denitrification and collectively form MBR technique, can improve the organic volumetric loading of processing system, group technology high treating effect, investment and operating cost are relatively low, water outlet can reach reuse standard, and investment and operating cost are relatively low.
Description
Technical field
The present invention relates to a kind of coking waste water treatment method based on jet biochemical reactor, belong to Industrial Wastewater Treatment skill
Art field.
Background technology
Coal chemical industry enterprises, in the production process such as coking, gas processed, discharges a large amount of complicated component, organic concentrations height, difficult degradation
Coking chemical waste water.Coking chemical waste water mainly contains inorganic pollution and oils, the volatilizations such as cyanide, rhodanide, ammonia nitrogen, heavy metal
The organic pollution such as phenol, polycyclic aromatic hydrocarbon.China promulgated " coking chemistry emission of industrial pollutants standard " in 2012
(GB16171-2012), Treatment of Coking Effluent and discharge are proposed higher requirement, organic pollution and nitrogen class are discharged control
Make stricter.Its regulation was from 1 day January in 2015, and disposal of pollutants limit value is: COD < 80mg/L, ammonia nitrogen < 10mg/L, total nitrogen <
20mg/L, volatile phenol < 0.3mg/L, sulfide < 0.5mg/L, cyanide < 0.2mg/L.Coking waste water treatment process mainly includes
Physical, chemical method and biochemical process.At present, application biochemical processing is most widely used, but single biochemical processing process
Often it is difficult to ensure that treatment effect.
For ensureing deamination effect, current coking chemical waste water biochemical treatment unit many employings nitrification/denitrification is core
Biological denitrification process, is mainly realized by anoxia (or anaerobism)/aerobic combination method, and Common combinations technique includes A/O method, O/A/O
Method, A/O/O method etc..But there are the following problems in Practical Project for above-mentioned technique:
(1), water outlet is the most up to standard.
When using above-mentioned biochemical combination treatment method to process coking chemical waste water, water inlet nutrient is wanted by coking chemical waste water
Seek generally C:N:P=100:5:1.And phenol content is higher in coking chemical waste water, therefore COD (COD) concentration is higher；And
Ammonia nitrogen concentration depends on leading portion ammonia distillation process operation stability, and general amplitude of variation is bigger, it is difficult to reach aforementioned proportion.If entered
Water COD concentration is high, and the dominant bacteria in aerobic reactor is heterotrophic bacteria, it is suppressed that the growth of Autotrophic nitrification bacterium.It addition, in Jin Shui
Biostatic agent also can affect the activity of nitrifier, causes nitric efficiency to decline, and water outlet COD COD, ammonia nitrogen, total nitrogen are difficult
With the most up to standard.
(2), oxygen transmission efficiency is low, aerating system energy consumption high.
In aeration process evaluation index, oxygen transmission efficiency is a very important evaluation index, which determines unit
The energy consumption of oxygenation capacity.At present, Treatment of Coking Effluent factory major part uses micro-pore aeration technology, such as micropore aeration pipe and aeration film
Dish.Its oxygen transmission efficiency only has 5%～20%, needs supporting powerful blower fan, and aeration system energy consumption accounts for treatment plant's total energy
The 50～70% of consumption.It addition, micro-hole aerator quantity is more, change, maintenance cost higher.
, organic loading low, floor space is big.
Conventional activated sludge process volumetric loading is generally less than 1.0kg BOD5/m3D, the Aeration tank needing large volume can
Meet and process requirement.
(4), advanced treating difficulty is big.
Film depth process i.e. nanofiltration (NF) and reverse osmosis (RO) combination have strict demand, bio-chemical effluent water quality to influent quality
Badly, fouling membrane can be caused to aggravate, frequently wash film, change film, increase operating cost.
Therefore as disclosed in CN101913728A a kind of " method for biochemically treating coking wastewater ", the method includes giving up coking
Water carries out pretreatment, pretreated coking chemical waste water feeding anaerobic pond is carried out anaerobic treatment, by the waste water after anaerobic treatment
Sending into aerobic three phase fluidized bed and carry out the steps such as Aerobic Process for Treatment, it utilizes anaerobic treatment and aerobic three phase fluidized bed to process coking and gives up
Water, the method refluxes without nitrification liquid, it is difficult to ensure total nitrogen qualified discharge.Secondly as utilize up-flow anaerobic sludge blanket to react
The carrier fluidized bed biofilm reactor of device, anoxia, two-stage aerobic carrier fluidized bed biofilm reactor Treatment of Wastewater in Coking, but its
Volumetric loading and sludge loading are relatively low, and reactor volume is relatively big, and cost of investment is high.And CN102897979A is disclosed " a kind of burnt
Change the processing method of waste water ", it includes biochemical treatment and the advanced treatment process of coking chemical waste water of coking chemical waste water；Coking chemical waste water
Biochemical treatment uses A2O technique, and coking wastewater deep treatment uses Inner electrolysis+Fenton oxidation coagulating sedimentation+activated carbon adsorption
Method, undeclared oxidation panel uses which kind of reactor and aeration mode, and advanced treatment process is simple, it is difficult to ensure treatment effect.
Summary of the invention
It is an object of the invention to provide a kind of stable, cost of investment is low, standard water discharge based on jet biochemical reaction
The coking waste water treatment method of device.
The present invention is that the technical scheme reaching above-mentioned purpose is: a kind of Treatment of Coking Effluent based on jet biochemical reactor
Method, it is characterised in that: sequentially include the following steps:
(1), air supporting pretreatment: the coking chemical waste water in regulating reservoir is passed through in air floatation machine, by the oils and fats in coking chemical waste water, glue
Shape thing and solid suspension form water-gas-granule three-phase mixed system in air floatation machine, deliver to preposition to the water outlet after separating
In denitrification pond, scum silica frost deliver to sludge dewatering system, the oils in coking chemical waste water and SS clearance >=90% after process, COD goes
Except rate >=10%；
(2), Prepositive denitrification processes: the water outlet after air-flotation process is delivered to the nitrification liquid with backflow in Prepositive denitrification pond
It is sufficiently mixed with mud, by the BOD in the former water of coking chemical waste water and the carbon source in mud, the organic matter in coking chemical waste water is carried out
Denitrification, sludge concentration controls 15～30g/L, dissolved oxygen concentration≤0.5mg/L；
(3), biochemical reactor processes:
1., the water outlet that Prepositive denitrification processes is delivered in one-level biochemical reactor, following in one-level biochemical reactor
Waste water is extracted out and sprays into one-level biochemical reactor by two-phase nozzle solid jet by ring pump, and aerating activated sludge is removed in waste water
High-concentration organic matter, the dominant bacteria of described activated sludge is heterotrophic bacteria, the hydraulic detention time control of one-level biochemical reactor
System is 3.5～4.5h, and sludge concentration is 15～30g/L, and dissolved oxygen controls 2～8mg/L, and COD clearance, 85～95%, is waved
Sending out phenol clearance >=99%, cyanide clearance is 85～95%；
2. the water outlet after, being processed by one-level biochemical reaction is sent in secondary biochemical reactor, in secondary biochemical reactor
Circulating pump waste water is extracted out and sprays into secondary biochemical reactor by two-phase nozzle solid jet, aerating activated sludge is to waste water
Carrying out nitration reaction, be nitrate nitrogen by mineralized nitrogen, the dominant bacteria of described activated sludge is ammonia nitrogen autotrophic bacteria, and secondary biochemical reacts
The hydraulic detention time of device controls 7～9h, the control of the sludge concentration of secondary biochemical reactor 15～30g/L, dissolved oxygen
Control 2～8mg/L；Ammonia nitrogen removal frank >=95%；
(4), degassing processes: reacted for biochemical reactor water outlet sent in degassing pond, by membranous disc aeration to residue ammonia
Nitrogen continues nitrification, deaerates under making activated sludge at suspended state in degassing pond, and dissolved oxygen concentration≤0.5mg/L, in degassing pond
Nitrification liquid be back to Prepositive denitrification pond, and the reflux ratio of nitrification liquid is 100～300%；
(5), rear-mounted denitrification processes: delivers in rear-mounted denitrification pond by the water outlet in degassing pond, throws in rear-mounted denitrification pond
Adding external carbon source, carry out anti-nitration reaction to remaining nitrate nitrogen in waste water and be converted into nitrogen, sludge concentration is 15～30g/L, molten
Solving oxygen concentration≤0.5mg/L, the water outlet of rear-mounted denitrification is delivered to intermediate pool and is precipitated, and the supernatant of intermediate pool delivers to external
Ultrafilter, the mud of bottom send sludge dewatering system, and the waterpower of intermediate pool stays the time to be 3～5h, and the sludge concentration of intermediate pool exists
15～30g/L；
(6), hyperfiltration treatment: the water outlet of intermediate pool is delivered in external ultrafilter, by the membrane module of external ultrafilter
Mud mixture carries out solid-liquid separation, and clear liquid sends into reverse osmosis membrane assembly or nanofiltration membrane component, and sludge reflux is to forward type nitre
Change in pond；
(7), reverse osmosis or nanofiltration device process: clear liquid after ultrafiltration is sent into reverse osmosis membrane assembly or nanofiltration membrane component, by instead
Organic pollution in clear liquid and salinity are retained by permeable membrane element or nanofiltration membrane component, and the concentrated solution after process send concentration
Liquid treating system, output Treated sewage reusing or qualified discharge.
The biochemical processing process of coking waste water treatment method of the present invention uses air supporting pretreatment, Prepositive denitrification to process, life
Change reactor for treatment and degassing process and rear-mounted denitrification processes group technology, removed in coking chemical waste water by air supporting pretreatment
Jelly and solid suspension, alleviate the load of subsequent treatment section, make subsequent treatment process energy stable operation.By preposition
Denitrification processes and carries out denitrogenation processing, can fully be diluted the coking chemical waste water of high organic concentrations, and can utilize coking chemical waste water
The BOD of Central Plains water carries out denitrification, and the nitrification liquid after the mud of nanofiltration and degassing being processed is back to forward type nitrification tank
Interior as carbon source, the organic mass-energy in coking chemical waste water is carried out abundant denitrification, reaches the purpose of denitrogenation, additional carbon can be reduced
Add, reduce processing cost.Biochemical reactor of the present invention processes and uses Two-Stage Biochemical reactor, by biochemical reactor
Circulating pump and two-phase nozzle solid jet, carry out high speed nozzle jet-flow aeration, add between air, activated sludge and waste water
Haptoreaction area so that activated sludge fully reacts with waste water, is lived by the aeration of the high oxygenation of biochemical reactor
Property mud remove the high-concentration organic matter in waste water, remove the COD in coking chemical waste water and ammonia nitrogen.The present invention uses injection circulation raw
Changing reactor, organic loading is high, can improve microbial reaction efficiency and coefficient of oxygen utilization, and sludge yield is low, simultaneously biochemical reactor
Floor space is little, it is ensured that nitration reaction is stably carried out.The present invention is processed by degassing and is avoided that because of the activity in biochemical reactor
Mud is in high oxygenation state, and in causing pond when making nitrate mixed-liquor return to Prepositive denitrification pond, dissolved oxygen is too high, and affects
The problem of denitrification effect, processes through rear-mounted denitrification, solves and can be applicable to denitrifying degradable carbon source in coking chemical waste water
Content is unstable, makes the problem that denitrification denitrogenation effect is difficult to ensure that.The present invention is entered by Prepositive denitrification and rear-mounted denitrification
Row denitrogenation processing, can fully ensure that denitrification effect so that water outlet total nitrogen can stably reaching standard.Inventive film advanced treatment process is adopted
Process with hyperfiltration treatment and reverse osmosis or nanofiltration, retain activated sludge by external ultrafiltration, it is not necessary to special membrane cisterna, reduce
Floor space, and clean, safeguard more convenient, through reverse osmosis or nanofiltration as film advanced treatment process, effluent quality is relatively
High, it is possible to stably to reach medium and small reuse or qualified discharge.Disposed of in its entirety technological design of the present invention is reasonable, have employed at efficient biochemical device
Science and engineering skill and film advanced treatment process combine, and retain activated sludge by external ultrafiltration, with Prepositive denitrification process, biochemistry instead
Answer device and rear-mounted denitrification to process technique A/O/A and collectively form MBR technique, in MBR technique, mud in each biochemical reaction tank
Concentration all can be controlled in 15～30g/L, improves the organic volumetric loading of processing system, group technology high treating effect, investment and
Operating cost is relatively low.
Accompanying drawing explanation
Below in conjunction with the accompanying drawings embodiments of the invention are described in further detail.
Fig. 1 is the schematic flow sheet of present invention coking waste water treatment method based on jet biochemical reactor.
Detailed description of the invention
As shown in Figure 1, present invention coking waste water treatment method based on jet biochemical reactor, sequentially include the following steps:
(1), air supporting pretreatment: the coking chemical waste water in regulating reservoir is passed through in air floatation machine, regulating reservoir can be first passed through coking is given up
Water carries out the regulation of water quality and quantity.By air floatation machine by the oils and fats in coking chemical waste water, jelly and solid suspension in air supporting
In machine formed water-gas-granule three-phase mixed system, after making particle adhesion bubble, formed apparent density less than water flco and on
Climb up on top of the water, form scum layer and separated, thus realize solid-liquid or liquid-liquid separation, the water outlet after separating is delivered to preposition
In denitrification pond, scum silica frost deliver to sludge dewatering system.The pneumatically supported hydraulic detention time of the present invention controls 0.8～1.5h, processes
Oils in rear coking chemical waste water and SS clearance >=90%, COD clearance >=10%.The present invention also can when air supporting pretreatment,
Adding dosing coagulant and flocculant to air floatation machine, by mass percentage, the addition of coagulant is coking chemical waste water total amount
0.001～0.01%, the addition of flocculant is the 0.005～0.015% of coking chemical waste water total amount；Coagulant can use tri-chlorination
Ferrum or ferrous sulfate and flocculant can use polyacrylamide, by coagulant and the effect of flocculant, by coking chemical waste water
Oils and fats, jelly and solid suspension can preferably form scum layer, remove oil, SS and the macromole in coking chemical waste water organic
Thing, brings more significant adverse effect to reduce to subsequent treatment especially film processing system.
(2), Prepositive denitrification processes: the water outlet after air-flotation process is delivered to the nitrification liquid with backflow in Prepositive denitrification pond
Being sufficiently mixed with mud, this nitrification liquid is 50～the nitrate nitrogen of 80% that biochemical reactor produces, before being back to behind degassed pond
Put in denitrification pond, focused as carbon source by the Biochemical oxygen demand BOD in the former water of coking chemical waste water and backflow nitrification liquid and mud
Change waste water and carry out denitrification, in anaerobic environment NO3-N and NO2-N by anaerobe and mud as carbon source in the case of
It is reduced into nitrogen to discharge, reaches biological denitrificaion, oxidation operation also can be made to decompose simultaneously.The waterpower of Prepositive denitrification of the present invention is stopped
Staying the time to control 6～7h, sludge concentration controls 15～30g/L, and dissolved oxygen concentration≤0.5mg/L, denitrification rate exists
0.09～0.12kg NO3-N/kg VS.d, denitrification load is at 0.9～1.2kg NO3-N/m3.d, ammonia nitrogen removal frank 75～
90%.
(3), biochemical reactor processes: the present invention passes through Two-Stage Biochemical reactor for treatment, removes except coking chemical waste water is highly concentrated
Degree, difficult degradation organic matter, reduce volatile phenol, cyanide and the ammonia nitrogen concentration in waste water.
1., the water outlet that Prepositive denitrification processes is delivered in one-level biochemical reactor, following in one-level biochemical reactor
Waste water is extracted out and sprays into one-level biochemical reactor by two-phase nozzle solid jet by ring pump, and aerating activated sludge is removed in waste water
High-concentration organic matter, the dominant bacteria of activated sludge is heterotrophic bacteria, and the hydraulic detention time of one-level biochemical reactor controls 3.5
～4.5h, sludge concentration is 15～30g/L, and dissolved oxygen controls 2～8mg/L, COD volumetric loading >=16kg COD/m3.d, warp
One-level biochemical reactor process after COD clearance 85～95%, volatile phenol clearance >=99%, cyanide clearance 85～
95%, remove high concentration, difficult degradation organic matter, reduce volatile phenol, cyanide and COD concentration.
2., secondary biochemical treatment: the water outlet after being processed by one-level biochemical reactor is sent in secondary biochemical reactor, through two
Waste water is extracted out and sprays into secondary biochemical reactor, aeration by two-phase nozzle solid jet by the circulating pump in level biochemical reactor
Activated sludge carries out nitration reaction to waste water, is nitrate nitrogen by mineralized nitrogen, and the dominant bacteria of activated sludge is ammonia nitrogen autotrophic bacteria, energy
Ensure that Nitrification is stably carried out.The hydraulic detention time of secondary biochemical reactor controls 7～9h, secondary biochemical reactor
The control of sludge concentration is 15～30g/L, and dissolved oxygen controls 2～8mg/L, ammonia nitrogen volumetric loading >=1.2kg NH4-N/m3.d,
Ammonia nitrogen removal frank >=95% of waste water after secondary biochemical reactor for treatment.
Firsts and seconds biochemical reactor of the present invention all uses injection circulation biochemical reactor, by big flow, big lift
Circulating pump, make the mixed liquor in firsts and seconds biochemical reactor extract out, then sprayed back by the two-phase nozzle of biochemical reactor
In biochemical reactor, the shearing regions of turbulent flow under vacuum state can be formed due to jet expansion, have air hose in the middle of nozzle simultaneously,
Air is taken out of by the coking chemical waste water of high flow rate from the central canal of nozzle, bypasses air through nozzle and forms small gas in shearing turbulent region
Bubble, violent turbulent flow makes the big activated sludge group in reactor resolve into little flco and forms primary aeration effect, can increase
Add the haptoreaction area between air, activated sludge and coking chemical waste water so that activated sludge fully reacts with waste water, carries
High microorganism reaction efficiency.Organic loading is high, can improve microbial reaction efficiency and coefficient of oxygen utilization, and sludge yield is low, gives birth to simultaneously
Change reactor floor space little, it is ensured that nitration reaction is stably carried out.
The height of one-level biochemical reactor of the present invention and secondary biochemical reactor is 7～14m, and ratio of height to diameter is 2.5～3.5,
Pump flow is the 300～1000% of flow of inlet water, nozzle instantaneous velocity 40～50m/s, the rate of transform of oxygen 35～
50%, the utilization rate of oxygen is at 0.5～3.0kg O2/m3.h.The one-level of the present invention and secondary biochemical reactor have higher oxygen and turn
Move efficiency and the utilization rate of oxygen, activated sludge, useless water and air in reactor in shuttling movement state, except high speed nozzle jet
Outside aeration, when circulating mixed liquor and being re-moved to two-phase nozzle region, bubble and mud the most broken generation secondary aeration
Effect, thus expand gas-solid-liquid contact area further, improve microbial reaction efficiency and coefficient of oxygen utilization, by the exposure of high oxygenation
Gas activated sludge removes the high-concentration organic matter in waste water, reduces volatile phenol, cyanide and ammonia nitrogen concentration in waste water.
(4), degassing processes: the reacted water outlet of biochemical reactor is sent in degassing pond, by membranous disc aeration to residue ammonia nitrogen
Continue nitrification, deaerate under making activated sludge at suspended state in degassing pond, owing to the activity after biochemical reactor processes is dirty
Mud is in high oxygenation state, and in causing pond when being avoided that because of nitrate mixed-liquor return to Prepositive denitrification pond, dissolved oxygen is too high, shadow
Ring denitrification effect, processed the dissolved oxygen reducing activated sludge by degassing.The deaerate hydraulic detention time in pond of the present invention is 0.5
～1.5h, dissolved oxygen concentration≤0.5mg/L, rear-mounted denitrification pond is delivered in the water outlet in degassing pond, nitrification liquid is back to preposition anti-nitre
Change pond, and the reflux ratio of nitrification liquid is 100～300%.
(5), rear-mounted denitrification processes: delivers in rear-mounted denitrification pond by the water outlet in degassing pond, throws in rear-mounted denitrification pond
Adding external carbon source, additional carbon is glucose or methanol or feces water, using as protection carbonization treatment, to remaining nitre in waste water
Nitrogen carries out anti-nitration reaction and is converted into nitrogen.The waterpower of rear-mounted denitrification of the present invention stays the time to be 3～5h, and sludge concentration is 15
～30g/L, dissolved oxygen concentration≤0.5mg/L, when carrying out denitrification with methanol as additional carbon, rear-mounted denitrification speed exists
0.12～0.2kg NO3-N/kg VS.d, denitrification load is at 1.2～1.5kg NO3-N/m3.d, to ensure after postorder processes
Water outlet total nitrogen is up to standard.
Water outlet being delivered to intermediate pool precipitate, the supernatant of intermediate pool delivers to external ultrafilter, base sludge send dirt
Mud dewatering system, the waterpower of intermediate pool stays the time to be 3～5h, and the sludge concentration of intermediate pool, 15～30g/L, can pass through intermediate pool
Carbonaceous organic material in waste water can be removed further, nitrogen that stripping denitrification produces, and certain dissolved oxygen can be kept, prevent dirt
Mud releases phosphorus affects water outlet.
(6), hyperfiltration treatment: the water outlet of intermediate pool is delivered in external ultrafilter, by the membrane module of external ultrafilter
Mud mixture carries out solid-liquid separation, and clear liquid sends into reverse osmosis membrane assembly or nanofiltration membrane component, and sludge reflux is to forward type nitre
Change in pond, can be as the carbon source of Prepositive denitrification reaction.The present invention passes through ultrafiltration, and microorganism is completely trapped at biological respinse
In device, instead of traditional second pond and filtering technique, make the sludge concentration in biochemical system can control 15～30g/L, this
Invention external ultrafilter uses tubular ultra-filtration membrane to separate, and its rate of circulating flow is 1～2m/s, and permeant flux is 45～70L/
m2.h。
(7), reverse osmosis or nanofiltration process: clear liquid after ultrafiltration is sent into reverse osmosis membrane assembly, and reverse osmosis membrane assembly is in clear liquid
Organic pollution and salinity retain, and the concentrated solution after process send concentrated solution processing system, output Treated sewage reusing, and the present invention is anti-
Permeable membrane element can use rolled film, and producing water ratio is 75～85%, and permeant flux is 15～20L/m2.h, after reverse-osmosis treated
Can reach the rejection such as organic pollution, monovalent salt, divalent salts can be to more than 99%.Clear liquid after reverse osmosis process processes
COD concentration is less than 0.5mg/L less than 10mg/L, ammonia nitrogen concentration less than 10mg/L, SS concentration less than 60mg/L, BOD concentration.Up to
To " urban sewage reutilization-industry water standard " (GB/T 19923-2005) recycle water standard.
Clear liquid after ultrafiltration also can be sent into nanofiltration membrane component and clear liquid carries out depth-type filtration process by the present invention, exports clear water
Concentrated solution processing system is sent to reverse osmosis membrane assembly, concentrated solution.Nanofiltration technique of the present invention use rolled film, producing water ratio be 85～
90%, permeant flux is 20～25L/m2.h, and after nanofiltration processes, nanofiltration clear liquid COD concentration is little less than 80mg/L, BOD concentration
In 20mg/L, volatile phenol concentration is 0.1mg/L, and concentration of cyanide is 0.1mg/L, and ammonia nitrogen concentration is low less than 10mg/L, SS concentration
In 0.5mg/L, can reach table 2 standard in " coking chemistry emission of industrial pollutants standard " (GB16171-2012).
In pretreated chemical sludge and intermediate pool base sludge are sent sludge dewatering system by the present invention, sludge dewatering
System carries out solid-liquid separation to mud, and clear liquid is back in air floatation machine, and the dry mud after dehydration can fill.And through nanofiltration or anti-
Concentrated solution after infiltration processes send concentrated solution processing system, the technique spray such as the concentrated solution clear liquid after membrane filtration is used for sintering, ironmaking
Return biochemical system after slag, or oxidation processes, or use evaporation technology to process, and concentrated solution dope, thus can realize coking chemical waste water
Zero-emission dispose.
The coking chemical waste water using coking waste water treatment method of the present invention to discharge certain coal chemical industry enterprises processes, through oil removing
Intaking as native system after processing with ammonia still process, the design water yield is 1000m3/ d, influent quality is as shown in table 1.
Table 1
| Water quality index | pH | COD | BOD | Ammonia nitrogen | Total nitrogen | Volatile phenol | Cyanide | SS |
| Numerical value mg/L | 6-9 | 4500 | 800 | 450 | 450 | 400 | 15 | 50 |
Embodiment 1
Coking chemical waste water is delivered to regulating reservoir carry out water quality and quantity and be adjusted, its water quality be COD concentration be 4500mg/L,
BOD concentration 800mg/L, ammonia nitrogen concentration 450mg/L, volatile phenol concentration 700mg/L, concentration of cyanide 30mg/L, total nitrogen concentration
500mg/L, SS concentration 50mg/L.Being passed through in air floatation machine by coking chemical waste water in regulating reservoir, hydraulic detention time is after 1h, separation
Water outlet deliver in Prepositive denitrification pond, scum silica frost delivers to sludge dewatering system, and presses GB16171-2012 standard detection, after process
Oils in coking chemical waste water and SS clearance 90%, COD clearance is 10%, and BOD clearance is 10%, and ammonia nitrogen removal frank exists
11%, nitrogen removal rate is 10%, and volatile phenol clearance is 14%, and cyanide clearance is 33%.
Water outlet Prepositive denitrification pond after air-flotation process, with the nitrification liquid of backflow and mud in Prepositive denitrification pond fully
Mixing, degassing pond in mixed liquid recycle ratio 100%, return sludge ratio 100%, the hydraulic detention time of Prepositive denitrification
Controlling at 6.5h, sludge concentration controls at 20g/L, and dissolved oxygen concentration is at 0.45mg/L, and denitrification rate is at 0.1kg NO3-N/
Kg VS.d, denitrification spatial load forecasting is at 1.0kg NO3-N/m3.d.After testing, compared with water former with coking chemical waste water, nitrogen removal rate
70%.
In sending biochemical reactor by the water outlet that Prepositive denitrification processes, one-level, secondary biochemical reactor internal circulation pump flow
For the 500% of flow of inlet water, nozzle instantaneous velocity is at 45m/s, and the rate of transform of oxygen is 40%, and the utilization rate of oxygen is at 1.5kg O2/
M3.h, the hydraulic detention time of one-level biochemical reactor controls at 4h, and sludge concentration is 20g/L, and dissolved oxygen controls at 4mg/L,
COD volumetric loading is 16kg COD/m3.d, after testing, after one-level biochemical reactor processes, the COD concentration of coking chemical waste water is
500mg/L, BOD concentration is 200mg/L, and ammonia nitrogen concentration is 25mg/L, and volatile phenol concentration is 0.2mg/L, and concentration of cyanide is
0.2mg/L, total nitrogen concentration is 60mg/L.
Water outlet after being processed by one-level biochemical reactor is sent in secondary biochemical reactor, the waterpower of secondary biochemical reactor
The time of staying controls at 8h, and the control of the sludge concentration of secondary biochemical reactor is at 20g/L, and dissolved oxygen controls at 4mg/L, ammonia nitrogen
Volumetric loading is at 1.2kg NH4-N/m3.d, and after testing, after secondary biochemical reactor for treatment, the COD concentration of coking chemical waste water is
320mg/L, BOD concentration is 50mg/L, and ammonia nitrogen concentration is 15mg/L, and volatile phenol concentration is 0.1mg/L, and concentration of cyanide is
0.1mg/L, total nitrogen concentration is 60mg/L.
Water outlet after being processed by biochemical reactor is sent in degassing pond, and the degassing tank waterpower time of staying is 1h, and dissolved oxygen is dense
Spending at 0.4mg/L, the nitrification liquid in degassing pond is back to Prepositive denitrification pond, and the reflux ratio of nitrification liquid is 100%, and deaerate pond
Water outlet deliver in rear-mounted denitrification pond, in rear-mounted denitrification pond, add external carbon source, the waterpower of rear-mounted denitrification stays the time
For 4h, sludge concentration is 20g/L, and dissolved oxygen concentration is at 0.4mg/L, and rear-mounted denitrification speed is at 0.13kg NO3-N/kg
VS.d, rear-mounted denitrification load is 1.3kg NO3-N/m3.d, water outlet being delivered to intermediate pool and precipitates, the waterpower of intermediate pool is stayed
Time is 4h, and the sludge concentration of intermediate pool is at 20g/L, and after testing, the COD concentration of intermediate pool water outlet is 300mg/L, BOD concentration
For 20mg/L, ammonia nitrogen concentration is 10mg/L, and volatile phenol concentration is 0.1mg/L, and concentration of cyanide is 0.1mg/L, and total nitrogen concentration is
25mg/L。
The water outlet of intermediate pool delivered in external ultrafilter, excess sludge send sludge dewatering system, external ultrafilter
Rate of circulating flow is 1～2m/s, and permeant flux is 45～70L/m2.h, carries out solid-liquid separation through the membrane module of external ultrafilter,
Reverse osmosis membrane assembly sent into by clear liquid, and in sludge reflux to forward type nitrification tank, the reflux ratio of mud is 100%.After testing, ultrafiltration
COD concentration in clear liquid be 250mg/L, BOD concentration be 20mg/L, ammonia nitrogen concentration is 10mg/L, and volatile phenol concentration is 0.1mg/
L, concentration of cyanide is 0.1mg/L, and total nitrogen concentration is that 25mg/L, SS concentration is less than 1mg/L.
Clear liquid after ultrafiltration is sent into reverse osmosis membrane assembly, and reverse osmosis membrane assembly producing water ratio is 75～85%, and permeant flux is
15～20L/m2.h, the Treated sewage reusing after reverse-osmosis treated post processing, concentrated solution send concentrated solution processing system, after testing, instead
Infiltration clear liquid COD concentration be 50mg/L, BOD concentration be 5mg/L, ammonia nitrogen concentration is 5mg/L, and volatile phenol concentration is 0.1mg/L, cyanogen
Compound concentration is 0.1mg/L, and total nitrogen concentration is that 10mg/L, SS concentration is less than 0.5mg/L.The clear liquid of coking chemical waste water after treatment
Can reach " urban sewage reutilization-industry water standard " (GB/T 19923-2005) recycle water standard.
Embodiment 2
Coking chemical waste water is delivered to regulating reservoir carry out water quality and quantity and be adjusted, its water quality be COD concentration be 4500mg/L,
BOD concentration 800mg/L, ammonia nitrogen concentration 500mg/L, volatile phenol concentration 700mg/L, concentration of cyanide 30mg/L, total nitrogen concentration
500mg/L, SS concentration 50mg/L.Being passed through in air floatation machine by coking chemical waste water in regulating reservoir, hydraulic detention time, at 1.2h, separates
After water outlet deliver in Prepositive denitrification pond, scum silica frost delivers to sludge dewatering system, adds dosing coagulant and flocculation to air floatation machine
Agent, by mass percentage, the addition of coagulant is the 0.005% of coking chemical waste water total amount, and the addition of flocculant is that coking is given up
The 0.01% of water inventory.And press GB16171-2012 standard detection, the oils in coking chemical waste water and SS clearance 92% after process,
COD clearance is 15%, and BOD clearance is 15%, and ammonia nitrogen removal frank is 13%, and nitrogen removal rate is 10%, and volatile phenol is removed
Rate is 15%, and cyanide clearance is 35%.
Water outlet after air-flotation process is sufficiently mixed with nitrification liquid and mud in delivering to Prepositive denitrification pond, part in degassing pond
Mixed liquid recycle ratio is 200%, and the hydraulic detention time of Prepositive denitrification controls at 7h, and sludge concentration controls at 25g/L, dissolves
Oxygen concentration is at 0.4mg/L, and denitrification rate controls at 0.12kg NO3-N/kg VS.d, and denitrification spatial load forecasting is at 1.2kg
NO3-N/m3.d.After testing, compared with water former with coking chemical waste water, nitrogen removal rate is 75%.
The water outlet that Prepositive denitrification processes is delivered in biochemical reactor, one-level, secondary biochemical reactor internal circulation pump stream
Amount is the 800% of flow of inlet water, and nozzle instantaneous velocity is at 45m/s, and the rate of transform of oxygen is 40%, and the utilization rate of oxygen is at 1.5kg
O2/m3.h.The hydraulic detention time of one-level biochemical reactor controls at 4.5h, and sludge concentration is 25g/L, and dissolved oxygen controls
4mg/L, COD volumetric loading is 120kg COD/m3.d.After testing, after one-level biochemical reactor processes, the COD of coking chemical waste water is dense
Degree is 180mg/L for 450mg/L, BOD concentration, and ammonia nitrogen concentration is 20mg/L, and volatile phenol concentration is 0.2mg/L, concentration of cyanide
For 0.2mg/L, total nitrogen concentration is 60mg/L.
Water outlet after being processed by one-level biochemical reactor is sent in secondary biochemical reactor, the waterpower of secondary biochemical reactor
The time of staying controls at 7.5h, and the control of the sludge concentration of secondary biochemical reactor is at 25g/L, and dissolved oxygen controls at 4mg/L, ammonia
Nitrogen volumetric loading is at 1.2kg NH4-N/m3.d.After testing, after secondary biochemical reactor for treatment, the COD concentration of coking chemical waste water is
250mg/L, BOD concentration is 40mg/L, and ammonia nitrogen concentration is 10mg/L, and volatile phenol concentration is 0.1mg/L, and concentration of cyanide is
0.1mg/L, total nitrogen concentration is 60mg/L.
Water outlet after being processed by biochemical reactor is sent in degassing pond, and the hydraulic detention time in degassing pond is 1.2h, dissolves
Oxygen concentration part nitrification liquid in 0.4mg/L, degassing pond is back to Prepositive denitrification pond, and the reflux ratio of nitrification liquid exists
The water outlet in 200% degassing pond is delivered in rear-mounted denitrification pond, adds external carbon source in rear-mounted denitrification pond, rear-mounted denitrification
Waterpower stays the time to be 4.2h, and sludge concentration is 25g/L, and dissolved oxygen concentration is at 0.4mg/L, and rear-mounted denitrification speed is at 0.18kg
NO3-N/kg VS.d, rear-mounted denitrification load is 1.8kg NO3-N/m3.d, intermediate pool is delivered in water outlet and precipitates, middle
The waterpower in pond stays the time to be 4.2h, and the sludge concentration of intermediate pool is at 25g/L.After testing, the COD concentration of intermediate pool water outlet is
200mg/L, BOD concentration is 15mg/L, and ammonia nitrogen concentration is 8mg/L, and volatile phenol concentration is 0.1mg/L, and concentration of cyanide is
0.1mg/L, total nitrogen concentration is 20mg/L.
The water outlet of intermediate pool delivered in external ultrafilter, excess sludge send sludge dewatering system, external ultrafilter
Rate of circulating flow is 1～2m/s, and permeant flux is 45～70L/m2.h, carries out solid-liquid separation through the membrane module of external ultrafilter,
Nanofiltration membrane component sent into by clear liquid, and in sludge reflux to forward type nitrification tank, the reflux ratio of mud is 100%.After testing, ultrafiltration is clear
COD concentration in liquid be 250mg/L, BOD concentration be 15mg/L, ammonia nitrogen concentration is 8mg/L, and volatile phenol concentration is 0.1mg/L, cyanogen
Compound concentration is 0.1mg/L, and total nitrogen concentration is that 20mg/L, SS concentration is less than 1mg/L.
Clear liquid after ultrafiltration is sent into nanofiltration device, and nanofiltration membrane component carries out depth-type filtration process, the product water of nanofiltration device to clear liquid
Rate is 85～90%, and permeant flux is 20～25L/m2.h, and after nanofiltration processes, output clear water is to reverse osmosis membrane assembly, concentration
Liquid send concentrated solution processing system.After testing, nanofiltration clear liquid COD concentration be 50mg/L, BOD concentration be 15mg/L, ammonia nitrogen concentration is
8mg/L, volatile phenol concentration is 0.1mg/L, and concentration of cyanide is 0.1mg/L, and total nitrogen concentration is less than in 10mg/L, SS concentration
0.5mg/L, can reach table 2 standard in " coking chemistry emission of industrial pollutants standard " (GB16171-2012).
Claims (6)
1. a coking waste water treatment method based on jet biochemical reactor, it is characterised in that: sequentially include the following steps:
(1), air supporting pretreatment: the coking chemical waste water in regulating reservoir is passed through in air floatation machine, by the oils and fats in coking chemical waste water, jelly
And solid suspension forms water-gas-granule three-phase mixed system in air floatation machine, preposition anti-nitre is delivered in the water outlet after separating
Change in pond, scum silica frost delivers to sludge dewatering system, the oils in coking chemical waste water and SS clearance >=90%, COD clearance after process
>=10%；
(2), Prepositive denitrification processes: the water outlet after air-flotation process is delivered to nitrification liquid and dirt with backflow in Prepositive denitrification pond
Mud is sufficiently mixed, and by the BOD in the former water of coking chemical waste water and the carbon source in mud, the organic matter in coking chemical waste water is carried out anti-nitre
Changing, sludge concentration controls 15～30g/L, dissolved oxygen concentration≤0.5mg/L；
(3), biochemical reactor processes:
1., the circulating pump in one-level biochemical reactor, in one-level biochemical reactor is delivered in the water outlet that Prepositive denitrification processes
Being extracted out by waste water and spray into one-level biochemical reactor by two-phase nozzle solid jet, aerating activated sludge removes the height in waste water
Concentration is organic, and the dominant bacteria of described activated sludge is heterotrophic bacteria, and the hydraulic detention time of one-level biochemical reactor controls
3.5～4.5h, sludge concentration is 15～30g/L, and dissolved oxygen controls 2～8mg/L, COD clearance 85～95%, volatile phenol
Clearance >=99%, cyanide clearance is 85～95%；
2., the water outlet after the process of one-level biochemical reaction is sent in secondary biochemical reactor, following in secondary biochemical reactor
Waste water is extracted out and sprays into secondary biochemical reactor by two-phase nozzle solid jet by ring pump, and waste water is carried out by aerating activated sludge
Nitration reaction, is nitrate nitrogen by mineralized nitrogen, and the dominant bacteria of described activated sludge is ammonia nitrogen autotrophic bacteria, secondary biochemical reactor
Hydraulic detention time controls 7～9h, and the control of the sludge concentration of secondary biochemical reactor is 15～30g/L, and dissolved oxygen controls
2～8mg/L；Ammonia nitrogen removal frank >=95%；
(4), degassing processes: reacted for biochemical reactor water outlet is sent in degassing pond, is continued residue ammonia nitrogen by membranous disc aeration
Continuous nitrification, deaerates under making activated sludge at suspended state in degassing pond, dissolved oxygen concentration≤0.5mg/L, the nitre in degassing pond
Change liquid and be back to Prepositive denitrification pond, and the reflux ratio of nitrification liquid is 100～300%；
(5), rear-mounted denitrification processes: deliver in rear-mounted denitrification pond, outside adding in rear-mounted denitrification pond by the water outlet in degassing pond
Carrying out carbon source, carry out anti-nitration reaction to remaining nitrate nitrogen in waste water and be converted into nitrogen, sludge concentration is 15～30g/L, dissolved oxygen
Concentration≤0.5mg/L, the water outlet of rear-mounted denitrification delivers to intermediate pool and precipitates, and the supernatant of intermediate pool delivers to external ultrafiltration
Device, the mud of bottom send sludge dewatering system, and the waterpower of intermediate pool stays the time to be 3～5h, the sludge concentration of intermediate pool 15～
30g/L；
(6), hyperfiltration treatment: the water outlet of intermediate pool is delivered in external ultrafilter, by the membrane module of external ultrafilter to mud
Aqueous mixtures carries out solid-liquid separation, and clear liquid sends into reverse osmosis membrane assembly or nanofiltration membrane component, and sludge reflux is to forward type nitrification tank
In；
(7), reverse osmosis or nanofiltration device process: clear liquid after ultrafiltration is sent into reverse osmosis membrane assembly or nanofiltration membrane component, passes through reverse osmosis
Organic pollution in clear liquid and salinity are retained by membrane module or nanofiltration membrane component, and the concentrated solution after process send at concentrated solution
Reason system, output Treated sewage reusing or qualified discharge.
Coking waste water treatment method based on jet biochemical reactor the most according to claim 1, it is characterised in that: described
Mud is separated by sludge dewatering system, and clear liquid is back in air floatation machine, dry mud landfill after dehydration.
Coking waste water treatment method based on jet biochemical reactor the most according to claim 1, it is characterised in that: described
During air supporting pretreatment, adding dosing coagulant and flocculant to air floatation machine, by mass percentage, the addition of coagulant is coking
The 0.001～0.01% of waste water total amount, the addition of flocculant is the 0.005～0.015% of coking chemical waste water total amount.
Coking waste water treatment method based on jet biochemical reactor the most according to claim 1, it is characterised in that: described
During Prepositive denitrification processes, denitrification rate is at 0.09～0.12kg NO3-N/kg VS.d, denitrification load 0.9～
1.2kg NO3-N/m3.d。
Coking waste water treatment method based on jet biochemical reactor the most according to claim 1, it is characterised in that: described
During rear-mounted denitrification processes, rear-mounted denitrification speed is at 0.12～0.2kg NO3-N/kg VS.d, rear-mounted denitrification load exists
1.2～1.5kg NO3-N/m3.d。
Coking waste water treatment method based on jet biochemical reactor the most according to claim 1, it is characterised in that: described
One-level biochemical reactor and secondary biochemical reactor are injection circulation biochemical reactor, and pump flow is that flow of inlet water is 300
～1000%, nozzle instantaneous velocity is 40～50m/s, the COD volumetric loading >=16kg COD/m of one-level biochemical reactor3.d,
Secondary biochemical reactor ammonia nitrogen volumetric loading is 1.2～1.5kg NH4-N/m3.d。
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| CN109179874A (en) * | 2018-09-21 | 2019-01-11 | 宝钢化工湛江有限公司 | Fenton oxidation combination constructed wetland plant handles coking wastewater technique |
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| CN112174441A (en) * | 2020-10-21 | 2021-01-05 | 南京江岛环境科技研究院有限公司 | System and method for treating and recycling machining wastewater by using air flotation pretreatment, biochemistry and double-membrane method |
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