CN101885566A - Treatment system and method of coking wastewater - Google Patents
Treatment system and method of coking wastewater Download PDFInfo
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- CN101885566A CN101885566A CN 201010239859 CN201010239859A CN101885566A CN 101885566 A CN101885566 A CN 101885566A CN 201010239859 CN201010239859 CN 201010239859 CN 201010239859 A CN201010239859 A CN 201010239859A CN 101885566 A CN101885566 A CN 101885566A
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Abstract
The invention discloses a treatment system and method of coking wastewater, belonging to the technical field of coking wastewater treatment. The system comprises an adjusting tank, an electrocoagulation reactor, a biochemical treatment device, a secondary sedimentation tank, a coagulation reaction tank and a coagulation sedimentation tank, wherein the adjusting tank is provided with a water inlet for introducing coking wastewater, the water outlet of the adjusting tank is connected with the electrocoagulation reactor, the biochemical treatment tank, the secondary sedimentation tank, the coagulation reaction tank and the coagulation sedimentation tank in turn; and the coagulation sedimentation tank is provided with a water outlet for discharging the treated water. By using the system of the invention, the treatment of coking wastewater for degrading CODCr and treating ammonia nitrogen can be performed; and the CODCr of the effluent can be below 100mg/L, ammonia nitrogen content can be below 15mg/L, the concentration of total cyanides can be below 0.5mg/l, and the grade A discharge standard of the integrated wastewater discharge standard (GB8978-96) can be reached.
Description
Technical field
The present invention relates to the Technologies of Coke Plant Wastewater Treatment field, particularly relate to a kind of treatment system and treatment process of coking chemical waste water.
Background technology
Coking chemical waste water is a kind of unmanageable trade effluent, its contain pyridine, furans, pyrroles, quinoline, indoles, etc. the compound of multiple difficult degradation, these compound properties are stable, and easily biomagnification has carcinogenic, teratogenesis, mutagenesis, single biological process are difficult to eliminate, and have only in conjunction with physicochemical method and could effectively remove, Fenton process is difficult to use because of operation under low pH, and ozone oxidation is because of need pure oxygen cost height and safeguard complicated.
Summary of the invention
The purpose of the embodiment of the invention provides a kind of treatment system and treatment process of coking chemical waste water, and this system carries out biochemical treatment to waste water again after the biodegradability that improves coking chemical waste water, make the COD of Treatment of Wastewater in Coking
CrWith NH
3-N has reached primary standard in the national sewage comprehensive emission standard (GB8978-1996), and this system architecture is simple, the processing efficiency height, and convenient management need not add the biodegradability that sanitary sewage improves waste water during processing.
The objective of the invention is to be achieved through the following technical solutions:
The embodiment of the invention provides a kind of treatment system of coking chemical waste water, comprising:
Equalizing tank, electric flocculation reactor, biochemical processing device, second pond, coagulation reaction tank and coagulative precipitation tank;
Described equalizing tank is provided with the water-in of introducing coking chemical waste water, and the water outlet of equalizing tank is connected with electric flocculation reactor, biochemical treatment tank, second pond, coagulation reaction tank and coagulative precipitation tank successively; Described coagulative precipitation tank is provided with discharges the water outlet of handling back water.
The embodiment of the invention also provides a kind of treatment process of coking chemical waste water, comprising:
Adopt aforesaid right to require 1～7 each described treatment system that coking chemical waste water is handled;
Regulate and handle: make handled coking chemical waste water enter the equalizing tank of treatment system, by equalizing tank regulating to the coking chemical waste water water yield;
The electricity flocculation treatment: the water outlet of equalizing tank enters electric flocculation reactor and carries out electric flocculation reaction, destroys the organic constitution of difficult for biological degradation in the coking chemical waste water and removes partial organic substances by electric flocculation reaction, improves the biodegradability of waste water;
Biochemical treatment: the water outlet of electric flocculation reactor enters biochemical processing device and carries out biochemical treatment, and the double oxygen reaction by biochemical treatment is hydrolyzed and denitrification denitrogenation, and the water outlet of the oxygen reaction of holding concurrently enters the aerobic reaction of biochemical treatment and removes COD
Cr, and carry out the oxidation of ammonia nitrogen and the removal of prussiate;
Aftertreatment: the water outlet of biochemical processing device enters second pond carry out secondary sedimentation and handle after, enter coagulation reactor again and carry out coagulating, the water outlet of coagulation reaction tank enters coagulative precipitation tank and carries out coagulating sedimentation processing removal pollutent, and the water outlet after coagulating sedimentation is handled effluxes as good water.
From the technical scheme that the embodiment of the invention provides as can be seen, in the embodiment of the invention by electric flocculation reactor is set before biochemical processing device, make the coking chemical waste water of processing carry out electric flocculation reaction processing through electric flocculation reactor, after improving the biodegradability of waste water, enter biochemical processing device again and carry out biochemical treatment, improved treatment effect, the COD of coking chemical waste water after treatment to coking chemical waste water
Cr, NH
3-N and total cyanogen concentration reach the primary standard of national sewage comprehensive emission standard (GB8978-1996).This system architecture is simple, and convenient management need not add the biodegradability that sanitary sewage improves waste water during processing, and processing cost is low, and water treatment working cost per ton only is about 7.0 yuan.
Description of drawings
The synoptic diagram of the treatment system that Fig. 1 provides for the embodiment of the invention 1;
Electric flocculation reactor structural representation in the treatment system that Fig. 2 provides for the embodiment of the invention 1;
The synoptic diagram of the treatment system that Fig. 3 provides for the embodiment of the invention 2;
Each label is among Fig. 1: the 1-equalizing tank; 2-electricity flocculation reactor; The 3-oxygen compatibility pool; 4-first Aerobic Pond; 5-second Aerobic Pond; The 6-second pond; The 7-coagulation reaction tank; The 8-coagulative precipitation tank; The 9-blower fan; 10,11-reflux pump; The 12-agitator; 13,14-partition wall;
Each label is among Fig. 1: the 1-equalizing tank; 2-electricity flocculation reactor; 3-first oxygen compatibility pool; 16-second oxygen compatibility pool; 4-first Aerobic Pond; 5-second Aerobic Pond; The 6-second pond; The 7-coagulation reaction tank; The 8-coagulative precipitation tank; The 9-blower fan; 10,11-reflux pump; 12,15-agitator; 13,14-partition wall;
The 20-positive pole; The 21-negative pole; 22-first water outlet; The 23-recycle pump; 24-first control valve; 25-the 3rd control valve; 26-second control valve; The 27-acid storage; 28-fails sour pump; 29-second water outlet; The 210-reactor body; 211-porous water distributor; The 212-negative electrode; The 213-anode.
Embodiment
The invention will be further described below in conjunction with the drawings and specific embodiments:
Embodiment 1
Present embodiment provides a kind of treatment system of coking chemical waste water, be mainly used in coking chemical waste water is handled, improve under the prerequisite of biodegradability of waste water need not adding sanitary sewage, can make the coking chemical waste water after the processing reach respective standard, as shown in Figure 1, this treatment system comprises: equalizing tank 1, electric flocculation reactor 2, biochemical processing device, second pond 6, coagulation reaction tank 7 and coagulative precipitation tank 8;
Wherein, equalizing tank 1 is provided with the water inlet A of introducing the coking chemical waste water of handling, and the water outlet of equalizing tank 1 is connected with electric flocculation reactor 2, biochemical treatment tank, second pond 6, coagulation reaction tank 7 and coagulative precipitation tank 8 successively; Coagulative precipitation tank 8 is provided with discharges the water outlet B of handling back water; The mud relief outlet of electricity flocculation reactor 2, second pond 6 and coagulative precipitation tank 8 all is connected to the water-in of biochemical processing device for 11 times by pipeline and reflux pump; And the mud relief outlet of electric flocculation reactor 2, second pond 6 and coagulative precipitation tank 7 effluxes a mouthful D with mud simultaneously and is connected.The part mud of so electric flocculation reactor, second pond and coagulative precipitation tank refluxes, and part mud effluxes.
As shown in Figure 2, electric flocculation reactor 2 concrete structures in the above-mentioned treatment system are: the length and width of reactor body 210 are high to be 2m * 1.5m * 1.5m, porous water distributor 211 is established in the water inlet of reactor body 210, in the reactor body 210 electrode assemblie is set, electrode assemblie length and width height is 1m * 0.4m * 1m, be provided as the anode 213 and negative electrode 212 of electrode on the electrode assemblie, anode 213 adopts stainless steel plate, negative electrode 212 adopts aluminium sheet, aluminium sheet and stainless steel plate interleaved are arranged on the electrode assemblie, spacing between aluminium sheet and the stainless steel plate is 2.1～3.5mm, adopt direct supply, anode and negative electrode respectively with direct supply just, negative pole 20,21 connect, and voltage is 12～18V between the pole plate of anode 213 and negative electrode 212; First water outlet 22 that this reactor connects oxygen compatibility pool is connected to the water-in of this reactor body 210 for 23 times through the recycle pump of backflow usefulness, and the circling water flow rate of recycle pump 23 is 3 times of water inlet (equalizing tank drainage water) flow; Second water outlet 29 that connects oxygen compatibility pool of this reactor body is connected through the acid storage 27 of second control valve 26 with reactor body 210 outsides, and acid storage 27 is connected to the water-in of this reactor body 210 for 28 times by pipeline and defeated sour pump.
During use, linking to each other in the positive pole of power supply and this electricity flocculation reactor as the anodic stainless steel plate, negative pole links to each other with aluminium sheet as negative electrode, the electricity wadding reactor water outlet of waste water and backflow together enters recycle pump, and enter in the electrode assemblie in the reactor body by the porous water distributor and to carry out electric flocculation treatment, electricity flocculation water part enters oxygen compatibility pool, is partly refluxed in this electricity flocculation reactor; The work of electricity flocculation reactor is after 3 days, stop into water, close first control valve and open the 3rd control valve, the waste water that retains in the electric flocculation reactor is entered oxygen compatibility pool, after the emptying, open defeated sour pump, dilute hydrochloric acid in the acid storage is pumped in the reactor, make electrode assemblie in acid solution, soak 10～15min after, reach the purpose of cleaning, open second control valve after the cleaning again, acid solution is entered acid storage make dilute hydrochloric acid repeated use capable of circulation.In the reality, two in parallel uses of electric flocculation reactor can be set in this treatment system, alternate run during work, assurance is to the continuity of wastewater treatment, this electricity flocculation reactor polar plate voltage is low, the power consumptive province, routine cleaning has guaranteed that with washing away of recycle pump the electrode processing efficiency is efficient with big flow backflow, has eliminated the low electrode assemblie that reaches of traditional electrical flocculation reactor processing efficiency and has cleaned and the inconvenient problem of replacing.The porous water distributor of reactor body water inlet guarantees that water distribution is even, is effectively exempted from the generation of short circuit, has guaranteed to handle the efficient of waste water.Advantage with processing efficiency height and simple and convenient operation and maintenance.The reaction times of waste water in electric flocculation reactor of handling is 10～15 minutes.This electricity flocculation reactor can carry out electric flocculation reaction to the waste water that enters, by the oxygenizement in the electric flocculation reaction process, oxidable complex organic compound is a simple organic, thereby improve the biodegradability of waste water, by the reductive action in the electric flocculation reaction process, reducible organism, also improve the biodegradability of waste water, weaken the restraining effect of waste water greatly to microorganism, thereby improve the oxygen compatibility pool of biological treatment and the waste water treatment efficiency of Aerobic Pond, second pond and coagulative precipitation tank, make water outlet up to standard.
Biochemical processing device in the above-mentioned treatment system is made of oxygen compatibility pool 3, first Aerobic Pond 4, second Aerobic Pond 5, blower fan 9, return line and reflux pump 10; Wherein, oxygen compatibility pool 3 is connected with first Aerobic Pond 4, second Aerobic Pond 5, and the three is an integral structure; Specifically be that twice partition wall 13,14 is set in the reaction tank of an integral body, be separated into three reaction tanks in the pond body with reaction tank, three reaction tanks are followed successively by oxygen compatibility pool 3, first Aerobic Pond 4 and second Aerobic Pond 5, and communicating aperture all is set on the per pass partition wall, and three reaction tanks are communicated with; This building jointly to the biochemical processing device of integral structure saved floor space, can reduce cost;
Be provided with agitator 12 in the described oxygen compatibility pool 3; Two Aerobic Pond bottoms are equipped with aerator, and described aerator is connected with blower fan 9;
Described first Aerobic Pond 4 is provided with alkali lye and the phosphatic inlet C that adds, and the refluxing opening that second Aerobic Pond, 5 bottoms are provided with is connected to the water-in of described oxygen compatibility pool 3 for 10 times by return line and reflux pump.
In the above-mentioned biochemical processing device, oxygen compatibility pool 3 can be designed to complete mixed type or mixed type, and organic hydrolysis reaction, the anti-nitration reaction of concurrent caliche hydrochlorate take place in the oxygen compatibility pool; Aerobic Pond 4,5 is can right and wrong single to be mixed or the reactor of plug-flow fully, is mixed type; Organic oxidation, the nitration reaction of ammonia nitrogen take place in the Aerobic Pond; Return sludge ratio is 100%, and return current ratio of the mixed liquid is 200～300%, and the oxygen compatibility pool sludge concentration is 3.2～4.1g/l, and sludge concentration is 3.2～4.4g/l in the Aerobic Pond; During work, the temperature of reaction of oxygen compatibility pool is 29 ℃～31 ℃, and sludge age is 20～25 days, DO is 0.1mg/l～0.4mg/l, pH is 7.1～7.8, can realize the hydrolysis of microorganism to organism and prussiate smoothly in the oxygen compatibility pool, and denitrifying bacterium is with nitrate reduction.The temperature of reaction of two aerobic reactors is 29 ℃～31 ℃, and sludge age is 20～25 days, and DO is 2.0～2.5mg/l, the pH value is 8.0～8.6, controlling reactor influent side DO is about 2.3mg/l, and water outlet side DO is 2.0～2.5mg/l, is 8.0～8.6 by adding liquid caustic soda control pH value.The small part nitration reaction takes place in the main decarburizing reaction that takes place simultaneously in first Aerobic Pond of influent side; And in second Aerobic Pond of water outlet side the main nitration reaction that Nitromonas takes place, the part decarburizing reaction takes place simultaneously.
During above-mentioned treatment system Treatment of Wastewater in Coking, the hydraulic detention time of coagulation reaction tank is 15min, and the surface load of coagulative precipitation tank is 1.0～1.3m
3/ m
2.h.
The treatment system of present embodiment is simple in structure, convenient management, because electric flocculation reactor is set before biochemical processing device, by electric flocculation reactor, the organism of difficult for biological degradation in the waste water is become the organism of readily biodegradable, significantly weakened simultaneously the restraining effect of venomous injurant to microorganism, integral body has changed the biochemical treatment character of waste water, make the bio-reaction system organic loading improve 15～20%, thereby reduce the bio-reaction system volume, sludge age reduces, and sludge settling does not power up the flocculation reactor fashion, makes the second pond surface load can improve 30%, reduced the settling tank volume, thereby saved investment, thereby guaranteed the biochemical treatment effect of follow-up biochemical processing device, made water outlet up to standard.Therefore, need not add the biodegradability that sanitary sewage improves waste water in treating processes, processing cost is low, and water treatment working cost per ton only is about 7.0 yuan.
Embodiment 2
Present embodiment provides a kind of treatment system of coking chemical waste water, be mainly used in coking chemical waste water is handled, improve under the prerequisite of biodegradability of waste water need not adding sanitary sewage, can make the coking chemical waste water after the processing reach respective standard, as shown in Figure 3, the treatment system that provides among the structure of this treatment system and the embodiment 1 is basic identical, and the biochemical processing device of this treatment system that different is is made of first oxygen compatibility pool 3, second oxygen compatibility pool 16, first Aerobic Pond 4, second Aerobic Pond 5, blower fan 9, return line and reflux pump 19; Wherein, first oxygen compatibility pool 3 is connected with second Aerobic Pond 5 successively with second oxygen compatibility pool 16, first Aerobic Pond 4, wherein, first oxygen compatibility pool 3 and second oxygen compatibility pool 16 are integral structure, specifically be to adopt the reaction tank of an integral body, partition wall 13 is set in it one, be separated into first oxygen compatibility pool and second oxygen compatibility pool in the pond body with reaction tank as oxygen compatibility pool, be equipped with communicating aperture on the partition wall, first oxygen compatibility pool is communicated with second oxygen compatibility pool; And first Aerobic Pond 4 and second Aerobic Pond 5 are integral structure, specifically be to adopt the reaction tank of an integral body as Aerobic Pond, partition wall 14 is set in it one, be separated into first Aerobic Pond and second Aerobic Pond in the pond body with reaction tank, be equipped with communicating aperture on the partition wall, first Aerobic Pond is communicated with second Aerobic Pond; The biochemical processing device of this structure, the Aerobic Pond branch of the oxygen compatibility pool of integral type and integral type is built, and improves microorganism active, and hold concurrently oxygen reactor and aerobic reactor branch are built the needs of building the place in order to adapt to, also help maintenance.
Be equipped with agitator in described two oxygen compatibility pools; Two Aerobic Pond bottoms are equipped with aerator, and described aerator is connected with described blower fan;
Described first Aerobic Pond is provided with alkali lye and the phosphatic inlet that adds, and the refluxing opening that second Aerobic Pond bottom is provided with is connected to the water-in of described oxygen compatibility pool by return line and backflow blowback.
Present embodiment provides a kind of treatment process of coking chemical waste water, can adopt the treatment system that provides among the foregoing description 1 or the embodiment 2, makes the biochemical waste water of processing reach respective standard, and this method comprises:
Regulate and handle: make handled coking chemical waste water enter the equalizing tank of treatment system, by equalizing tank regulating to the coking chemical waste water water yield;
The electricity flocculation treatment: the water outlet of equalizing tank enters electric flocculation reactor and carries out electric flocculation reaction, electric flocculation reaction is carried out in the water outlet of equalizing tank in electric flocculation reactor time is 10～15 minutes, destroy the organic constitution of difficult for biological degradation in the coking chemical waste water and remove partial organic substances by electric flocculation reaction, weaken the restraining effect of waste water greatly to microorganism, improve the biodegradability of waste water, the biodegradability of waste water improves after the electric flocculation reaction; Improve organic removal load of biological treatment system, improve the sedimentation function of second pond mud, weaken the coagulative precipitation tank dosing;
Biochemical treatment: the water outlet of electric flocculation reactor enters biochemical processing device and carries out biochemical treatment, and the double oxygen reaction by biochemical treatment is hydrolyzed and denitrification denitrogenation, and the water outlet of the oxygen reaction of holding concurrently enters the aerobic reaction of biochemical treatment and removes COD
Cr, and carry out the oxidation of ammonia nitrogen and the removal of prussiate;
In the above-mentioned biochemical treatment, the temperature of reaction of the oxygen of holding concurrently in oxygen compatibility pool reaction is 29 ℃～31 ℃, and sludge concentration is 3.2～4.1g/l, and sludge age is 20～25 days, and DO is 0.1mg/l～0.4mg/l, and the pH value is 7.1～7.8;
The temperature of reaction of carrying out aerobic reaction in the Aerobic Pond is 29 ℃～31 ℃, and sludge concentration is 3.2～4.4g/l, and sludge age is 20～25 days, and DO is 2.0～2.5mg/l, and the pH value is 8.0～8.6;
In the biochemical treatment, mud and mixed solution are refluxed, return sludge ratio is 100%, and return current ratio of the mixed liquid is 200～300%, and the oxygen reactor sludge concentration of holding concurrently is 3.2～4.1g/l, and sludge concentration is 3.2～4.4g/l in the aerobic reactor.
Aftertreatment: the water outlet of biochemical processing device enters second pond carry out secondary sedimentation and handle after, enter coagulation reactor again and carry out coagulating, the hydraulic detention time of coagulating is 15 minutes, the water outlet of coagulation reaction tank enters coagulative precipitation tank and carries out coagulating sedimentation processing removal pollutent, and the surface load of coagulative precipitation tank is 1.0～1.3m
3/ m
2.h, the water outlet after coagulating sedimentation is handled effluxes as good water.
In the above-mentioned treatment process, mainly be the biodegradability that improves the coking chemical waste water of handling by electric flocculation reaction, thereby improve the processing efficiency and the treatment effect of biochemical processing device; In the electricity flocculation reaction process, improve the biochemical of coking chemical waste water, comprising by following reaction:
Oxygenizement direct oxidation in oxygenizement (oxidable complex organic compound is a simple organic, thereby improves the biodegradability of the waste water) electrolytic process, promptly pollutent directly loses electronics and oxidation takes place at anode; Indirect oxidation: utilize the lower negatively charged ion of electrode potential in the solution, for example OH-, Cl-lose active substance [0] that electronics generates new stronger oxygenant, Cl2 etc. at anode, utilize these active substances to make pollutent lose electronics, play oxygenolysis, with BOD5, CODcr in the reduction stoste, NH3-N etc.
Reductive action (reducible organism, thus the biodegradability of waste water improved, thus improve the processing efficiency of waste water.) reductive action in the electrolytic process directly reduces, promptly pollutent directly obtains electronics and reductive action takes place on negative electrode.The cohesion soluble anode is anode such as iron, aluminium for example, pass to direct current after, after anode loses electronics, form metallic cation Fe2+, Al3+, generate metal hydroxides colloid flocculation agent with the OH-in the solution, adsorptive power is extremely strong, and pollutants in waste water matter sorption-coprecipitation is removed.
In the treatment process of present embodiment, by the electricity flocculation is combined with A-O technology coking chemical waste water is handled, by electric flocculation reaction, can be with the organism modification or the destruction of some difficult degradations in the coking chemical waste water, become the organism of easy biological treatment, particularly adopt electric flocculation reactor and corresponding processing parameter in the embodiment of the invention, the biodegradability of the coking chemical waste water after electric flocculation reaction is handled is improved, make the processing efficiency of A-O improve, the COD clearance of the A-O art breading coking chemical waste water of equal treatment condition improves 6～8 percentage points, therefore, the method that this electricity flocculation and A-O technology combine coking chemical waste water is handled, the biodegradability of sanitary sewage raising coking chemical waste water need not be added in the treating processes, water outlet COD can be made after the processing
CrReach below the 100mg/l, ammonia nitrogen reaches below the 15mg/l, and the total cyanogen concentration of water outlet is below the 0.5mg/l, reaches primary standard in the national sewage comprehensive emission standard (GB8978-96).
In the above-mentioned treatment process, the mud that the mud that electric flocculation reactor produces, second pond excess sludge and coagulative precipitation tank produce carries out transporting outward behind the mechanical dehydration as whole excess sludges.
In sum, in the embodiment of the invention by electric flocculation reactor is set before biochemical processing device, make electric flocculation reaction equipment as pre-treatment, improve the biodegradability of waste water, easier carrying out when making follow-up biochemical processing device carry out biochemical treatment, improved treatment effect and processing efficiency, reduced processing cost coking chemical waste water.
The above; only for the preferable embodiment of the present invention, but protection scope of the present invention is not limited thereto, and anyly is familiar with those skilled in the art in the technical scope that the present invention discloses; the variation that can expect easily or replacement all should be encompassed within protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with the protection domain of claims.
Claims (10)
1. the treatment system of a coking chemical waste water is characterized in that, comprising:
Equalizing tank, electric flocculation reactor, biochemical processing device, second pond, coagulation reaction tank and coagulative precipitation tank;
Described equalizing tank is provided with the water-in of introducing coking chemical waste water, and the water outlet of equalizing tank is connected with electric flocculation reactor, biochemical treatment tank, second pond, coagulation reaction tank and coagulative precipitation tank successively; Described coagulative precipitation tank is provided with discharges the water outlet of handling back water.
2. the treatment system of coking chemical waste water as claimed in claim 1 is characterized in that, described system also comprises:
The excess sludge relief outlet of described electric flocculation reactor, second pond and coagulative precipitation tank all is connected to sludge treating system by pipeline, and the excess sludge relief outlet of second pond also is connected to the oxygen compatibility pool water-in by the backflow blowback.
3. the treatment system of coking chemical waste water as claimed in claim 1 is characterized in that, described electric flocculation reactor comprises:
Reactor body, electrode assemblie, recycle pump, defeated sour pump, acid storage and a plurality of control valve;
Reactor body is provided with water-in, the water inlet is provided with the porous water distributor, be provided with electrode assemblie in the reactor body, be provided as the anode and the negative electrode of electrode on the electrode assemblie, anode adopts stainless steel plate, negative electrode adopts aluminium sheet, and aluminium sheet and stainless steel plate interleaved on electrode assemblie is arranged, and the spacing between aluminium sheet and the stainless steel plate is 2.1～3.5mm; Anode and negative electrode and voltage are that the direct supply of 12～18V is connected; First water outlet that connects oxygen compatibility pool of reactor body returns the water-in that is connected to this reactor body through the recycle pump and first control valve of backflow usefulness;
Second water outlet that connects oxygen compatibility pool of reactor body is connected with acid storage through second control valve, and acid storage is connected to the water-in of this reactor body by pipeline and defeated sour blowback.
4. the treatment system of coking chemical waste water as claimed in claim 1 is characterized in that, described biochemical processing device comprises:
Oxygen compatibility pool, first Aerobic Pond, second Aerobic Pond, blower fan, return line and reflux pump;
Described oxygen compatibility pool is connected with first Aerobic Pond, second Aerobic Pond, and the three is an integral structure;
Be provided with agitator in the described oxygen compatibility pool; Two Aerobic Pond bottoms are equipped with aerator, and described aerator is connected with described blower fan;
Described first Aerobic Pond is provided with alkali lye and the phosphatic inlet that adds, and the refluxing opening that second Aerobic Pond bottom is provided with is connected to the water-in of described oxygen compatibility pool by return line and backflow blowback.
5. the treatment system of coking chemical waste water as claimed in claim 4 is characterized in that, described oxygen compatibility pool is connected with Aerobic Pond, and the three specifically comprises for integral structure:
The twice partition wall is set in the reaction tank of an integral body, is separated into three reaction tanks in the pond body with reaction tank, three reaction tanks are followed successively by oxygen compatibility pool, first Aerobic Pond and second Aerobic Pond, and communicating aperture all is set on the per pass partition wall, and three reaction tanks are communicated with.
6. the treatment system of coking chemical waste water as claimed in claim 1 is characterized in that, described biochemical processing device comprises:
First oxygen compatibility pool, second oxygen compatibility pool, first Aerobic Pond, second Aerobic Pond, blower fan, return line and reflux pump;
Described first oxygen compatibility pool is connected successively with second oxygen compatibility pool, first Aerobic Pond and second Aerobic Pond, and wherein, first oxygen compatibility pool and second oxygen compatibility pool are integral structure; First Aerobic Pond and second Aerobic Pond are integral structure;
Be equipped with agitator in described two oxygen compatibility pools; Two Aerobic Pond bottoms are equipped with aerator, and described aerator is connected with described blower fan;
Described first Aerobic Pond is provided with alkali lye and the phosphatic inlet that adds, and the refluxing opening that second Aerobic Pond bottom is provided with is connected to the water-in of described oxygen compatibility pool by return line and backflow blowback.
7. the treatment system of coking chemical waste water as claimed in claim 6 is characterized in that, described first oxygen compatibility pool and second oxygen compatibility pool are that integral structure specifically comprises:
The reaction tank that oxygen compatibility pool is as a whole is provided with partition wall one in it, be separated into first oxygen compatibility pool and second oxygen compatibility pool in the pond body with reaction tank, is equipped with communicating aperture on the partition wall, and first oxygen compatibility pool is communicated with second oxygen compatibility pool;
Described first Aerobic Pond and second Aerobic Pond are that integral structure specifically comprises:
The reaction tank that Aerobic Pond is as a whole is provided with partition wall one in it, be separated into first Aerobic Pond and second Aerobic Pond in the pond body with reaction tank, is equipped with communicating aperture on the partition wall, and first Aerobic Pond is communicated with second Aerobic Pond.
8. the treatment process of a coking chemical waste water is characterized in that, comprising:
Adopt aforesaid right to require 1～7 each described treatment system that coking chemical waste water is handled;
Regulate and handle: make handled coking chemical waste water enter the equalizing tank of treatment system, by equalizing tank regulating to the coking chemical waste water water yield;
The electricity flocculation treatment: the water outlet of equalizing tank enters electric flocculation reactor and carries out electric flocculation reaction, destroys the organic constitution of difficult for biological degradation in the coking chemical waste water and removes partial organic substances by electric flocculation reaction, improves the biodegradability of waste water;
Biochemical treatment: the water outlet of electric flocculation reactor enters biochemical processing device and carries out biochemical treatment, and the double oxygen reaction by biochemical treatment is hydrolyzed and denitrification denitrogenation, and the water outlet of the oxygen reaction of holding concurrently enters the aerobic reaction of biochemical treatment and removes COD
Cr, and carry out the oxidation of ammonia nitrogen and the removal of prussiate;
Aftertreatment: the water outlet of biochemical processing device enters second pond carry out secondary sedimentation and handle after, enter coagulation reactor again and carry out coagulating, the water outlet of coagulation reaction tank enters coagulative precipitation tank and carries out coagulating sedimentation processing removal pollutent, the water outlet standard discharge after coagulating sedimentation is handled.
9. the treatment process of coking chemical waste water as claimed in claim 8 is characterized in that, in the described electric flocculation treatment, electric flocculation reaction is carried out in the water outlet of equalizing tank in electric flocculation reactor time is 10～15 minutes, improves the biodegradability of waste water after the flocculation reaction;
Described method also comprises:
In the biochemical treatment, mud and mixed solution are refluxed, return sludge ratio is 100%, and return current ratio of the mixed liquid is 200～300%, and the oxygen reactor sludge concentration of holding concurrently is 3.2～4.1g/l, and sludge concentration is 3.2～4.4g/l in the aerobic reactor.
10. the treatment process of coking chemical waste water as claimed in claim 8 is characterized in that, in the described biochemical treatment, the temperature of reaction that the oxygen of holding concurrently reacts is 29 ℃～31 ℃, and sludge concentration is 3.2～4.1g/l, and sludge age is 20～25 days, DO is 0.1mg/l～0.4mg/l, and the pH value is 7.1～7.8;
The temperature of reaction of aerobic reaction is 29 ℃～31 ℃, and sludge concentration is 3.2～4.4g/l, and sludge age is 20～25 days, and DO is 2.0～2.5mg/l, and the pH value is 8.0～8.6;
The hydraulic detention time of described coagulating is 15 minutes, and the surface load of coagulative precipitation tank is 1.0～1.3m
3/ m
2.h.
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| CN201010239859XA CN101885566B (en) | 2010-07-28 | 2010-07-28 | Treatment system and method of coking wastewater |
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| CN201010239859XA CN101885566B (en) | 2010-07-28 | 2010-07-28 | Treatment system and method of coking wastewater |
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| CN101885566A true CN101885566A (en) | 2010-11-17 |
| CN101885566B CN101885566B (en) | 2012-07-25 |
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| CN103011514A (en) * | 2012-12-13 | 2013-04-03 | 杭州绿色环保技术开发有限公司 | Coking wastewater biochemical treatment process and device |
| CN103011410A (en) * | 2012-12-06 | 2013-04-03 | 杭州绿色环保技术开发有限公司 | Synchronous degradation process and device for COD (Chemical Oxygen Demand) and N (Nitrogen) of high concentration wastewater in same pool |
| CN103395941A (en) * | 2013-08-09 | 2013-11-20 | 中国矿业大学(北京) | Lignite upgrading condensate recycling system |
| CN103539292A (en) * | 2013-11-18 | 2014-01-29 | 江苏省环境科学研究院 | Coagulation and sedimentation method for deep treatment of biochemical tail water of printing and dyeing wastewater |
| CN104176860A (en) * | 2014-08-13 | 2014-12-03 | 东莞市东元新能源科技有限公司 | Electric flocculation effluent treatment system |
| CN105036458A (en) * | 2015-06-19 | 2015-11-11 | 广州中科建禹环保有限公司 | Wastewater treatment process adopting porous filler to fix dominant bacteria |
| CN105776525A (en) * | 2016-03-01 | 2016-07-20 | 江苏南大环保科技有限公司 | Integrated two-phase anaerobic desulfurization reactor and wastewater treatment method thereof |
| CN105836971A (en) * | 2016-05-19 | 2016-08-10 | 东莞理工学院 | Electric flocculation wastewater treatment simulation demonstration system and method |
| CN106587535A (en) * | 2016-12-30 | 2017-04-26 | 中冶赛迪工程技术股份有限公司 | Coking wastewater treatment process and system |
| CN107055944A (en) * | 2017-02-27 | 2017-08-18 | 陕西省石油化工研究设计院 | A kind of emulsion paint Waste Water Treatment and method |
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| CN103011410A (en) * | 2012-12-06 | 2013-04-03 | 杭州绿色环保技术开发有限公司 | Synchronous degradation process and device for COD (Chemical Oxygen Demand) and N (Nitrogen) of high concentration wastewater in same pool |
| CN103011410B (en) * | 2012-12-06 | 2014-12-03 | 杭州绿色环保技术开发有限公司 | Synchronous degradation process and device for COD (Chemical Oxygen Demand) and N (Nitrogen) of high concentration wastewater in same pool |
| CN103011514A (en) * | 2012-12-13 | 2013-04-03 | 杭州绿色环保技术开发有限公司 | Coking wastewater biochemical treatment process and device |
| CN103395941A (en) * | 2013-08-09 | 2013-11-20 | 中国矿业大学(北京) | Lignite upgrading condensate recycling system |
| CN103395941B (en) * | 2013-08-09 | 2014-12-10 | 中国矿业大学(北京) | Lignite upgrading condensate recycling system |
| CN103539292A (en) * | 2013-11-18 | 2014-01-29 | 江苏省环境科学研究院 | Coagulation and sedimentation method for deep treatment of biochemical tail water of printing and dyeing wastewater |
| CN103539292B (en) * | 2013-11-18 | 2015-04-08 | 江苏省环境科学研究院 | Coagulation and sedimentation method for deep treatment of biochemical tail water of printing and dyeing wastewater |
| CN104176860B (en) * | 2014-08-13 | 2015-12-09 | 东莞市东元新能源科技有限公司 | A kind of electricity flocculation Waste Water Treatment |
| CN104176860A (en) * | 2014-08-13 | 2014-12-03 | 东莞市东元新能源科技有限公司 | Electric flocculation effluent treatment system |
| CN105036458A (en) * | 2015-06-19 | 2015-11-11 | 广州中科建禹环保有限公司 | Wastewater treatment process adopting porous filler to fix dominant bacteria |
| CN105776525A (en) * | 2016-03-01 | 2016-07-20 | 江苏南大环保科技有限公司 | Integrated two-phase anaerobic desulfurization reactor and wastewater treatment method thereof |
| CN105776525B (en) * | 2016-03-01 | 2019-03-01 | 南京大学 | Integral type diphasic anaerobic desulfurization reactor and its wastewater treatment method |
| CN105836971A (en) * | 2016-05-19 | 2016-08-10 | 东莞理工学院 | Electric flocculation wastewater treatment simulation demonstration system and method |
| CN105836971B (en) * | 2016-05-19 | 2019-03-08 | 东莞理工学院 | Electric flocculation wastewater treatment analog demenstration system and method |
| CN106587535A (en) * | 2016-12-30 | 2017-04-26 | 中冶赛迪工程技术股份有限公司 | Coking wastewater treatment process and system |
| CN107055944A (en) * | 2017-02-27 | 2017-08-18 | 陕西省石油化工研究设计院 | A kind of emulsion paint Waste Water Treatment and method |
| CN107055944B (en) * | 2017-02-27 | 2023-05-16 | 陕西省石油化工研究设计院 | Emulsion paint wastewater treatment system and method |
| CN111675427A (en) * | 2020-06-05 | 2020-09-18 | 成都飞创科技有限公司 | Rural domestic sewage treatment system |
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