CN205874139U - Coking wastewater treatment system - Google Patents
Coking wastewater treatment system Download PDFInfo
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- CN205874139U CN205874139U CN201620685838.3U CN201620685838U CN205874139U CN 205874139 U CN205874139 U CN 205874139U CN 201620685838 U CN201620685838 U CN 201620685838U CN 205874139 U CN205874139 U CN 205874139U
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- 238000004939 coking Methods 0.000 title claims abstract description 150
- 238000004065 wastewater treatment Methods 0.000 title abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 182
- 238000011282 treatment Methods 0.000 claims abstract description 87
- 239000002351 wastewater Substances 0.000 claims abstract description 45
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 24
- 231100000719 pollutant Toxicity 0.000 claims abstract description 24
- 239000010802 sludge Substances 0.000 claims abstract description 20
- 238000005273 aeration Methods 0.000 claims abstract description 15
- 230000003197 catalytic effect Effects 0.000 claims abstract description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000001301 oxygen Substances 0.000 claims abstract description 4
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 4
- 239000002894 chemical waste Substances 0.000 claims description 105
- 238000006243 chemical reaction Methods 0.000 claims description 53
- 238000005345 coagulation Methods 0.000 claims description 32
- 230000015271 coagulation Effects 0.000 claims description 32
- 238000000034 method Methods 0.000 claims description 27
- 230000008569 process Effects 0.000 claims description 27
- 239000010865 sewage Substances 0.000 claims description 27
- 238000006555 catalytic reaction Methods 0.000 claims description 18
- 239000000463 material Substances 0.000 claims description 18
- 230000001112 coagulating effect Effects 0.000 claims description 17
- 230000001105 regulatory effect Effects 0.000 claims description 17
- 230000003139 buffering effect Effects 0.000 claims description 13
- 238000005188 flotation Methods 0.000 claims description 13
- 238000006385 ozonation reaction Methods 0.000 claims description 13
- 238000001556 precipitation Methods 0.000 claims description 12
- 230000033228 biological regulation Effects 0.000 claims description 10
- 230000008859 change Effects 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 8
- 239000002699 waste material Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 5
- 239000002893 slag Substances 0.000 claims description 5
- 230000036284 oxygen consumption Effects 0.000 claims description 4
- 239000002244 precipitate Substances 0.000 claims description 4
- 239000000725 suspension Substances 0.000 claims description 3
- 239000000126 substance Substances 0.000 abstract description 15
- 230000003647 oxidation Effects 0.000 abstract description 7
- 238000007254 oxidation reaction Methods 0.000 abstract description 7
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 3
- 238000011221 initial treatment Methods 0.000 abstract 2
- 230000000694 effects Effects 0.000 description 10
- 239000000706 filtrate Substances 0.000 description 9
- 238000004080 punching Methods 0.000 description 6
- 239000000571 coke Substances 0.000 description 5
- 238000007599 discharging Methods 0.000 description 5
- 238000009826 distribution Methods 0.000 description 4
- 239000003814 drug Substances 0.000 description 4
- 230000000813 microbial effect Effects 0.000 description 4
- 238000005276 aerator Methods 0.000 description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 238000011001 backwashing Methods 0.000 description 3
- 230000003851 biochemical process Effects 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000004060 metabolic process Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 231100000611 venom Toxicity 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 1
- 241000976983 Anoxia Species 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000007953 anoxia Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
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- 230000003467 diminishing effect Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000004299 exfoliation Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
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- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
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- 230000020477 pH reduction Effects 0.000 description 1
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- 238000010926 purge Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000003252 repetitive effect Effects 0.000 description 1
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- 239000010117 shenhua Substances 0.000 description 1
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- 229910052719 titanium Inorganic materials 0.000 description 1
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- 231100000331 toxic Toxicity 0.000 description 1
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- 239000003403 water pollutant Substances 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The utility model discloses a coking wastewater treatment system, include: the primary treatment section for carry out the preliminary treatment in order to detach oil pollutant wherein to coking wastewater, the secondary treatment section is used for coming from the coking wastewater of primary treatment section carries out biochemical treatment in order to detach bad news oxygen pollutant wherein, for example COD organic pollutant, BOD organic pollutant etc, the tertiary treatment section is used for coming from the coking wastewater of secondary treatment section carries out ozone catalytic oxidation and MBAF aeration biochemical treatment, the sludge treatment section is used for coming from the mud of secondary treatment section and tertiary treatment section is handled. The utility model discloses a coking wastewater treatment system under the less condition of economic input, can carry out efficient handling to the polluting substances among the coking wastewater, guarantees out that water reaches national emission standard.
Description
Technical field
This utility model belongs to field of waste water treatment, particularly to a kind of coking wastewater processing system.
Background technology
Coking one Chang Shi China Shenhua Energy Co., Ltd. is produced as main subsidiary factory with coking, is positioned at Inner Mongol E Er
Meng Xi industrial park, Duo Si city, floor space is 300,000 square metres.700000 tons/year of stamp-charging coke projects started to raise in October, 2002
Building, coke oven type of furnace TJL4350D type side-arranged tamping coke oven, a coke oven goes into operation in October, 2002, is completed in October, 2003 and throws
Produce；No. two coke ovens go into operation in August, 2003, and in October, 2004 goes into operation, and safety in production at present is stable normal.Solve coked waste water at present
Pollution problem has two Basic Ways: one is innovation production technology, strengthens operational management, reduces the sewage water yield, and repetitive cycling is used
Water, is inherently eliminated and discharges with pollution abatement thing；Two is coked waste water to be carried out process reach emission request.The most at present
For, pollutant emission is completely eliminated by coking production technological innovation and also can not reach, and existing sewage disposal system includes
Coagulation section, two stage treatment section and Treatment of Sludge section, coagulation section includes grid and sewage lifting pump sump, oil interceptor, tune
Joint pond, accident pool, flotation tank, oil-collecting collection slag bath, coagulation section as pretreatment for removing the oiliness such as tar in sewage
Pollutant, equalize water quality and quantity；Two stage treatment section includes AO biochemistry pool (that is, Prepositive denitrification pond) and second pond, is used for removing
COD organic dirt matter in sewage and NH3-N polluter (that is, ammonia and nitrogen pollution material), Treatment of Sludge section includes sludge condensation
Pond and dewaterer, for processing the mud produced in sewage disposal.Owing to existing sewage disposal system can not effectively process it
In hardly degraded organic substance and after processing water quality often colourity high, therefore along with continuous to coking sewage drainage standard of country
Improving, the sewage after existing sewage disposal system processes can not reach discharging standards.
Utility model content
The purpose of this utility model is to provide a kind of coking wastewater processing system, and this coking wastewater processing system can be focused
Change waste water and carry out overall synthetic improvement, make the water outlet after process reach discharging standards.
The technical solution of the utility model is as follows:
A kind of coking wastewater processing system, including:
Coagulation section: for coking chemical waste water is carried out pretreatment to remove oiliness pollutant therein；
Two stage treatment section: therein to remove for the coking chemical waste water from described coagulation section being carried out biochemical treatment
Oxygen consumption pollutant；
Tertiary treatment stage: expose for the coking chemical waste water from described two stage treatment section being carried out catalytic ozonation and MBAF
Gas biochemical treatment；
Treatment of Sludge section: for the mud from described two stage treatment section and tertiary treatment stage is processed；
Described tertiary treatment stage includes:
Coagulation reaction tank: from the coking chemical waste water of described two stage treatment section and it is carried out coagulating for receiving；
Coagulative precipitation tank: from the coking chemical waste water of described coagulation reaction tank and precipitate for reception；
First intermediate pool: for receiving from the coking chemical waste water of described coagulative precipitation tank and it is carried out homogenizing all measuring tune
Joint；
Ozone catalytic reaction tank: for receiving ozone and the coking chemical waste water from described first intermediate pool, so that it to be entered
Row catalysis oxidation；
Second intermediate pool: for receiving from the coking chemical waste water of described ozone catalytic reaction tank and that it is carried out homogenizing is equal
Amount regulation；
MBAF reaction tank: from the coking chemical waste water of described second intermediate pool and it is located further for reception
Reason；
Discharge bay: for receiving from the coking chemical waste water of described MBAF reaction tank and by its reuse or discharge.
Preferably, described discharge bay to described MBAF reaction tank being provided with back wash line, being used for will be from described water outlet
The coking chemical waste water output in pond carries out backwash to described MBAF reaction tank.
Preferably, described tertiary treatment stage also includes backwash water regulating reservoir, described backwash water regulating reservoir for receive from
The backwash waste of described MBAF reaction tank, and output this to described coagulation reaction tank and be circulated.
Preferably, it is provided with in described ozone catalytic reaction tank:
Aeration plate: for described ozone catalytic reaction tank is carried out ozonation aerated；
Vent ozone destructor: be used for absorbing the remaining ozone of process.
Preferably, described MBAF reaction tank is arranged in advanced treating, is provided with MBAF reaction in described MBAF reaction tank
Device.
Preferably, described MBAF reactor includes buffering water distributing area, filter material layer and exhalant region；
Buffering water distributing area: be positioned at the bottom of described MBAF reactor, for receiving Jiao from described second intermediate pool
Change waste water；
Filter material layer: be positioned at the middle level of described MBAF reactor, for entering the coking chemical waste water from described buffering water distributing area
Row purified treatment；
Exhalant region: be positioned at the top layer of described MBAF reactor, and be provided with effluent trough, for by Jiao from described filter material layer
Change waste water to discharge.
Preferably, described filter material layer is provided with the gripper shoe for support filtrate, and described gripper shoe is provided with for being passed through
Gas or the filter of clear water, to carry out backwash to described MBAF reactor.
Preferably, described Treatment of Sludge section includes:
Sludge-tank: for receiving the mud from described coagulative precipitation tank；
Sludge concentration tank: for receiving from described two stage treatment section and the mud of described sludge-tank；
Dewaterer: from the mud of described sludge concentration tank and it is dehydrated for receiving, and discharges mud cake.
Preferably, described coagulation section includes:
Grid and sewage lifting pump sump: for processing the coking chemical waste water from foul water system to remove wherein
Float and floating thing, and be lifted into subsequent processing device；
Accident pool: for receiving the accident draining of other processing equipments；
Oil interceptor: for the coking chemical waste water from foul water system, from described grid and sewage lifting pump sump
Coking chemical waste water and the coking chemical waste water from accident pool carry out processing to remove oiliness pollutant therein；
Regulating reservoir: all measure regulation for the coking chemical waste water from oil interceptor is carried out homogenizing；
Flotation tank: for receive from described regulating reservoir coking chemical waste water and remove further oiliness pollutant therein with
Float；
Oil-collecting collection slag bath: for receiving the oiliness pollutant from described flotation tank and float.
Preferably, described two stage treatment section bag:
AO biochemistry pool: for receive from described flotation tank coking chemical waste water and remove COD organic pollution therein and
NH3-N polluter；
Second pond: for receiving the coking chemical waste water from described AO biochemistry pool, and it is carried out mud-water separation.
The beneficial effects of the utility model are:
(1) coking wastewater processing system of the present utility model, not only includes at coagulation section, two stage treatment section and mud
Reason section, also includes for the coking chemical waste water from two stage treatment section carries out what catalytic ozonation and MBAF aeration biochemical processed
Tertiary treatment stage, catalytic ozonation processes good decolorizing effect, there is not secondary pollution, and can the efficient oxidation at normal temperatures and pressures
The Organic substance (such as Nitrobenzol) of difficult degradation, is decomposed into degradable small organic molecule by larger molecular organics；And be aided with
After MBAF aeration biochemical process, can effectively remove the organic pollution materials in coking chemical waste water, it is ensured that water outlet reach country discharge
Standard；It also avoid simultaneously and be used alone catalytic ozonation when processing, added amount of chemical increases, problem that operating cost is high,
Advantageously reduce economic input；
(2) setting of each several part in tertiary treatment stage, it is ensured that on the basis of relatively small economy puts into, in coking chemical waste water
Pollutant be effectively treated, make water outlet reach discharging standards；
(3) setting of back wash line, available water outlet after treatment carries out backwash to MBAF reaction tank, it is to avoid clear water
Use, the beneficially recycling of water, reduce water consumption and use by water rate；
(4) setting of backwash water regulating reservoir, can receive the backwash waste in MBAF reaction tank, and be inputted coagulating
Pond is circulated；
(5) aeration plate and the setting of vent ozone destructor in ozone catalytic reaction tank, it is ensured that ozone is in coking chemical waste water
Organic pollution carry out fully oxidized while, prevent unnecessary ozone to be diffused in working environment and staff caused
Actual bodily harm；
(6) setting of regional in MBAF reactor, is conducive to carrying out the coking chemical waste water from the second intermediate pool
Effectively process, remove residual organic substances therein and ammonia nitrogen pollutant；Buffering water distributing area can make sewage uniformly flow into MBAF reaction
In device；
(7) setting of each several part in Treatment of Sludge section, the coagulation that can simultaneously process two stage treatment section and tertiary treatment stage sinks
Mud in pond, shallow lake, before coking chemical waste water enters tertiary treatment stage, the most first disposes a part of mud, alleviates tertiary treatment stage
Pressure；
(8) setting of each several part in coagulation section, can remove the float in coking chemical waste water and oiliness pollutant so that
Pretreatment to coking chemical waste water reaches preferable effect, provides convenient for subsequent treatment；
(9) setting of each several part in two stage treatment section, can remove COD, the NH in coking chemical waste water3The venomous injurants such as-N
Matter, the process of follow-up tertiary treatment stage.
Accompanying drawing explanation
Fig. 1 is coking wastewater processing system of the present utility model flow chart in one embodiment；
Fig. 2 is coking wastewater processing system of the present utility model flow chart in another embodiment.
Detailed description of the invention
Below by way of detailed description of the invention, this novel technical scheme and effect thereof are described further.Following embodiment party
Formula is merely to illustrate the content that this is novel, is not limited to this novel protection domain.This novel design of application is new to this
The simple change that type is carried out is all in this novel claimed scope.
Coking wastewater processing system of the present utility model, including:
Coagulation section: for coking chemical waste water is carried out pretreatment to remove oiliness pollutant therein, such as tar；
Two stage treatment section: therein to remove for the coking chemical waste water from described coagulation section being carried out biochemical treatment
Oxygen consumption pollutant, such as COD organic pollution, BOD organic pollution and NH3-N polluter etc.；
Tertiary treatment stage: expose for the coking chemical waste water from described two stage treatment section being carried out catalytic ozonation and MBAF
Gas biochemical treatment；
Treatment of Sludge section: for the mud from described two stage treatment section and tertiary treatment stage is processed.
Coking wastewater processing system of the present utility model, in the case of economic input is less, can be in coking chemical waste water
Polluter is effectively treated, it is ensured that water outlet reaches discharging standards.
In one embodiment, described tertiary treatment stage includes:
Coagulation reaction tank: from the coking chemical waste water of described two stage treatment section and it is carried out coagulating for receiving；
Coagulative precipitation tank: from the coking chemical waste water of described coagulation reaction tank and precipitate for reception；
First intermediate pool: for receiving from the coking chemical waste water of described coagulative precipitation tank and it is carried out homogenizing all measuring tune
Joint；
Ozone catalytic reaction tank: for receiving ozone and the coking chemical waste water from described first intermediate pool, so that it to be entered
Row catalysis oxidation, degrade Organic substance therein, such as volatile phenol；It is provided with activated-carbon catalyst in described ozone catalytic reaction tank；
Preferably there are 2 ozone catalytic reaction tanks；
Second intermediate pool: for receiving from the coking chemical waste water of described ozone catalytic reaction tank and that it is carried out homogenizing is equal
Amount regulation；
MBAF reaction tank: for receive from described second intermediate pool coking chemical waste water and remove residual Organic substance and
NH3-N polluter, and retain float；
Discharge bay: for receiving from the coking chemical waste water of described MBAF reaction tank and by its reuse or discharge.
At coking chemical waste water from two stage treatment section is carried out that catalytic ozonation and MBAF aeration biochemical process three grades
Reason section, catalytic ozonation processes good decolorizing effect, there is not secondary pollution, and can the efficient oxidation difficult degradation at normal temperatures and pressures
Organic substance (such as Nitrobenzol), larger molecular organics is decomposed into degradable small organic molecule；And be aided with subsequently
MBAF aeration biochemical processes, and can effectively remove the organic pollution materials in coking chemical waste water, it is ensured that water outlet reaches discharging standards；
It also avoid simultaneously and be used alone catalytic ozonation when processing, added amount of chemical increases, problem that operating cost is high, is conducive to
Reduce economic input.
MBAF reaction tank, i.e. modified form BAF, structure is as broad as long with tradition BAF (BAF),
Wherein the granularity of filtrate diminishes, traditional 15-20mm become 10mm so that the absorbability of filtrate strengthens；MBAF is anti-
Answer pond mainly by aerating system and the optimum organization of filtrate, improve aeration effect and treatment effect, the filtrate granularity of system
After diminishing, improving the disposal ability of waste water, treatment effect improves.
In a preferred embodiment, described MBAF reaction tank has 4, and 4 MBAF reaction tanks are set up in parallel.
In existing processing system, tradition BAF (BAF) has 3, in the processing system of the application, and MBAF
Reaction tank has 4, after process progression is promoted to 4 by 3, increases the treating capacity of waste water, and treatment effect is more preferable.
In one embodiment, described MBAF reaction tank is arranged in advanced treating, sets in described MBAF reaction tank
There is MBAF reactor.
It is room between advanced treating, it is contemplated that winter temperature is relatively low and MBAF reactor filtering velocity is relatively low, for ensureing at biochemical
Manage effect and prevent face, pond from freezing, MBAF reaction tank being located in advanced treating.
In one embodiment, described MBAF reactor includes buffering water distributing area, filter material layer and exhalant region；
Buffering water distributing area: be positioned at the bottom of described MBAF reactor, for receiving Jiao from described second intermediate pool
Change waste water；
Filter material layer: be positioned at the middle level of described MBAF reactor, for entering the coking chemical waste water from described buffering water distributing area
Row purified treatment；
Exhalant region: be positioned at the top layer of described MBAF reactor, and be provided with effluent trough, for by Jiao from described filter material layer
Change waste water to discharge.
Filter material layer fills efficient ceramic grain filter, and it is big that efficient ceramic grain filter has specific surface, and porosity is high, and retaining power is strong,
Filtering velocity is high, and service life is long, and backwash water consumption is few, is difficult to harden, not the advantage such as easy-weathering, and does not contains harmful thing
Matter.
Buffering water distributing area can make to flow uniformly through filter course from the coking chemical waste water of the second intermediate pool, and enters at coking chemical waste water
When entering filter course, carried out blast aeration by aerator simultaneously and in pond, supply the sky needed for microbial film metabolism by aerator
Gas (oxygen source), the microbial film being grown on filtrate draws solubility organic pollution as its physiological activity from coking chemical waste water
Required nutrient substance, decomposes organic pollution in metabolic process, makes coking chemical waste water be purified.
The setting of regional in MBAF reactor, is conducive to carrying out the coking chemical waste water from the second intermediate pool effectively
Process, remove residual organic substances therein and ammonia nitrogen pollutant；Buffering water distributing area can make sewage uniformly flow in MBAF reactor.
In one embodiment, described discharge bay to described MBAF reaction tank is provided with back wash line, in the future
Export extremely described MBAF reaction tank from the coking chemical waste water of described discharge bay and carry out backwash.
When MBAF reactor ran after certain time, owing to thickening coming off of microbial film on filtrate, can be with in water outlet
The microbial film of partial exfoliation, makes water outlet water degradation, now must close the water inlet pipe valve of MBAF reaction tank, starts backwash
Water pump also opens back wash line, utilizes deposit water outlet in discharge bay that the filter material layer of MBAF reactor is carried out backwash.
The setting of back wash line, available water outlet after treatment carries out backwash to MBAF reaction tank, it is to avoid clear water
Use, the beneficially recycling of water, reduce water consumption and use by water rate.
MBAF reactor is periodic duty, is a complete cycle from starting to be filled into backwash complete.Preprocessed
Sewage enter bottom filter tank, bottom filter tank, carry out aeration.In the reactor, Organic substance is decomposed by microbiological oxidation,
NH3-N is oxidized to NO3--N, additionally, due to there is anaerobism/oxygen environment of holding concurrently, achievement unit while nitrification in biomembranous inside
Divide denitrification.
Along with the carrying out filtered, the Biomass newly generated due to filling surface gets more and more, and the SS retained is continuously increased,
The incipient stage loss of flood peak increases slowly, when solid matter accumulation reaches to a certain degree, blocks filtering layer, and stops releasing of bubble
Put, it will cause the loss of flood peak to quickly reach the limit, now enter backwash regeneration, with remove excess in filter bed biomembrane and
SS, recovers disposal ability.Wherein, the loss of flood peak refer to the water of Unit Weight or other liquid in flow process because overcoming current
Resistance work done and the mechanical energy lost.
In one embodiment, described filter material layer is provided with the gripper shoe for support filtrate, and described gripper shoe is arranged
There is the filter for being passed through gas or clear water, so that described MBAF reactor is carried out backwash.
Backwash uses air-water associating backwash.For ensureing water distribution, uniform air distribution, filtrate gripper shoe is evenly arranged
There are the special water distribution of MBAF reactor or the filter of distribution.MBAF reactor backwash cycle 24h, can react according to water quality and MBAF
Pond situation is adjusted.During MBAF reactor backwash, MBAF reaction tank stops water inlet, opens backwash tube valve, finally opens
Open backwashing pump；Backwash uses first gas punching, the then mixed punching of air water, and the order of last water punching, air purge intensity is about 10-15L/
m2S, washing intensity is 4-6L/m2S, washes intensity and keeps constant in whole backwash process.Gas punching, the mixed punching of air water and water
The time of punching should find most economical combination according to influent quality on the premise of ensureing effluent quality.After backwash terminates, first close
Closing backwashing pump, be then shut off back flush valves, MBAF reaction tank is intake again.The instantaneous displacement of backwash waste is very big, from
Stream is emitted into backwash water regulating reservoir, boosted enters coagulation reaction tank circulation with stable low discharge.
In one embodiment, described tertiary treatment stage also includes backwash water regulating reservoir, and described backwash water regulating reservoir is used
In receiving from the backwash waste of described MBAF reaction tank, and output this to described coagulation reaction tank and be circulated.
Owing to the instantaneous backwash waste amount of MBAF reaction tank is relatively big, the setting of backwash water regulating reservoir, can reduce drain pipe
Road and the impact of structures.
In one embodiment, it is provided with in described ozone catalytic reaction tank:
Aeration plate: for described ozone catalytic reaction tank is carried out ozonation aerated；Preferably aeration plate is micropore pure titanium aeration
Dish.
Vent ozone destructor: be used for absorbing the remaining ozone of process.
The concrete setting of ozone catalytic reaction tank, it is ensured that the organic pollution in coking chemical waste water is carried out fully by ozone
While oxidation, prevent unnecessary ozone to be diffused in working environment and staff is caused actual bodily harm.
In one embodiment, described Treatment of Sludge section includes:
Sludge-tank: for receiving the mud from described coagulative precipitation tank；
Sludge concentration tank: for receiving from described two stage treatment section and the mud of described sludge-tank；
Dewaterer: from the mud of described sludge concentration tank and it is dehydrated for receiving, and discharges mud cake.
The concrete setting of Treatment of Sludge section, can process in the coagulative precipitation tank of two stage treatment section and tertiary treatment stage simultaneously
Mud, before coking chemical waste water enters tertiary treatment stage, the most first disposes a part of mud, alleviates the pressure of tertiary treatment stage.
In one embodiment, described coagulation section includes:
Grid and sewage lifting pump sump: for the coking chemical waste water of input (without pressure sewage) is processed to remove therein
Float and floating thing, and it is lifted into subsequent processing device；Wherein, refer to give up by the coking of gravity input without pressure sewage
Water；
Accident pool: for receiving the accident draining of other processing equipments；
Oil interceptor: for the coking chemical waste water (having pressure sewage) to input, from described grid and Jiao of sewage lifting pump sump
Change waste water and the coking chemical waste water from accident pool carries out processing to remove the oiliness pollutant such as tar therein；Wherein, there is pressure dirt
Water refers to be promoted the coking chemical waste water of input by elevator pump；
Regulating reservoir: all measure regulation for the coking chemical waste water from oil interceptor is carried out homogenizing；
Flotation tank: from the coking chemical waste water of described regulating reservoir and remove oil slick therein and suspension further for reception
Thing；Medicament quickening can be added during air supporting process；
Oil-collecting collection slag bath: for receiving the oil slick from described flotation tank and float.
Coagulation section as pretreatment for removing oiliness pollutant and the float such as tar in sewage.
In one embodiment, described two stage treatment section includes AO biochemistry pool and second pond；
AO biochemistry pool: for receive from described flotation tank coking chemical waste water and remove COD organic pollution therein and
NH3-N polluter, wherein, NH3-N polluter utilizes nitrification and anti-digestion reaction to remove；
Second pond: for receiving the coking chemical waste water from described AO biochemistry pool, and it is carried out mud-water separation.
COD, NH in coking chemical waste water3The poisonous and harmful substance content such as-N are higher, effect toxic to microorganism, have a strong impact on
The growth of microorganism, causes biochemical system to be not normally functioning, and therefore must control to enter the venomous injurant in biochemistry pool sewage
The concentration of matter.
In AO biochemistry pool, A section is anoxia section, before being positioned at O section, mainly utilizes the denitrifying bacterium in pond, mixing backflow
Close the NO in liquid3 -And NO2 -It is transformed into N2, hydrolysis acidification remove the part carbonaceous organic material in water inlet simultaneously；O section is aerobic
Section, uses micro-hole aerator as oxygenation means, is substantially carried out the degraded of nitration reaction and carbonaceous organic material.
Coking wastewater processing system of the present utility model work process in one embodiment is as shown in Figure 1:
Coking chemical waste water input coagulation section carries out pretreatment to remove the oiliness pollutant such as tar therein；From one-level
The coking chemical waste water input two stage treatment section of processing section carries out biochemical treatment to remove COD organic pollution therein, the organic dirt of BOD
The oxygen consumption pollutant such as dye thing；Coking chemical waste water from two stage treatment section inputs in coagulation reaction tank and precipitates, and period adds mixed
Solidifying medicament, to remove the Organic substance in coking chemical waste water and float；Coking chemical waste water from coagulation reaction tank inputs coagulating sedimentation
Pond is precipitated；Coking chemical waste water from coagulative precipitation tank inputs the first intermediate pool to carry out homogenizing and all measures regulation；From
The coking chemical waste water input ozone catalytic reaction tank of one intermediate pool carries out catalytic ozonation reaction, has removing COD therein
Organic pollutants matter, and macromole hardly degraded organic substance therein is decomposed into little molecule easily biodegradable organics；From ozone catalytic
The coking chemical waste water of reaction tank inputs the second intermediate pool to carry out homogenizing and all measures regulation；Defeated from the coking chemical waste water of the second intermediate pool
Enter MBAF reaction tank and carry out biochemical reaction to remove wherein remaining small organic molecule；Coking chemical waste water from MBAF reaction tank
Input discharge bay storage, for reuse or discharge；Mud from coagulative precipitation tank inputs sludge-tank；From two stage treatment section and
The mud input sludge concentration tank of sludge-tank concentrates, and inputs dewaterer and be dehydrated, and can add medicament and accelerate dehydration (medicine
Mud floc sedimentation can be contributed to mud-water separation by agent), mud cake is transported outward；Between when the system is operated longer time, start backwash to MBAF
Reaction tank carries out backwash, backwashing water input backwash water regulating reservoir, and circulates output in coagulation reaction tank.
Coking wastewater processing system of the present utility model work process in another embodiment is as shown in Figure 2:
Coking chemical waste water input coagulation section carries out pretreatment, through grid after first coking chemical waste water (without pressure sewage) inputs
Process to remove float therein, after through sewage pump well promote input oil interceptor in remove oiliness therein pollution
Thing, meanwhile, coking chemical waste water (having pressure sewage) inputs and also removes oiliness pollutant therein in oil interceptor；Accident pool is used for receiving it
The accident draining of his processing equipment, and be inputted oil interceptor and process；Coking chemical waste water from oil interceptor inputs regulation
Pond carries out homogenizing and all measures regulation；Coking chemical waste water from regulating reservoir inputs flotation tank to remove oil slick therein and suspension further
Thing；Oil slick and float input oil-collecting collection slag bath from flotation tank are collected and transport outward；Coking chemical waste water from flotation tank
The AO biochemistry pool of input two stage treatment section carries out processing to remove COD organic pollution therein and NH3-N polluter；From
The coking chemical waste water input second pond of described AO biochemistry pool carries out mud-water separation；Mud from second pond inputs Treatment of Sludge section
Sludge concentration tank process, from second pond coking chemical waste water input tertiary treatment stage coagulation reaction tank process；
Subsequent process is as the work process of system shown in Figure 1.
Utilize intrinsic coking wastewater processing system and coking wastewater processing system of the present utility model to coking chemical waste water
Result be compared as follows:
When utilizing intrinsic coking wastewater processing system that coking chemical waste water is processed, the coking chemical waste water test of import and export
Result is as shown in table 1；
Table 1 utilizes the coking chemical waste water test result that intrinsic coking wastewater processing system is imported and exported
When utilizing coking wastewater processing system of the present utility model that coking chemical waste water is processed, import and each several part water outlet
Coking chemical waste water test result as shown in table 2；
Table 2 utilizes the coking chemical waste water test result that coking wastewater processing system of the present utility model is imported and exported
From the comparison of Tables 1 and 2, coking wastewater processing system of the present utility model, relative to original design, can be effective
Treatment of Wastewater in Coking, reduces the pH of coking chemical waste water water outlet, COD, float, volatile phenol and ammonia nitrogen, makes the every of water outlet
Index reaches the discharge standard of even better than country.
Claims (10)
1. a coking wastewater processing system, it is characterised in that including:
Coagulation section: for coking chemical waste water is carried out pretreatment to remove oiliness pollutant therein；
Two stage treatment section: for the coking chemical waste water from described coagulation section is carried out biochemical treatment to remove oxygen consumption therein
Pollutant；
Tertiary treatment stage: raw for the coking chemical waste water from described two stage treatment section being carried out catalytic ozonation and MBAF aeration
Change processes；
Treatment of Sludge section: for the mud from described two stage treatment section and tertiary treatment stage is processed；
Described tertiary treatment stage includes:
Coagulation reaction tank: from the coking chemical waste water of described two stage treatment section and it is carried out coagulating for receiving；
Coagulative precipitation tank: from the coking chemical waste water of described coagulation reaction tank and precipitate for reception；
First intermediate pool: for receiving from the coking chemical waste water of described coagulative precipitation tank and it is carried out homogenizing all measuring regulation；
Ozone catalytic reaction tank: for receiving ozone and carrying out the coking chemical waste water from described first intermediate pool being catalyzed oxygen
Change；
Second intermediate pool: for receiving from the coking chemical waste water of described ozone catalytic reaction tank and it is carried out homogenizing all measuring tune
Joint and buffering；
MBAF reaction tank: from the coking chemical waste water of described second intermediate pool and it is carried out biochemical treatment for receiving；
Discharge bay: for receiving from the coking chemical waste water of described MBAF reaction tank and by its reuse or discharge.
Coking wastewater processing system the most according to claim 1, it is characterised in that anti-from described discharge bay to described MBAF
Ying Chi is provided with back wash line, carries out instead for the coking chemical waste water from described discharge bay is exported extremely described MBAF reaction tank
Wash.
Coking wastewater processing system the most according to claim 2, it is characterised in that described tertiary treatment stage also includes backwash
Water regulating reservoir, described backwash water regulating reservoir is for receiving the backwash waste from described MBAF reaction tank, and outputs this to institute
State coagulation reaction tank to be circulated.
4. according to the coking wastewater processing system described in any one of claim 1-3, it is characterised in that described ozone catalytic is reacted
It is provided with in pond:
Aeration plate: for described ozone catalytic reaction tank is carried out ozonation aerated；
Vent ozone destructor: be used for absorbing the remaining ozone of process.
5. according to the coking wastewater processing system described in any one of claim 1-3, it is characterised in that described MBAF reaction tank sets
It is placed in advanced treating, in described MBAF reaction tank, is provided with MBAF reactor.
Coking wastewater processing system the most according to claim 5, it is characterised in that described MBAF reactor includes that buffering is joined
Pool, filter material layer and exhalant region；
Buffering water distributing area: be positioned at the bottom of described MBAF reactor, gives up for receiving the coking from described second intermediate pool
Water；
Filter material layer: be positioned at the middle level of described MBAF reactor, for carrying out the coking chemical waste water from described buffering water distributing area only
Change processes；
Exhalant region: be positioned at the top layer of described MBAF reactor, and be provided with effluent trough, for giving up from the coking of described filter material layer
Water is discharged.
Coking wastewater processing system the most according to claim 6, it is characterised in that described filter material layer is provided with to be filtered for support
The gripper shoe of material, described gripper shoe is provided with the filter for being passed through gas or clear water, to carry out described MBAF reactor
Backwash.
8. according to the coking wastewater processing system described in claim 1-3 or any one of 6-7, it is characterised in that at described mud
Reason section includes:
Sludge-tank: for receiving the mud from described coagulative precipitation tank；
Sludge concentration tank: for receiving from described two stage treatment section and the mud of described sludge-tank；
Dewaterer: from the mud of described sludge concentration tank and it is dehydrated for receiving, and discharges mud cake.
Coking wastewater processing system the most according to claim 8, it is characterised in that described coagulation section includes:
Grid and sewage lifting pump sump: be used for processing the coking chemical waste water from foul water system to remove therein hanging
Float and floating thing, and it is lifted into subsequent processing device；
Accident pool: for receiving the accident draining of other processing equipments；
Oil interceptor: for the coking chemical waste water from foul water system, from described grid and the coking of sewage lifting pump sump
Waste water and the coking chemical waste water from accident pool carry out processing to remove oiliness pollutant therein；
Regulating reservoir: all measure regulation for the coking chemical waste water from oil interceptor is carried out homogenizing；
Flotation tank: from the coking chemical waste water of described regulating reservoir and remove oiliness pollutant therein and suspension further for reception
Thing；
Oil-collecting collection slag bath: for receiving the oiliness pollutant from described flotation tank and float.
Coking wastewater processing system the most according to claim 9, it is characterised in that described two stage treatment section bag:
AO biochemistry pool: from the coking chemical waste water of described flotation tank and remove COD organic pollution therein and NH for reception3-N
Polluter；
Second pond: for receiving the coking chemical waste water from described AO biochemistry pool, and it is carried out mud-water separation.
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| CN201620685838.3U CN205874139U (en) | 2016-06-30 | 2016-06-30 | Coking wastewater treatment system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107879461A (en) * | 2017-11-01 | 2018-04-06 | 北京化工大学 | A kind of processing unit of coking chemical waste water and the processing method of coking chemical waste water |
| CN108083583A (en) * | 2017-12-29 | 2018-05-29 | 桑德生态科技有限公司 | A kind of difficult degradation coking wastewater deep treatment puies forward mark system and method |
| CN114477626A (en) * | 2021-12-31 | 2022-05-13 | 新兴铸管股份有限公司 | Coking wastewater treatment system |
-
2016
- 2016-06-30 CN CN201620685838.3U patent/CN205874139U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107879461A (en) * | 2017-11-01 | 2018-04-06 | 北京化工大学 | A kind of processing unit of coking chemical waste water and the processing method of coking chemical waste water |
| CN108083583A (en) * | 2017-12-29 | 2018-05-29 | 桑德生态科技有限公司 | A kind of difficult degradation coking wastewater deep treatment puies forward mark system and method |
| CN114477626A (en) * | 2021-12-31 | 2022-05-13 | 新兴铸管股份有限公司 | Coking wastewater treatment system |
| CN114477626B (en) * | 2021-12-31 | 2023-10-27 | 新兴铸管股份有限公司 | Coking wastewater treatment system |
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