CN107673549A - Processing unit up to standard for high-concentration phenolic wastewater - Google Patents

Processing unit up to standard for high-concentration phenolic wastewater Download PDF

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Publication number
CN107673549A
CN107673549A CN201610616110.XA CN201610616110A CN107673549A CN 107673549 A CN107673549 A CN 107673549A CN 201610616110 A CN201610616110 A CN 201610616110A CN 107673549 A CN107673549 A CN 107673549A
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CN
China
Prior art keywords
parts
baf ponds
catalysis oxidation
oxidation pond
clear water
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Pending
Application number
CN201610616110.XA
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Chinese (zh)
Inventor
吕佩嵘
凌二锁
吴盼盼
徐知雄
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ZHONGHAI ASPHALT (TAIZHOU) CO Ltd
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ZHONGHAI ASPHALT (TAIZHOU) CO Ltd
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Priority to CN201610616110.XA priority Critical patent/CN107673549A/en
Publication of CN107673549A publication Critical patent/CN107673549A/en
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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
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
    • 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
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • C02F2101/345—Phenols
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C02F2201/007—Modular design
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems

Abstract

The present invention discloses a kind of processing unit up to standard for high-concentration phenolic wastewater, its catalysis oxidation pond, oxidation-stabilized pond, rear biochemical BAF ponds pass sequentially through back segment transfer conduit with clear water reserviors and connected, and the discharge bay is connected to inside catalysis oxidation pond with catalysis oxidation pond by inlet channel；One ozone generator is connected to inside catalysis oxidation pond by gas pipeline, the clear water reserviors are provided with inlet opening, apopore, the inlet opening of the clear water reserviors is connected with rear biochemical BAF ponds by back segment transfer conduit, the clear water reserviors are connected to a backwashing pump one end, and the carrier is made up of the component of following parts by weight：High density polyethylene (HDPE), acrylic resin, white lime, Tao Shi Powdered Activated Carbons, precipitated calcium carbonate, maleic anhydride, cumyl peroxide, gelatin, chitin, magnetic.The present invention can prevent the microbial film that carrier outer surface adheres to from being come off because being rubbed between carrier in water, short the time required to biofilm, improve waste water treatment efficiency.

Description

Processing unit up to standard for high-concentration phenolic wastewater
Technical field
The present invention relates to a kind of processing unit up to standard for high-concentration phenolic wastewater, belong to technical field of waste water processing.
Background technology
The processing method for being presently used for phenol wastewater mainly has extraction, absorption method, chemical oxidization method, biochemical treatment process Deng.Extraction high energy consumption, extractant easily occurs and residues in follow-up waste water, influences follow-up processing procedure；Absorption method operation letter It is single, it is suitable for the relatively low waste water of amount containing phenol, but equipment one-time investment is larger, and adsorbent reactivation is difficult；Though chemical method energy Oxidation removes phenol, but direct oxidation operating cost is higher.
The content of the invention
It is an object of the present invention to provide a kind of processing unit up to standard for high-concentration phenolic wastewater, and this is used for high concentration and contains phenol The processing unit operating cost up to standard of waste water is low, simple to operate, stable, and obtains the mesh of efficient degradation organic pollution , the high saline sewage advanced treating of petroleum chemical industry and qualified discharge under low cost can be achieved.
To reach above-mentioned purpose, the technical solution adopted by the present invention is：A kind of place up to standard for high-concentration phenolic wastewater Device is managed, the handling process be based on a special processor, and the special processor includes catalysis oxidation pond, oxidation-stabilized Pond, rear biochemical BAF ponds, clear water reserviors, the comprehensive tank of dilution, pretreated primary BAF ponds, pretreatment two level BAF ponds and discharge bay, it is described The comprehensive tank of dilution, pretreated primary BAF ponds, pretreatment two level BAF ponds pass sequentially through leading portion transfer conduit with discharge bay and connected, institute State catalysis oxidation pond, oxidation-stabilized pond, rear biochemical BAF ponds pass sequentially through back segment transfer conduit with clear water reserviors and connected, the water outlet Pond is connected to inside catalysis oxidation pond with catalysis oxidation pond by inlet channel；
One ozone generator is connected to inside catalysis oxidation pond by gas pipeline, and the clear water reserviors are provided with inlet opening, water outlet Hole, the inlet opening of the clear water reserviors are connected with rear biochemical BAF ponds by back segment transfer conduit, and the clear water reserviors are connected to a backwash Pump one end, this backwashing pump other end is connected to catalysis oxidation pond, inside rear biochemical BAF ponds by back segment reflux line, described to urge Change oxidation pond and ozone catalytic particle is filled with fixed bed form, the comprehensive tank of dilution is provided with charge door and agitator；
The ozone catalytic particle is made up of the component of following parts by weight：
Particle diameter is 2 ~ 4mm 88.7 ~ 91.3 parts of activated alumina particle,
1.2 ~ 1.5 parts of cupric oxide,
4 ~ 7 parts of polyethylene glycol,
1.5 ~ 2 parts of polyvinyl alcohol,
0.8 ~ 1 part of titanium dioxide,
0.3 ~ 0.5 part of hydroxypropyl cellulose,
0.2 ~ 0.4 part of manganese dioxide；
By 88.7 ~ 91.3 parts of the activated alumina particle and 1.2 ~ 1.5 parts of cupric oxide, polyethylene glycol 4 ~ 7 that the particle diameter is 2 ~ 4mm Part, 1.5 ~ 2 parts of polyvinyl alcohol, 0.8 ~ 1 part of titanium dioxide, 0.3 ~ 0.5 part of hydroxypropyl cellulose, 0.2 ~ 0.4 part of manganese dioxide exist Mixed in stirring mixer so that uniform mixed 1.2 ~ 1.5 parts of cupric oxide, 4 ~ 7 parts of polyethylene glycol, polyvinyl alcohol 1.5 ~ 2 Part, 0.8 ~ 1 part of titanium dioxide, 0.3 ~ 0.5 part of hydroxypropyl cellulose, 0.2 ~ 0.4 part of manganese dioxide are covered in the active oxidation Alumina particles surface forms catalyst mother bulb；Catalyst mother bulb is dried successively again, is calcined the acquisition loaded catalyst；
Several biologic packing materials are placed with biochemical BAF ponds after described, the biologic packing material is overlying on carrier surface by carrier and extension Microbial film composition；
The carrier is made up of the component of following parts by weight：
65 ~ 75 parts of high density polyethylene (HDPE),
10 ~ 15 parts of acrylic resin,
6 ~ 8 parts of low density polyethylene (LDPE),
5 ~ 15 parts of white lime,
5 ~ 20 parts of Tao Shi Powdered Activated Carbons,
6 ~ 10 parts of precipitated calcium carbonate,
3 ~ 5 parts of maleic anhydride,
0.2 ~ 0.6 part of cumyl peroxide,
1.5 ~ 3 parts of gelatin,
1 ~ 2 part of chitin,
0.5 ~ 2 part of magnetic,
0.5 ~ 1 part of pentaerythritol stearate.
Further improved technical scheme is as follows in above-mentioned technical proposal：
Preferably, the backwash sedimentation basin, leading portion supernatant liquid pool and pretreatment backwashing pump, the backwash that also include being sequentially connected sink Shallow lake pond is connected to pretreated primary BAF ponds, pretreatment two level BAF ponds, the pretreatment backwash by the first pipeline, second pipe Pump is connected to pretreated primary BAF ponds, pretreatment two level BAF ponds by leading portion reflux line.
Preferably, the ozone generator is connected to the bottom in catalysis oxidation pond by gas pipeline.
Preferably, drying time is 4 ~ 6 hours under the conditions of 100 ~ 120 DEG C in the step 3.
Preferably, roasting time is 7 ~ 9 hours under the conditions of 350 ~ 520 DEG C in the step 4.
Because above-mentioned technical proposal is used, the present invention has following advantages and effect compared with prior art：
1st, the present invention is used for the processing unit up to standard of high-concentration phenolic wastewater, and its catalytic ozonation technology compares other chemical oxygens Change method, reaction rate is rapid, the hydroxyl radical free radical of a large amount of active non-selectivities of generation, the multiple pollutant in oxidized waste water, The biodegradability of waste water is improved, oxidation water outlet enters interior circulation BAF, made in the filtering of biological bed, bioflocculation and biological adsorption Under, the material such as organic matter contained in waste water is further adsorbed oxidation, and it is low that this method effectively combines biochemical treatment cost The advantages of honest and clean and advanced oxidation high efficiency, improve the feasibility of phenol wastewater processing up to standard；Secondly, improve to oil The tolerance of the high saline sewage of work so that in the catalytic oxidation treatment process to saline sewage, catalyst ozone produces Active hydroxyl radical free radical, removal, decolouring to waste water COD, de- stench, degraded toxic pollutant and improves giving birth to for waste water The property changed keeps good effect.
2nd, the present invention is used for the processing unit up to standard of high-concentration phenolic wastewater, and macromolecular hardly degraded organic substance is oxidized to by it The easily biochemical organic matter of small molecule, and then improved the biochemical of water outlet, then by rear biochemical interior circulation BAF systems in water Organic matter carry out mineralising, final outflow water is less than 30mg/L, embodies economy, the high efficiency of the group technology.
3rd, the present invention is used for the processing unit up to standard of high-concentration phenolic wastewater, thereafter carrier biofilm speed in biochemical BAF ponds It hurry up, difficult for drop-off, treatment effeciency is high, the processing of low-concentration organic and ammonia nitrogen suitable for sewage, low-concentration organic waste water, this The biologic packing material of invention has extremely strong hydrophily and bioaffinity, and filler has very strong absorption strong biomembrane in itself Degree, is advantageous to the retention and accumulation of biomass on filling carrier, its ammonia nitrogen removal frank more than 92%, COD clearances more than 78%, because This can well adapt to the wastewater treatment under low consistency conditions.
4th, the present invention be used for high-concentration phenolic wastewater processing unit up to standard, thereafter in biochemical BAF ponds carrier in high density Further added in 65 ~ 75 parts of polyethylene, 10 ~ 15 parts of acrylic resin, 6 ~ 10 parts of precipitated calcium carbonate, 3 ~ 5 parts of maleic anhydride 0.5 ~ 2 part of 0.2 ~ 0.6 part of diisopropylbenzene (DIPB), 1.5 ~ 3 parts of gelatin and magnetic are aoxidized, filler is not only improved and carries compared with ferromagnetism formation magnetic Change effect, improve Pollutants in Wastewater conversion rate and efficiency, produce absorption affinity, the adsorbance on increase filler surface；Meanwhile mistake 1.5 ~ 3 parts of 0.2 ~ 0.6 part of diisopropylbenzene (DIPB), gelatin activity that can improve microorganism are aoxidized, microorganism is fitted after magnetization in water The microorganism that should be survived has bigger propagation and metabolic capability so that organic pollution leads in the presence of low-intensity magnetic field The effect such as magnetic force key, magnetic force, Lorentz force and mangneto cavity effect is crossed through magnetic to gather, adsorb, being enriched to magnetic biological filling material table Face；Oxygen is paramagnet, can be adsorbed under magnetic fields near biologic packing material during aeration, the oxygen on increase filler surface is dense Degree, promotes the breeding of aerobe, and low-intensity magnetic field also has the function that the activity of inducing microbial and enzymatic activity in addition；Again, its Used using 1 ~ 2 part of collocation of 1.5 ~ 3 parts of gelatin and chitin so that bio-carrier, shorten the biofilm cycle, and strengthen biomembrane suction Attached intensity, it is difficult for drop-off.
5th, the present invention is used for the processing unit up to standard of high-concentration phenolic wastewater, and it further uses high-density polyethylene in being formulated Resin material based on alkene 60 ~ 70 parts of 10 ~ 15 parts of acrylic resins of collocation, 6 ~ 8 parts of low density polyethylene (LDPE)s, addition maleic anhydride 3 ~ 5 parts, the contact angle of sewage and carrier is reduced, improves the hydrophily and impact resistance of carrier, makes microorganism be easier to adhere to On carrier, hydrophilic bio-carrier specific surface area is big, adsorptivity is extremely strong, the micro- life that can prevent carrier outer surface from adhering in water Thing film comes off because being rubbed between carrier, short the time required to biofilm, improves waste water treatment efficiency；Secondly, magnetic 0.5 during it is formulated ~ 2 parts combine 0.5 ~ 1 part of pentaerythritol stearate, are advantageous to improve the biofilm amount of carrier biofilm.
Brief description of the drawings
Accompanying drawing 1 be handling process of the present invention based on special processor structural representation；
Accompanying drawing 2 is the partial structural diagram of accompanying drawing 1.
In the figures above：1st, catalysis oxidation pond；2nd, oxidation-stabilized pond；3rd, rear biochemical BAF ponds；4th, clear water reserviors；41st, intake Hole；42nd, apopore；51st, leading portion transfer conduit；52nd, back segment transfer conduit；6th, elevator pump；7th, inlet channel；8th, ozone occurs Device；9th, gas pipeline；10th, back segment reflux line；11st, backwashing pump；12nd, ozone catalytic particle；15th, pretreated primary BAF ponds； 16th, two level BAF ponds are pre-processed；17th, discharge bay；18th, comprehensive tank is diluted；181st, charge door；182nd, agitator；19th, backwash precipitates Pond；201st, the first pipeline；202nd, backwash sedimentation basin；21st, leading portion supernatant liquid pool；22nd, backwashing pump is pre-processed；23rd, leading portion return duct Road.
Embodiment
With reference to embodiment, the invention will be further described：
Embodiment 1 ~ 4：A kind of processing unit up to standard for high-concentration phenolic wastewater, the handling process are based on a dedicated processes Device, the special processor include catalysis oxidation pond 1, oxidation-stabilized pond 2, rear biochemical BAF ponds 3, clear water reserviors 4, dilution synthesis Tank 18, pretreated primary BAF ponds 15, pretreatment two level BAF ponds 16 and discharge bay 17, the dilution synthesis tank 18, pretreatment one Level BAF ponds 15, pretreatment two level BAF ponds 16 and discharge bay 17 pass sequentially through leading portion transfer conduit 51 and connected,
The catalysis oxidation pond 1, oxidation-stabilized pond 2, rear biochemical BAF ponds 3 and clear water reserviors 4 pass sequentially through back segment transfer conduit 52 and connected Connecing, the discharge bay 17 is connected to inside catalysis oxidation pond 1 with catalysis oxidation pond 1 by inlet channel 7,
One ozone generator 8 is connected to inside catalysis oxidation pond 1 by gas pipeline 9, and the clear water reserviors 4 are provided with inlet opening 41st, apopore 42, the inlet opening 41 of the clear water reserviors 4 are connected with rear biochemical BAF ponds 3 by back segment transfer conduit 52, described clear Pond 4 is connected to the one end of a backwashing pump 11, and this other end of backwashing pump 11 is connected to catalysis oxidation pond by back segment reflux line 10 1st, inside rear biochemical BAF ponds 3, the catalysis oxidation pond 1 is filled with ozone catalytic particle 12 with fixed bed form, and the dilution is comprehensive Close tank 18 and be provided with charge door 181 and agitator 182；
The ozone catalytic particle 12 is made up of the component of following parts by weight, as shown in table 1：
Table 1
Embodiment 1 Embodiment 2 Embodiment 3 Embodiment 4
Activated alumina particle 90 parts 89.5 parts 89 parts 91 parts
1.2 ~ 1.5 parts of cupric oxide 1.25 part 1.4 part 1.2 part 1.3 part
4 ~ 7 parts of polyethylene glycol 5.2 part 6 parts 4.5 part 6.2 part
1.5 ~ 2 parts of polyvinyl alcohol 1.5 part 1.8 part 2 parts 1.6 part
0.8 ~ 1 part of titanium dioxide 1 part 0.9 part 0.95 part 0.8 part
0.3 ~ 0.5 part of hydroxypropyl cellulose 0.45 part 0.38 part 0.5 part 0.35 part
0.2 ~ 0.4 part of manganese dioxide 0.3 part 0.2 part 0.25 part 0.32 part
The activated alumina particle particle diameter is 2 ~ 4mm；
By 88.7 ~ 91.3 parts of the activated alumina particle and 1.2 ~ 1.5 parts of cupric oxide, polyethylene glycol 4 ~ 7 that the particle diameter is 2 ~ 4mm Part, 1.5 ~ 2 parts of polyvinyl alcohol, 0.8 ~ 1 part of titanium dioxide, 0.3 ~ 0.5 part of hydroxypropyl cellulose, 0.2 ~ 0.4 part of manganese dioxide exist Mixed in stirring mixer so that uniform mixed 1.2 ~ 1.5 parts of cupric oxide, 4 ~ 7 parts of polyethylene glycol, polyvinyl alcohol 1.5 ~ 2 Part, 0.8 ~ 1 part of titanium dioxide, 0.3 ~ 0.5 part of hydroxypropyl cellulose, 0.2 ~ 0.4 part of manganese dioxide are covered in the active oxidation Alumina particles surface forms catalyst mother bulb；Catalyst mother bulb is dried successively again, is calcined the acquisition loaded catalyst.
Also include the backwash sedimentation basin 19, leading portion supernatant liquid pool 21 and pretreatment backwashing pump 22 being sequentially connected, the backwash Sedimentation basin 19 is connected to pretreated primary BAF ponds 15, pretreatment two level BAF ponds 16 by the first pipeline 201, second pipe 201, The pretreatment backwashing pump 22 is connected to pretreated primary BAF ponds 15, pretreatment two level BAF ponds by leading portion reflux line 23 16。
Above-mentioned ozone generator 8 is connected to the bottom in catalysis oxidation pond 1 by gas pipeline 9.
Drying time is 5 hours under the conditions of 100 ~ 120 DEG C in above-mentioned steps three；At 350 ~ 520 DEG C in above-mentioned steps four Under the conditions of roasting time be 8 hours.
Ozone catalytic particulate catalytic effect assessment of the present invention, experimental method and data are shown in Table 2：
In the experiment of dynamic continuous flow catalytic ozonation, catalyst amountses 1.5L, ozone dosage 100mg/L, waterpower are stopped Time 1h is stayed, using gas flowmeter control ozone dosage in experiment, passes through peristaltic pump continuum micromeehanics.3 cycles of operation urge After changing effect stability, COD is repeatedly measured by sampling, averages.
Experiment condition：Dynamic continuous flow operational mode, the h of ozone dosage 100mg/L, HRT=1.
Intake source：Certain factory's phenol wastewater water, COD about 350 mg/L, TDS 3500mg/L.
It is resistance to relative to Zhonghai Asphalt's conventional alumina ozone catalyst from table 2 it was found from data High salt ozone catalyst catalysis oxidation phenol wastewater, it is 100mg/L in ozone dosage, hydraulic detention time is that 1 h runs bar Under part, COD clearances are up to 34.2%, and ozone efficiency is 1.1, far superior to conventional ozone catalyst.
Several biologic packing materials are placed with biochemical BAF ponds 3 after described, the biologic packing material is overlying on carrier by carrier and extension The microbial film composition on surface；
The carrier is made up of the component of following parts by weight, as shown in table 3：
Table 3
The density of above-mentioned carrier is 0.96~0.98g/cm3。
Above-mentioned white lime is with Tao Shi Powdered Activated Carbons and precipitated calcium carbonate according to 1：1.2：0.9 parts by weight mix.
A kind of preparation method for above-mentioned carrier, comprise the following steps：
Step 1: taking 3 ~ 5 parts of maleic anhydride, 0.2 ~ 0.6 part of cumyl peroxide, they are dissolved with 2.5 kilograms of acetone and made Into acetone soln, it is placed in mixer；
Step 2: 65 ~ 75 parts of high density polyethylene (HDPE), 10 ~ 15 parts of acrylic resin, low density polyethylene (LDPE) are added into mixer again 6 ~ 8 parts, 5 ~ 15 parts of white lime, 5 ~ 20 parts of Tao Shi Powdered Activated Carbons, 6 ~ 10 parts of precipitated calcium carbonate, 1.5 ~ 3 parts of gelatin, chitin 1 ~ The uniformly mixing of 2 parts and 0.5 ~ 2 part of magnetic, 0.5 ~ 1 part of pentaerythritol stearate, it is placed in after taking-up in unlimited container and allows acetone Naturally volatilize, make solid；
Step 3: above-mentioned solid material is put into double screw extruder, melting extrusion is granulated；
Step 4: the particle produced above is put into 45 type single screw extrusion machines, by extrusion die extrusion forming, obtain Filler is cylinder, and axial cross reinforcing rib is set in it, sets axially radial fin on cylinder outer wall.
The present invention is used for the processing unit up to standard of high-concentration phenolic wastewater, and the course of work is as follows, comprises the steps：
（1）High saliferous phenol wastewater squeezes into interior circulation BAF systems by pump, and sewage is lifted along aeration tube, then by biological bed, is formed Recycle stream.Water velocity inside packing layer reaches 20~30m/h, improves the mass transfer velocity between biomembrane and aqueous phase, improves The treatment efficiency and impact resistance of reactor, while prevent and gas caused by the channel to be formed directly is aerated to packing layer Water short circuit phenomenon occurs.The biochemical component of high saliferous phenol wastewater is degraded by the BAF systems of pretreatment, so as to drop Low bio-chemical effluent COD；
（2）Biochemistry pre-processes water outlet gravity flow into catalytic ozonation, rear biochemical interior circulation BAF coupling technique processing systems, should System carries out catalytic oxidation first with ozone, using a part of refractory organic of ozone oxidation, makes macromolecular Oxidation operation can improve the biodegradability of pretreatment water outlet into small organic molecule；
（3）Circulation BAF advanced treatment systems in catalytic ozonation water outlet is biochemical after entering, the biochemical reaction tank utilize domestication Mushroom carries out biodegradation to the small organic molecule of ozone oxidation water outlet, water outlet COD is further reduced.
Wherein, step（1）In in order to ensure pretreatment IRBAF devices in microorganism growth, total dissolved solid is dense Degree control is 1.3% to 2.5%；
Step（2）In middle catalytic ozonation technique, control ozone dosage is not more than 100mg/L, to be followed in biochemistry after satisfaction Ring BAF demands.Catalyst exists as a fixed bed in catalytic ozonation pond, and the present embodiment catalyst is that metal ion is born Supported catalyst, can catalysis ozone produce hydroxyl radical free radical, while reduce the activation energy of hydroxyl radical free radical oxidation reaction, make to contain The organic matter of difficult degradation is mineralized removal in phenol sewage.
Step（3）Circulation BAF advanced treatment systems in middle catalytic ozonation water outlet gravity flow is biochemical after entering, utilize micro- life Thing carries out biodegradation to the organic matter after catalytic ozonation, to reduce processing cost.
When influent COD is 1100-1300mg/L, it is less than 120mg/L, COD by pre-processing the water outlet of IRBAF biochemical systems Clearance is up to 90%, it can be seen that high efficiency of the interior circulation BAF reactors to high saliferous phenol wastewater；It is biochemical for pretreatment Waste water difficult for biological degradation after processing, using catalytic ozonation high-level oxidation technology, utilize metal ion loaded catalyst Catalysis ozone produces the hydroxyl radical free radical of strong oxidizing property, and the organic matter of bio-refractory is aoxidized, and on the one hand has by Machine thing mineralising can reduce water outlet COD, learn that water outlet COD is less than 60mg/L by table 3；On the other hand macromolecular difficult degradation can be had Machine thing is oxidized to the easily biochemical organic matter of small molecule, and then is improved the biochemical of water outlet.Pass through rear biochemical interior circulation BAF again System carries out mineralising to the organic matter in water, and final outflow water is less than 30mg/L, embodies economy, the high efficiency of the group technology.
The above embodiments merely illustrate the technical concept and features of the present invention, and its object is to allow person skilled in the art Scholar can understand present disclosure and implement according to this, and it is not intended to limit the scope of the present invention.It is all according to the present invention The equivalent change or modification that Spirit Essence is made, it should all be included within the scope of the present invention.

Claims (5)

  1. A kind of 1. processing unit up to standard for high-concentration phenolic wastewater, it is characterised in that：It is special that the handling process is based on one Processing unit, the special processor include catalysis oxidation pond（1）, oxidation-stabilized pond（2）, rear biochemical BAF ponds（3）, clear water reserviors （4）, the comprehensive tank of dilution（18）, pretreated primary BAF ponds（15）, pretreatment two level BAF ponds（16）And discharge bay（17）, it is described dilute Release comprehensive tank（18）, pretreated primary BAF ponds（15）, pretreatment two level BAF ponds（16）And discharge bay（17）Pass sequentially through leading portion Transfer conduit（51）Connection,
    The catalysis oxidation pond（1）, oxidation-stabilized pond（2）, rear biochemical BAF ponds（3）And clear water reserviors（4）Pass sequentially through back segment transmission Pipeline（52）Connection, the discharge bay（17）With catalysis oxidation pond（1）Pass through inlet channel（7）It is connected to catalysis oxidation pond（1） It is internal；
    One ozone generator（8）Pass through gas pipeline（9）It is connected to catalysis oxidation pond（1）Inside, the clear water reserviors（4）It is provided with Inlet opening（41）, apopore（42）, the clear water reserviors（4）Inlet opening（41）With rear biochemical BAF ponds（3）Pass through back segment transfer tube Road（52）Connection, the clear water reserviors（4）It is connected to a backwashing pump（11）One end, this backwashing pump（11）The other end is flowed back by back segment Pipeline（10）It is connected to catalysis oxidation pond（1）, rear biochemical BAF ponds（3）Inside, the catalysis oxidation pond（1）With fixed bed form Filled with ozone catalytic particle（12）, the comprehensive tank of dilution（18）It is provided with charge door（181）And agitator（182）；
    The ozone catalytic particle（12）It is made up of the component of following parts by weight：
    Particle diameter is 2 ~ 4mm 88.7 ~ 91.3 parts of activated alumina particle,
    1.2 ~ 1.5 parts of cupric oxide,
    4 ~ 7 parts of polyethylene glycol,
    1.5 ~ 2 parts of polyvinyl alcohol,
    0.8 ~ 1 part of titanium dioxide,
    0.3 ~ 0.5 part of hydroxypropyl cellulose,
    0.2 ~ 0.4 part of manganese dioxide；
    By 88.7 ~ 91.3 parts of the activated alumina particle and 1.2 ~ 1.5 parts of cupric oxide, polyethylene glycol 4 ~ 7 that the particle diameter is 2 ~ 4mm Part, 1.5 ~ 2 parts of polyvinyl alcohol, 0.8 ~ 1 part of titanium dioxide, 0.3 ~ 0.5 part of hydroxypropyl cellulose, 0.2 ~ 0.4 part of manganese dioxide exist Mixed in stirring mixer so that uniform mixed 1.2 ~ 1.5 parts of cupric oxide, 4 ~ 7 parts of polyethylene glycol, polyvinyl alcohol 1.5 ~ 2 Part, 0.8 ~ 1 part of titanium dioxide, 0.3 ~ 0.5 part of hydroxypropyl cellulose, 0.2 ~ 0.4 part of manganese dioxide are covered in the active oxidation Alumina particles surface forms catalyst mother bulb；Catalyst mother bulb is dried successively again, is calcined the acquisition ozone catalytic particle （12）；
    Biochemical BAF ponds after described（3）Several biologic packing materials are inside placed with, the biologic packing material is overlying on carrier table by carrier and extension The microbial film composition in face；
    The carrier is made up of the component of following parts by weight：
    65 ~ 75 parts of high density polyethylene (HDPE),
    10 ~ 15 parts of acrylic resin,
    6 ~ 8 parts of low density polyethylene (LDPE),
    5 ~ 15 parts of white lime,
    5 ~ 20 parts of Tao Shi Powdered Activated Carbons,
    6 ~ 10 parts of precipitated calcium carbonate,
    3 ~ 5 parts of maleic anhydride,
    0.2 ~ 0.6 part of cumyl peroxide,
    1.5 ~ 3 parts of gelatin,
    1 ~ 2 part of chitin,
    0.5 ~ 2 part of magnetic,
    0.5 ~ 1 part of pentaerythritol stearate.
  2. 2. the processing unit up to standard according to claim 1 for high-concentration phenolic wastewater, it is characterised in that：Also include according to The backwash sedimentation basin of secondary connection（19）, leading portion supernatant liquid pool（21）With pretreatment backwashing pump（22）, the backwash sedimentation basin（19） Pass through the first pipeline（201）, second pipe（201）It is connected to pretreated primary BAF ponds（15）, pretreatment two level BAF ponds（16）, The pretreatment backwashing pump（22）Pass through leading portion reflux line（23）It is connected to pretreated primary BAF ponds（15）, pretreatment two level BAF ponds（16）.
  3. 3. the processing unit up to standard according to claim 1 for high-concentration phenolic wastewater, it is characterised in that：The step Roasting time is 7 ~ 9 hours under the conditions of 350 ~ 520 DEG C in four.
  4. 4. the processing unit up to standard according to claim 1 for high-concentration phenolic wastewater, it is characterised in that：The ozone Generator（8）Pass through gas pipeline（9）It is connected to catalysis oxidation pond（1）Bottom.
  5. 5. the processing unit up to standard according to claim 1 for high-concentration phenolic wastewater, it is characterised in that：The step Drying time is 4 ~ 6 hours under the conditions of 100 ~ 120 DEG C in three.
CN201610616110.XA 2016-08-01 2016-08-01 Processing unit up to standard for high-concentration phenolic wastewater Pending CN107673549A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109485135A (en) * 2019-01-08 2019-03-19 贵州大学 A kind of phenolic wastewater treatment is passed through pipeline with high-concentrated ozone

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Publication number Priority date Publication date Assignee Title
CN105481177A (en) * 2015-12-27 2016-04-13 苏州科环环保科技有限公司 Low-consumption nitrification and denitrification coal chemical wastewater advanced treatment device
CN105692880A (en) * 2016-01-27 2016-06-22 苏州科环环保科技有限公司 Suspended biological stuffing for water treatment

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Publication number Priority date Publication date Assignee Title
CN105481177A (en) * 2015-12-27 2016-04-13 苏州科环环保科技有限公司 Low-consumption nitrification and denitrification coal chemical wastewater advanced treatment device
CN105692880A (en) * 2016-01-27 2016-06-22 苏州科环环保科技有限公司 Suspended biological stuffing for water treatment

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109485135A (en) * 2019-01-08 2019-03-19 贵州大学 A kind of phenolic wastewater treatment is passed through pipeline with high-concentrated ozone

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