CN106396187A - Cyanide wastewater treating and recycling method - Google Patents
Cyanide wastewater treating and recycling method Download PDFInfo
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- CN106396187A CN106396187A CN201611015376.5A CN201611015376A CN106396187A CN 106396187 A CN106396187 A CN 106396187A CN 201611015376 A CN201611015376 A CN 201611015376A CN 106396187 A CN106396187 A CN 106396187A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
- C02F2101/18—Cyanides
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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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Abstract
The invention discloses a cyanide wastewater treating and recycling method. The cyanide wastewater treating and recycling method includes the steps of (A) delivering cyanide wastewater from a production line to a first oxidation reaction pool, adding high-purity chlorine dioxide and alkaline liquor sequentially and mixing with stirring; (B) enabling the wastewater to automatically flow into a second oxidation reaction pool after reaction, adding sodium hypochlorite and mixing with stirring; (C) enabling the wastewater to automatically flow into a flocculation pool, adding a flocculating agent and mixing with stirring; (D) enabling the wastewater to automatically flow into a precipitating pool for precipitation; (E) delivering cupreous sludge isolated from the precipitating pool to a pressure filter for pressure filtering and transporting out filtered sludge, and delivering liquid supernatant to membrane filtering equipment for filtering to finally obtain qualified water which can be recycled and used in production. The cyanide wastewater treating and recycling method has the advantages that big change is not needed, an existing wastewater treating device can be adopted, only several pipelines need to be adjusted, workload for water treatment is reduced greatly, construction investment is reduced, operation is facilitated, and cost is reduced.
Description
Technical field
The present invention relates to field of waste water treatment, the method for more particularly to a kind of cyanide wastewater process and reuse.
Background technology
In the development of the national economy, non-ferrous metal metallurgy, intermetallic composite coating, coking, plating, chemical industry, process hides, instrument, ore dressing
Etc. commercial production, it is obtained for and constantly develops, cyanide wastewater is also mainly derived from these commercial production.Because cyanide wastewater belongs to
In high toxicity inorganic wastewater, all there is stronger toxic action to biological and environment, and the hydrogen of severe toxicity can be produced in acid condition
Fluoric acid gas, directly has fatal harm, is the waste water that state compulsion is processed, must not arbitrarily or not qualified discharge.Therefore, to containing
Cyanogen waste water processed after qualified discharge or be back to production, all there is important reality and social meaning.
Since the appearance having cyanide wastewater, people begin to the treatment research to cyanide wastewater, for a long time, with section
The continuous development of technology, has been provided with seven big class, 20 kinds of processing methods up till now.So far, application is most, and compares
Generally the alkaline oxygenated method in the chemical oxidization method of chemical classes is hypochlorite oxidation method, and this method was applied from nineteen forty-two
In commercial production, technics comparing is ripe, stable, reliability, low cost are a little, be easy to automatic control.But, sodium hypochlorite available chlorine content
Low, effect duration is short, is difficult to store, dosage is big, produces the quantity of slag also greatly, freight volume is big, and broken cyanide ability is also lower slightly, and impact resistance is poor,
Processing cost is not also very good；Particularly to the enterprise being intended to Treated sewage reusing, energy efficient, also not very good.With containing
The increasingly increase of cyanogen wastewater flow rate, the raising containing cyanogen amount, it is difficult to meet this waste water only with these simple treatment technology methods
The stable operation processing and the needs of reuse, but there is presently no the more preferable processing method of discovery, it is therefore desirable at cyanide wastewater
The continuous lifting of reason technology, preferably process, reuse technology have become problem urgently to be resolved hurrily to expect one.
In order to change above situation, solve customer demand, to adapt to the needs of economic development and environmental conservation, we are directed to
Cyanide wastewater, on improving treatment effect, is prepared high-pure chlorinedioxide using excessively former conventional generator and to be replaced sodium hypochlorite and carry out
Process, although broken cyanide effect is highly desirable, chlorine dioxide adding of agent cannot realize automatic control, very easily excessive, to the filter membrane longevity
Life also can impact, and brings loss, and feedwater reuse brings unfavorable factor；And it is high to consume alkali, increased processing cost, operation
Trouble.Therefore, we have carried out corresponding many research under with reference to on-site actual situations again and have tested, to change traditional place
Reason technical method, and the deficiency of the former high-pure chlorinedioxide generator of single application, research design go out one more preferably, more suitable
Preferably, more energy efficient equipment and technical method.
Content of the invention
The technology of the present invention be defect according to former conventional processing technique method and single employing chlorine dioxide treatment not
Foot, provides and a kind of carries out wastewater treatment using strong oxidizer high-pure chlorinedioxide with former oxidizing agent sodium hypochlorite's method of combining
Technology, and can not need to change a kind of method of former handling process.First have to adopt high-pure chlorinedioxide, particularly will adopt
The high-pure chlorinedioxide prepared with low acid system technology, this technical method is using adding most of chlorine dioxide online, strong by it
Oxidisability, breaks CN-The complexation of ion, to remaining CN-Ion, then add liquor natrii hypochloritises, make broken cyanide completely up to standard, so
By coagulating sedimentation, and pass through membrane filtration, finally make wastewater treatment up to standard, then be back in production.
A kind of cyanide wastewater processes the method with reuse, comprises the steps：
(A) cyanide wastewater sent on production line is sent in the first oxidation reaction pond, add high-pure chlorinedioxide successively
And alkali liquor, mix and blend；
(B) the reacted waste water of step (A), from flowing in the second oxidation reaction pond, adds sodium hypochlorite, mix and blend；
(C) the reacted waste water of step (B) and adds flocculant, mix and blend from inflow flocculation basin；
(D) waste water in step (C) flows into sedimentation tank；
(E) copper-contained sludge that sedimentation tank is isolated is delivered to pressure filter filter pressing, mud outward transport after filter；Supernatant sends to film mistake
Filter equipment filter, finally qualified water up to standard again reuse to production and application.
Cyanide wastewater of the present invention process and reuse method, wherein, pH value in described first oxidation reaction pond
Control 10～11, the mix and blend time is 15～25 minutes；PH value in described second oxidation reaction pond controls 9.5～
10, the mix and blend time is 15～25 minutes；The mix and blend time in flocculation basin is 15～25 minutes；Precipitation in sedimentation tank
Time is 15～25 minutes.
Cyanide wastewater of the present invention processes the method with reuse, and wherein, described high-pure chlorinedioxide is using low acid
Amount prepares the high-pure chlorinedioxide that the method for chlorine dioxide prepares.
Cyanide wastewater of the present invention processes the method with reuse, wherein, in step (B), described high-purity the two of addition
Chlorine monoxid is 1 with the mass ratio of described sodium hypochlorite:2～7, during addition, evenly carry out in described second oxidation reaction pond
The adding of sodium hypochlorite, and control ORP 500～650.
Cyanide wastewater of the present invention processes the method with reuse, wherein,
Described flocculant is the 0.1%PAM of the PAC and 20～60L/h of the 10% of 30～70L/h；
The supernatant that sedimentation tank is isolated, adds any reducing agent to control ORP between 200～500, regulates water
After matter oxidisability, send to membrane filter system filter, finally qualified water up to standard again reuse to production and application.
Cyanide wastewater of the present invention processes the method with reuse, and wherein, described low acid amount prepares the side of chlorine dioxide
Method comprises the steps：
P3 solution and sulfuric acid solution are added in preparation facilitiess and carry out reaction generation chlorine dioxide, in course of reaction
In persistently carry out aeration；Described P3 solution concentration is 40～46%, and described sulfuric acid solution concentration is 70～75%, described P3 solution
Mol ratio with sulfuric acid solution is 1：1.07～1.16, and the volume ratio of described P3 solution and sulfuric acid solution is 1：0.48～1：
0.56；The reaction of described P3 solution and sulfuric acid solution divides first, second, third three-level to carry out, and above-mentioned third-order reaction is mutually only
Carry out in three vertical reactors, the reaction temperature of described first, second order reaction is 65～70 DEG C, described third level reaction
Reaction temperature be 68～73 DEG C.
Cyanide wastewater of the present invention processes the method with reuse, and wherein, described low acid amount prepares the side of chlorine dioxide
Method equipment therefor includes A reactor, second reactor and the three reactor being sequentially connected, described one-level, second reactor
Between and described two grades, three reactor between respectively pass through the first overflow pipe, second overflow pipe connection, described A reactor
On be connected with P3 solution conveyor tube road, sulfuric acid solution transfer pipeline and aeration tube, described one-level, two grades, three reactor top
It is respectively connected with a relief tube, described three reactor top is also associated with exhaust tube, described three reactor is provided with heating
Device；
Described A reactor is tank-like body, and described tank-like body inner wall lower is fixed with several transverse baffles, described
Each transverse baffle sets gradually from high to low, described P3 solution conveyor tube road, sulfuric acid solution transfer pipeline and aeration tube and tank
The junction point of shape body is respectively positioned on below minimum transverse baffle；
Described second reactor is tank-like body, and the tank-like body inwall constituting second reactor is fixed with vertical deflection plate, institute
State vertical deflection plate for L-shaped and described vertical deflection plate extends to bottom from the top of described tank-like body, described first overflow
Pipe is located at the top of described tank-like body and is located at described vertical folding with the junction point of the described tank-like body constituting second reactor
The lower section of stream plate；
Described three reactor is tank-like body, and described heater is electromagnetic induction heater, described electromagnetic induction heating
Device is coated on the tank-like body outer wall constituting three reactor.
Cyanide wastewater of the present invention processes the method with reuse, and wherein, described A reactor, second reactor are equal
It is made up of PVC material, described three reactor is made of titanium, the feed end on described P3 solution conveyor tube road, sulfuric acid solution conveying
The inlet end of the feed end of pipeline and described aeration tube all in the same plane, and the charging on described P3 solution conveyor tube road
End, the feed end of sulfuric acid solution transfer pipeline and the inlet end angle of described aeration tube are 60 °；
Described A reactor, second reactor and three reactor are triangularly arranged；
The junction point of described first overflow pipe and described A reactor is located at described A reactor top, and described second
The junction point of overflow pipe and described second reactor is located at the top of described second reactor, described second overflow pipe and described three
The junction point of stage reactor is located at the bottom of described three reactor.
A kind of cyanide wastewater of the present invention processes the device used by method with reuse, including the dioxy being sequentially connected
Change chlorine broken cyanide device, chlorine dioxide water sprayer, cyanide wastewater processing pond and film filter, described cyanide wastewater processing pond include according to
First oxidation reaction pond of secondary connection, the second oxidation reaction pond, flocculation basin and sedimentation tank, described sedimentation tank also with filter press
It is connected；Described cyanide wastewater is processed and the device of reuse also includes circulating pump, the entrance of described circulating pump and described first oxidation
The bottom of reaction tank is connected, and the outlet of described circulating pump is connected with the entrance of described chlorine dioxide water sprayer；Described filter press
The upper entrance of machine is connected with the lower part outlet of described sedimentation tank, and the lower part outlet of described filter press connects sludge outlet pipe
Road；The entrance of described film filter is connected with the outlet of sedimentation tank, the outlet of described film filter and wastewater outlet reuse pipeline
It is connected.
Cyanide wastewater of the present invention processes the device used by method with reuse, wherein, anti-in the described first oxidation
It is provided with agitating device in Ying Chi, described second oxidation reaction pond and described flocculation basin；The going out of described chlorine dioxide water sprayer
Mouth connects the entrance in described first oxidation reaction pond by the first pipeline, and described first pipeline extend into described first oxidation reaction
The bottom in pond；；The top in described first oxidation reaction pond is connected with waste water inlet pipeline and sodium hydroxide inlet ductwork respectively, institute
The top stating the second oxidation reaction pond is connected with sodium hypochlorite inlet's pipeline, the top of described flocculation basin respectively with PAC inlet tube
Road is connected with PAM inlet ductwork.
Cyanide wastewater of the present invention is processed and the method difference from prior art of reuse is：
Part I：
The side adding high-pure chlorinedioxide and sodium hypochlorite Treatment of Cyanide-containing Wastewater online in proportion step by step of the present invention
Method compared with existing traditional processing method, the main distinction be employ the higher chlorine dioxide of oxidisability first carry out most
Process, greatly reduce freight volume, storage capacity, dosage and the product quantity of slag of sodium hypochlorite, broken cyanide effect is ideal, is processed into
This is low, and impact resistance is strong, can tackle wastewater flow rate and the suddenly change containing cyanogen amount；The supplement recycling sodium hypochlorite adds, and makes brokenly
Cyanogen is up to standard, also can achieve the automatic operation of waste water final process it is ensured that stablizing of cyanide wastewater process is carried out simultaneously, particularly exists
While broken cyanide, to reduction COD and Cu2+Deng suffering from more preferable process effect；Meanwhile, adopt former conventional generator with independent
Prepare chlorine dioxide method to compare, the main distinction is preferably to solve the problems, such as that chlorine dioxide broken cyanide device cannot realize automatic control,
The excess avoiding medicament adds, and can preferably expensive filter membrane be protected, and extends its life-span, can reduce larger
Loss, so that waste water up to standard can steadily reuse be produced, and preparation cost is low, and broken cyanide alkali consumption is few, and processing cost is low, this
For the enterprise of Treated sewage reusing must having particularly significant meaning.This handling process method, because being not required to carry out big change, can be adopted
With raw wastewater processing meanss it is only necessary to the adjustment of individual tubes, greatly reduce water process workload, decrease construction investment,
Not only facilitate operation, reduce cost, and wastewater treatment can be made integrated with reclaiming system, make processing meanss operation side
Just, operate steadily, clearly, waste water completely can up to standard, reuse for treatment effect.This handling process method is that domestic do not had
, it is once that new innovation is attempted, be that cyanide wastewater is processed, reuse provides a new equipment and technical method.
Of the present invention add online high-pure chlorinedioxide and sodium hypochlorite Treatment of Cyanide-containing Wastewater method in proportion step by step
Compared with additive method, great advantage is that broken cyanide effect is ideal, is that traditional treatment method can not be compared, low cost,
Decrease a lot of workloads, adding of agent achieves automatic control, easy to operate, stable, be effectively protected the longevity of filter membrane
Life, has reached the purpose of Treated sewage reusing, has been that enterprise reduces expense, received client's height favorable comment, greatly meet client
Needs.
In preferred version, highlighting high-pure chlorinedioxide of the present invention is the method preparation preparing chlorine dioxide using low acid amount
The high-pure chlorinedioxide obtaining；The described high-pure chlorinedioxide adding is 1 with the mass ratio of described sodium hypochlorite:2～7, add
When, evenly in described second oxidation reaction pond, carry out adding of sodium hypochlorite, and control ORP 500～650, this step
Addition in rapid and method are both for preparing, in the low acid amount using the present invention, the height that the method for chlorine dioxide prepares
For pure chlorine dioxide, using rear effect is significant, common chlorine dioxide does not reach so more preferable effect.
Part II：
In the preferred technical solution of the present invention, the high-pure chlorinedioxide of employing is the chlorine dioxide of low acid amount preparation, this side
In method, reaction is carried out using P3 solution and sulfuric acid solution and produce lasting aeration in chlorine dioxide, and course of reaction, change
Former traditional ternary method preparation method and formula, are a kind of original new technologies, compared with former high-purity process of preparing, system
During standby, not only sulfuric acid dosage is few, it is low to consume, and feed stock conversion is high, low cost, and its former ternary method cost is 0.01569
Unit/g, now low acid system cost be only 0.01072 yuan/g, be the least cost of domestic high-purity preparation method it is often more important that, reaction
The residual liquid amount producing afterwards is few, acid content few (specifically seeing attached list), be truly realized domestic high-purity preparation method minimum with acid amount,
Maximum conversion, least cost, minimum residual liquid amount, minimum residual acid amount, greatly meet the different demands of client, solve visitor
The desired always problem reducing with acid amount, reducing residual liquid amount, reduce cost in family, and the purity of chlorine dioxide that the method is obtained
High, activity is high, and sterilization, sterilization, oxidation stain thing effect are preferable, can meet the water process needs of various places, especially to relatively
Intractable industrial wastewater provides processing method it is ensured that the water treatment efficiency in later stage can be up to standard, has reached high-purity preparation side
The best level of method, has filled up the market vacancy.
In addition, P3 solution concentration is 40～46%, sulfuric acid solution concentration is rubbing of 70～75%, P3 solution and sulfuric acid solution
That ratio is 1：1.07～1.16, and the volume ratio of P3 solution and sulfuric acid solution is 1：0.48～0.56, using above-mentioned solution concentration
Reach material balance and heat balance it is ensured that reaction is fully carried out, both ensure that the acidity of reaction mother liquor, also enable reaction
Safe and stable, rapidly carry out；
Further, because the present invention low acid amount prepares the reaction point three-level of P3 solution and sulfuric acid solution in the method for chlorine dioxide
Carry out, third-order reaction is carried out in three separate reactors, while ensureing residence time of material, so that material is obtained
Sufficient radiating and heating, it is separate to carry out three warm single controls, third-order reaction in course of reaction, increased the stream of reaction mother liquor
Dynamic course, constantly changes micromixing effect, improves the admixture of reaction mother liquor, promotes W-response speed, improves reaction
Effect, its feed stock conversion can be more than more than 98%, has reached the advanced level of domestic high-pure chlorinedioxide technology of preparing.
Because apparatus of the present invention include the A reactor, second reactor and the three reactor that are sequentially connected, change
Former ternary method, only with single structure of reactor form, is equivalent to and for course of reaction to be divided into premix section, hybrid reaction section and
End reaction section, while extending residence time of material, makes material obtain sufficient radiating and heat；
Further, due to being fixed with transverse baffle in A reactor, in second reactor, it is fixed with vertical deflection plate, the
One overflow pipe is located at A reactor top, the junction point of the second overflow pipe and second reactor with the junction point of A reactor
Positioned at the top of second reactor, the junction point of the second overflow pipe and three reactor is located at the bottom of three reactor, makes anti-
Answer mother solution constantly to change admixture under aeration, there is the time of staying of abundance, improve materials conversion rate further, accelerate anti-
Answer speed, meanwhile, also solve heat dissipation problem well；
Further, A reactor, second reactor and three reactor are triangularly arranged, high safety, compact conformation,
Equipment volume is much smaller than the volume of ternary method.
Part III：
The device that the method for the invention adopts is partially improved to pipeline, adds, have adjusted equipment component, it is to avoid
Big construction investment is so that it may realize adding the technical method of high-pure chlorinedioxide and sodium hypochlorite, medicine online in proportion step by step
Agent adds and achieves automatic control, easy to operate, greatly reduces water process workload, not only facilitates operation, reduces cost, resists
Impact is strong, can tackle wastewater flow rate and the suddenly change containing cyanogen amount；And wastewater treatment can be made integrated with reclaiming system, make place
Reason device is easy to operate, operates steadily, clearly, waste water completely can be with reuse up to standard for treatment effect.This handling process method
It is domestic unexistent, is once that new innovation is attempted, be that cyanide wastewater is processed, reuse provides a new technical method.
Compared with prior art, great advantage is that broken cyanide effect is ideal to assembly of the invention, is traditional treatment method
Can not compare, adding of agent achieves automatic control, easy to operate, stable, it is effectively protected the life-span of filter membrane, keep away
Exempt from big loss, reached the purpose of Treated sewage reusing, be that enterprise reduces expense, receive client's height favorable comment, greatly
Meet the needs of client.
Below in conjunction with the accompanying drawings the cyanide wastewater of the present invention is processed and the method for reuse is described further.
Brief description
Fig. 1 processes the structural representation with the device of the method for reuse for cyanide wastewater of the present invention；
Fig. 2 is the structural representation of the device that low acid amount prepares chlorine dioxide in the present invention；
Fig. 3 prepares P3 solution conveyor tube road, sulfuric acid solution transfer pipeline in the device of chlorine dioxide for the present invention low acid amount
And the connection diagram of aeration tube and A reactor.
Specific embodiment
Embodiment 1
(A) cyanide wastewater sent on production line is sent in the first oxidation reaction pond, add high-pure chlorinedioxide successively
And alkali liquor, mix and blend；
(B) the reacted waste water of step (A), from flowing in the second oxidation reaction pond, adds sodium hypochlorite, mix and blend；
(C) the reacted waste water of step (B) and adds flocculant, mix and blend from inflow flocculation basin；
(D) waste water in step (C) flows into sedimentation tank；
(E) copper-contained sludge that sedimentation tank is isolated is delivered to pressure filter filter pressing, mud outward transport after filter；Supernatant sends to film mistake
Filter equipment filter, finally qualified water up to standard again reuse to production and application.
Embodiment 2
A kind of cyanide wastewater is processed and the method for reuse is added in proportion step by step using high-pure chlorinedioxide and sodium hypochlorite
Method, is carried out as follows：
(1) by the cyanide wastewater sent on production line, mainly contain CN-、Cu2+, the component such as COD, be sent to the first oxidation
In reaction tank, add high-pure chlorinedioxide first；Meanwhile, add alkali liquor, pH controls 10～11 about, mix and blend 15～25
Minute, abolish most of CN-Ion, makes Cu2+Heavy metal separate out, generates Cu (OH)2Colloid substances；
(2) by reacted for step (1) waste water from flowing into the second oxidation reaction pond, add sodium hypochlorite in right amount, pH controls
9.5～10 about, abolish remaining a small amount of CN-Ion；Wherein, the ratio according to chlorine dioxide and sodium hypochlorite is 1:2～7
(mass ratio) adds, at the uniform velocity carry out adding of sodium hypochlorite in the second oxidation reaction pond, and control ORP left 500～650
The right side, through mix and blend 15～25 minutes, using the strong oxidizing property of chlorine dioxide and the oxidisability of sodium hypochlorite, is breaking in a large number
Except CN-After ion, it is supplemented with abolishing remaining CN-Ion, is allowed to form free state material, clears up CN-, the component such as COD, make
Cu2+Separate out, regeneration Cu (OH)2Colloid substances；
(3) by the waste water of step (2) from flowing into flocculation basin, add flocculant, mix and blend 15～25 minutes, make Cu
(OH)2Colloid substances flocculate into bulky grain thing；Flocculant is the 0.1% of the PAC and 20～60L/h of the 10% of interpolation 30～70L/h
PAM；
(4) waste water of step (3) is flowed into sedimentation tank, stop 15～25 minutes, make the cupric of bulky grain copper colloid substances dirty
Mud is realized precipitating completely, is separated from water, and removes Cu2+；
(5) copper-contained sludge isolating step (4) delivers to pressure filter filter pressing, mud outward transport after filter；The supernatant isolated
Liquid, controls ORP 200～500 to add the amount of any reducing agent, after regulating water quality oxidisability, sends to membrane filter system mistake
Filter, finally qualified water up to standard again reuse to production and application.
Embodiment 3
It is with the difference of embodiment 2, the low acid system of raw material high-pure chlorinedioxide of employing prepares, effect
More preferably, it is preferred version on the basis of embodiment 2, other steps are with embodiment 2.
Embodiment 4
Cyanide wastewater is sent in the first oxidation reaction pond, first adds a large amount of high-pure chlorinedioxides, meanwhile, add alkali liquor,
PH is controlled to be 10, mix and blend 20 minutes, waste water flows into the second oxidation reaction pond certainly, according to chlorine dioxide and sodium hypochlorite 1:7
The ratio of (mass ratio), then add sodium hypochlorite, controls pH to be 9.5, and controls ORP to be 560, through mix and blend 15 minutes,
Waste water from flowing into flocculation basin, adds the 0.1%PAM of 10% PAC and 30L/h of 60L/h, mix and blend 15 minutes, waste water again
Flow into sedimentation tank again, stop 25 minutes, so that copper-contained sludge is precipitated completely, be separated from water；The supernatant isolated controls ORP400
To add reducing agent, then send to filtration film device filter, finally qualified water up to standard again reuse to production and application.
Cyanide wastewater processes and takes a sample test result：Free cyanogen content 0.08mg/L.
Embodiment 5
Cyanide wastewater is sent in the first oxidation reaction pond, first adds a large amount of high-pure chlorinedioxides, meanwhile, add alkali liquor,
PH is controlled to be 11, mix and blend 15 minutes, waste water flows into the second oxidation reaction pond certainly, according to chlorine dioxide and sodium hypochlorite 1:2
The ratio of (mass ratio), adds sodium hypochlorite, controls pH to be 10, and controls ORP to be 600, through mix and blend 20 minutes, waste water
Again from flowing into flocculation basin, add the 0.1%PAM of 10% PAC and 20L/h of 70L/h, mix and blend 25 minutes, waste water flows again
Enter sedimentation tank, stop 20 minutes, so that copper-contained sludge is precipitated completely, be separated from water；The supernatant isolated controls ORP500 to add
Plus reducing agent, then send to filtration film device filter, finally qualified water up to standard again reuse to production and application.
Cyanide wastewater processes and takes a sample test result：Free cyanogen content 0.04mg/L.
Embodiment 6
Cyanide wastewater is sent in the first oxidation reaction pond, first adds a large amount of high-pure chlorinedioxides, meanwhile, add alkali liquor,
PH is controlled to be 10.5, mix and blend 15 minutes, waste water flows into the second oxidation reaction pond certainly, according to chlorine dioxide and sodium hypochlorite 1:
The ratio of 4 (mass ratioes), adds sodium hypochlorite, controls pH to be 10, and controls ORP to be 650, through mix and blend 25 minutes, gives up
Water from flowing into flocculation basin, adds the 0.1%PAM of 10% PAC and 50L/h of 40L/h, mix and blend 20 minutes, waste water is more again
Flow into sedimentation tank, stop 15 minutes, so that copper-contained sludge is precipitated completely, be separated from water；The supernatant isolated controls ORP200 to come
Add reducing agent, then send to filtration film device filter, finally qualified water up to standard again reuse to production and application.
Cyanide wastewater processes and takes a sample test result：Free cyanogen content 0.07mg/L.
Embodiment 7
Cyanide wastewater is sent in the first oxidation reaction pond, first adds a large amount of high-pure chlorinedioxides, meanwhile, add alkali liquor,
PH is controlled to be 11, mix and blend 20 minutes, waste water flows into the second oxidation reaction pond certainly, according to chlorine dioxide and sodium hypochlorite 1:5
The ratio of (mass ratio), adds sodium hypochlorite, controls pH to be 9.5, and controls ORP to be 500, through mix and blend 25 minutes, gives up
Water from flowing into flocculation basin, adds the 0.1%PAM of 10% PAC and 40L/h of 30L/h, mix and blend 20 minutes, waste water is more again
Flow into sedimentation tank, stop 20 minutes, so that copper-contained sludge is precipitated completely, be separated from water；The supernatant isolated controls ORP300 to come
Add reducing agent, then send to filtration film device filter, finally qualified water up to standard again reuse to production and application.
Cyanide wastewater processes and takes a sample test result：Free cyanogen content 0.05mg/L.
Explanation：In embodiment 4-7, the high-pure chlorinedioxide of employing is the high-pure chlorinedioxide of low acid system preparation, is excellent
Choosing method, also enables the purpose of the present invention using additive method (chlorine dioxide that such as ternary method prepares), also at this
Invention protection domain within, but from effect for, more preferable using low acidic process waste water effect.
Embodiment 8
Using high-pure chlorinedioxide be the preparation of low acid system high-pure chlorinedioxide, the method that low acid amount prepares chlorine dioxide
Comprise the steps：
P3 solution and sulfuric acid solution are added in preparation facilitiess and carry out reaction generation chlorine dioxide, in course of reaction
In persistently carry out aeration；P3 solution concentration is 40～46%, and sulfuric acid solution concentration is 70～75%, P3 solution and sulfuric acid solution
Mol ratio is 1：1.07～1.16, and the volume ratio of P3 solution and sulfuric acid solution is 1：0.48～1：0.56；P3 solution and sulphuric acid
The reaction of solution divides first, second, third three-level to carry out, and above-mentioned third-order reaction is carried out in three separate reactors,
The reaction temperature of first, second order reaction is 65～70 DEG C, and the reaction temperature of third level reaction is 68～73 DEG C.
As shown in Figures 2 and 3, the method equipment therefor that low acid amount prepares chlorine dioxide includes the first order reaction being sequentially connected
Device 11, second reactor 12 and three reactor 13, distinguish between one-level, second reactor and between two grades, three reactor
Connected by the first overflow pipe 14, the second overflow pipe 15, A reactor 11 is connected with P3 solution conveyor tube road 21, sulphuric acid molten
Liquid transfer pipeline 22 and aeration tube 23, one-level, two grades, three reactor top be respectively connected with a relief tube, three reactor 13
Top is also associated with exhaust tube 24, and three reactor 13 is provided with heater；
A reactor 11 is tank-like body, and tank-like body inner wall lower is fixed with several transverse baffles 111, each horizontal folding
Stream plate 111 sets gradually from high to low, P3 solution conveyor tube road 21, sulfuric acid solution transfer pipeline 22 and aeration tube 23 and tank-like body
Junction point be respectively positioned on below minimum transverse baffle；
Second reactor 12 is tank-like body, and the tank-like body inwall constituting second reactor 12 is fixed with vertical deflection plate 121,
Vertical deflection plate 121 is L-shaped and vertical deflection plate 121 extends to bottom from the top of tank-like body, the first overflow pipe 14 and structure
The junction point becoming the tank-like body of second reactor 12 is located at the top of tank-like body and is located at the lower section of vertical deflection plate 121；
Three reactor 13 is tank-like body, and heater is electromagnetic induction heater 131, and electromagnetic induction heater 131 wraps
Overlay on the tank-like body outer wall constituting three reactor 13.
A reactor 11, second reactor 12 are made by PVC material, and three reactor 13 is made of titanium, P3 solution
The inlet end of the feed end of transfer pipeline 21, the feed end of sulfuric acid solution transfer pipeline 22 and aeration tube 23 is all in same plane
Interior, and the inlet end of the feed end, the feed end of sulfuric acid solution transfer pipeline 22 and aeration tube 23 on P3 solution conveyor tube road 21
Angle is 60 °；
A reactor 11, second reactor 12 and three reactor 13 are triangularly arranged；
The junction point of the first overflow pipe 14 and A reactor 11 is located at A reactor 11 top, the second overflow pipe 15 with
The junction point of second reactor 12 is located at the top of second reactor, the junction point position of the second overflow pipe 15 and three reactor 13
Bottom in three reactor 13.
Supplementary notes：
The present invention low acid amount prepares the embodiment of the method one of chlorine dioxide
P3 solution by 40% mixed liquor of C catalyst (sodium chlorate with) and 71% dilution heat of sulfuric acid respectively through P3 solution
Transfer pipeline 21, sulfuric acid solution transfer pipeline 22 add in A reactor 11, and 40% P3 solution and 71% dilute sulfuric acid are molten
The mol ratio of liquid is 1：1.07th, volume ratio is 1：0.5, in A reactor 11, P3 solution and dilution heat of sulfuric acid react shape
Become reaction mother liquor, aeration tube 23 continues aeration during the course of the reaction, above-mentioned reaction mother liquor enters two grades instead through the first overflow pipe 14
Answer device 12, enter three reactor 13 through the second overflow pipe 15 after reacting in second reactor 12, reaction mother liquor is through above-mentioned
Three reactor sufficiently mixes, and reacts fully and carries out, and finally gives high-purity, highly active chlorine dioxide, through taking out
Trachea 24 is delivered in processed water body, the reaction temperature of A reactor 11 naturally maintain 65 DEG C, second reactor 12 anti-
Temperature is answered naturally to be maintained 65 DEG C, control system controls heater, under the automatically controlling of control system, three reactor 13
Interior reaction temperature is maintained at 68 DEG C, and its reaction principle is as follows：
NaClO3(+C)+H2SO4→ClO2↑+Na2SO4+H2O+O2↑
In above-mentioned preparation process, scene is sampled analysis detection, testing result to three reactor 13：Chlorine dioxide
Gas purity is 99.91%, and feed stock conversion is 98.4%.
The present invention low acid amount prepares the embodiment of the method two of chlorine dioxide
P3 solution by 43% mixed liquor of C catalyst (sodium chlorate with) and 75% dilution heat of sulfuric acid respectively through P3 solution
Transfer pipeline 21, sulfuric acid solution transfer pipeline 22 add in A reactor 11, and 43% P3 solution and 75% dilute sulfuric acid are molten
The mol ratio of liquid is 1：1.1st, volume ratio is 1：0.52, in A reactor 11, P3 solution and dilution heat of sulfuric acid react shape
Become reaction mother liquor, aeration tube 23 continues aeration during the course of the reaction, above-mentioned reaction mother liquor enters two grades instead through the first overflow pipe 14
Answer device 12, enter three reactor 13 through the second overflow pipe 15 after reacting in second reactor 12, reaction mother liquor is through above-mentioned
Three reactor sufficiently mixes, and reacts fully and carries out, and finally gives high-purity, highly active chlorine dioxide, through taking out
Trachea 24 is delivered in processed water body, the reaction temperature of A reactor 11 naturally maintain 70 DEG C, second reactor 12 anti-
Temperature is answered naturally to be maintained 69 DEG C, control system controls heater, under the automatically controlling of control system, three reactor 13
Interior reaction temperature is maintained at 70 DEG C, and its reaction principle is as follows：
NaClO3(+C)+H2SO4→ClO2↑+Na2SO4+H2O+O2↑
In above-mentioned preparation process, scene is sampled analysis detection, testing result to three reactor 13：Chlorine dioxide
Gas purity is 99.96%, and feed stock conversion is 98.9%.
The present invention low acid amount prepares the embodiment of the method three of chlorine dioxide
P3 solution by 44% mixed liquor of C catalyst (sodium chlorate with) and 72% dilution heat of sulfuric acid respectively through P3 solution
Transfer pipeline 21, sulfuric acid solution transfer pipeline 22 add in A reactor 11, and 44% P3 solution and 72% dilute sulfuric acid are molten
The mol ratio of liquid is 1：1.09th, volume ratio is 1：0.56, in A reactor 11, P3 solution and dilution heat of sulfuric acid react
Form reaction mother liquor, aeration tube 23 continues aeration during the course of the reaction, above-mentioned reaction mother liquor enters two grades through the first overflow pipe 14
Reactor 12, enters three reactor 13 through the second overflow pipe 15 after reacting, reaction mother liquor is through upper in second reactor 12
State three reactor sufficiently to mix, react fully and carry out, finally give high-purity, highly active chlorine dioxide, warp
Exhaust tube 24 is delivered in processed water body, and the reaction temperature of A reactor 11 maintains 70 DEG C, second reactor 12 naturally
Reaction temperature is maintained 70 DEG C naturally, and control system controls heater, under the automatically controlling of control system, three reactor
Reaction temperature in 13 is maintained at 73 DEG C, and its reaction principle is as follows：
NaClO3(+C)+H2SO4→ClO2↑+Na2SO4+H2O+O2↑
In above-mentioned preparation process, scene is sampled analysis detection, testing result to three reactor 13：Chlorine dioxide
Gas purity is 99.94%, and feed stock conversion is 99.03%.
The present invention low acid amount prepares the embodiment of the method four of chlorine dioxide
P3 solution by 46% mixed liquor of C catalyst (sodium chlorate with) and 70% dilution heat of sulfuric acid respectively through P3 solution
Transfer pipeline 21, sulfuric acid solution transfer pipeline 22 add in A reactor 11, and 45% P3 solution and 70% dilute sulfuric acid are molten
The mol ratio of liquid is 1：1.16th, volume ratio is 1：0.48, in A reactor 11, P3 solution and dilution heat of sulfuric acid react
Form reaction mother liquor, aeration tube 23 continues aeration during the course of the reaction, above-mentioned reaction mother liquor enters two grades through the first overflow pipe 14
Reactor 12, enters three reactor 13 through the second overflow pipe 15 after reacting, reaction mother liquor is through upper in second reactor 12
State three reactor sufficiently to mix, react fully and carry out, finally give high-purity, highly active chlorine dioxide, warp
Exhaust tube 24 is delivered in processed water body, and the reaction temperature of A reactor 11 maintains 69 DEG C, second reactor 12 naturally
Reaction temperature is maintained 68 DEG C naturally, and control system controls heater, under the automatically controlling of control system, three reactor
Reaction temperature in 13 is maintained at 71 DEG C, and its reaction principle is as follows：
NaClO3(+C)+H2SO4→ClO2↑+Na2SO4+H2O+O2↑
In above-mentioned preparation process, scene is sampled analysis detection, testing result to three reactor 13：Chlorine dioxide
Gas purity is 99.95%, and feed stock conversion is 98.7%.
The present invention low acid amount prepares the method for chlorine dioxide and the comparison sheet of traditional ternary method is as follows：
Embodiment 9
On the basis of embodiment 1～8, present invention also offers a kind of preferred device for the inventive method, tool
Body is as follows：
As shown in figure 1, a kind of cyanide wastewater processes the device with reuse, including the chlorine dioxide broken cyanide device being sequentially connected
1st, chlorine dioxide water sprayer 2, cyanide wastewater processing pond and film filter 9, cyanide wastewater processing pond includes first being sequentially communicated
Oxidation reaction pond 4, the second oxidation reaction pond 5, flocculation basin 6 and sedimentation tank 8, sedimentation tank 8 is also connected with filter press 7；Containing cyanogen
The device of wastewater treatment and reuse also includes circulating pump 3, and the entrance of circulating pump 3 is connected with the bottom in the first oxidation reaction pond 4, follows
The outlet of ring pump 3 is connected with the entrance of chlorine dioxide water sprayer 2.
Above scheme can achieve the purpose of the present invention, and on this basis, the present invention gives following preferred version again：
It is provided with agitating device 10 in the first oxidation reaction pond 4 second oxidation reaction pond 5 and flocculation basin 6；Titanium dioxide
The outlet of chlorine water emitter 2 connects the entrance in the first oxidation reaction pond 4 by the first pipeline 201, and the first pipeline 201 extend into first
The bottom in oxidation reaction pond 4.
The top in the first oxidation reaction pond 4 is connected with waste water inlet pipeline 401 and sodium hydroxide inlet ductwork 402 respectively,
The top in the second oxidation reaction pond 5 is connected with sodium hypochlorite inlet's pipeline 501, the top of flocculation basin 6 respectively with PAC inlet ductwork
601 are connected with PAM inlet ductwork 602；The upper entrance of filter press 7 is connected with the lower part outlet of sedimentation tank 8, filter press
The lower part outlet of machine 7 connects sludge outlet pipeline 701；The entrance of film filter 9 is connected with the outlet of sedimentation tank 8, film filter 9
Outlet be connected with wastewater outlet reuse pipeline 901.
Embodiment described above is only that the preferred embodiment of the present invention is described, the not model to the present invention
Enclose and be defined, on the premise of without departing from design spirit of the present invention, the technical side to the present invention for the those of ordinary skill in the art
Various modifications and improvement that case is made, all should fall in the protection domain of claims of the present invention determination.
Claims (10)
1. a kind of cyanide wastewater process and reuse method it is characterised in that：Comprise the steps：
(A) cyanide wastewater sent on production line is sent in the first oxidation reaction pond, add high-pure chlorinedioxide and alkali successively
Liquid, mix and blend；
(B) the reacted waste water of step (A), from flowing in the second oxidation reaction pond, adds sodium hypochlorite, mix and blend；
(C) the reacted waste water of step (B) and adds flocculant, mix and blend from inflow flocculation basin；
(D) waste water in step (C) flows into sedimentation tank；
(E) copper-contained sludge that sedimentation tank is isolated is delivered to pressure filter filter pressing, mud outward transport after filter；Supernatant is sent to membrane filtration and is set
Standby filter, finally qualified water up to standard again reuse to production and application.
2. cyanide wastewater according to claim 1 process and reuse method it is characterised in that：Described first oxidation reaction
PH value in pond controls 10～11, and the mix and blend time is 15～25 minutes；PH value control in described second oxidation reaction pond
9.5～10, the mix and blend time is 15～25 minutes to system；The mix and blend time in flocculation basin is 15～25 minutes；Precipitation
Sedimentation time in pond is 15～25 minutes.
3. cyanide wastewater according to claim 2 process and reuse method it is characterised in that：Described high-pure chlorinedioxide
It is that the high-pure chlorinedioxide that the method for chlorine dioxide prepares is prepared using low acid amount.
4. cyanide wastewater according to claim 3 process and reuse method it is characterised in that：In step (B), addition
Described high-pure chlorinedioxide is 1 with the mass ratio of described sodium hypochlorite:2～7, during addition, evenly anti-to the described second oxidation
Ying Chizhong carries out adding of sodium hypochlorite, and controls ORP 500～650.
5. cyanide wastewater according to claim 4 process and reuse method it is characterised in that：
Described flocculant is the 0.1%PAM of the PAC and 20～60L/h of the 10% of 30～70L/h；
The supernatant that sedimentation tank is isolated, adds any reducing agent to control ORP between 200～500, regulates water quality oxygen
Change property after, send to membrane filter system filter, finally qualified water up to standard again reuse to production and application.
6. cyanide wastewater according to claim 3 process and reuse method it is characterised in that：Described low acid amount preparation two
The method of chlorine monoxid comprises the steps：
P3 solution and sulfuric acid solution are added in preparation facilitiess and carry out reaction generation chlorine dioxide, hold during the course of the reaction
Continue and carry out aeration；Described P3 solution concentration is 40～46%, and described sulfuric acid solution concentration is 70～75%, described P3 solution and sulfur
The mol ratio of acid solution is 1：1.07～1.16, and the volume ratio of described P3 solution and sulfuric acid solution is 1：0.48～1：0.56；
The reaction of described P3 solution and sulfuric acid solution divides first, second, third three-level to carry out, and above-mentioned third-order reaction is separate three
Carry out in individual reactor, the reaction temperature of described first, second order reaction is 65～70 DEG C, the reaction of described third level reaction
Temperature is 68～73 DEG C.
7. cyanide wastewater according to claim 6 process and reuse method it is characterised in that：Described low acid amount preparation two
The method equipment therefor of chlorine monoxid includes A reactor (11), second reactor (12) and the three reactor being sequentially connected
(13), pass through respectively between described one-level, second reactor and between described two grades, three reactor the first overflow pipe (14),
Second overflow pipe (15) connects, and described A reactor (11) is connected with P3 solution conveyor tube road (21), sulfuric acid solution conveying
Pipeline (22) and aeration tube (23), described one-level, two grades, three reactor top be respectively connected with a relief tube, described three-level is anti-
Answer device (13) top to be also associated with exhaust tube (24), described three reactor (13) is provided with heater；
Described A reactor (11) is tank-like body, and described tank-like body inner wall lower is fixed with several transverse baffles (111),
Described each transverse baffle (111) sets gradually from high to low, described P3 solution conveyor tube road (21), sulfuric acid solution transfer pipeline
And the junction point of aeration tube (23) and tank-like body is respectively positioned on below minimum transverse baffle (22)；
Described second reactor (12) is tank-like body, and the tank-like body inwall constituting second reactor (12) is fixed with vertical deflection plate
(121), described vertical deflection plate (121) is L-shaped and described vertical deflection plate (121) extends to from the top of described tank-like body
Bottom, described first overflow pipe (14) is located at described tank-like body with the junction point of the described tank-like body constituting second reactor (12)
Top and be located at described vertical deflection plate (121) lower section；
Described three reactor (13) is tank-like body, and described heater is electromagnetic induction heater (131), described electromagnetic induction
Heater (131) is coated on the tank-like body outer wall constituting three reactor (13).
8. cyanide wastewater according to claim 7 process and reuse method it is characterised in that：Described A reactor
(11), second reactor (12) is made by PVC material, and described three reactor (13) is made of titanium, described P3 solution conveying
The inlet end of the feed end of pipeline (21), the feed end of sulfuric acid solution transfer pipeline (22) and described aeration tube (23) is all same
In plane, and the feed end of described P3 solution conveyor tube road (21), the feed end of sulfuric acid solution transfer pipeline (22) with described
The inlet end angle of aeration tube (23) is 60 °；
Described A reactor (11), second reactor (12) and three reactor (13) are triangularly arranged；
Described first overflow pipe (14) is located at described A reactor (11) top with the junction point of described A reactor (11),
The junction point of described second overflow pipe (15) and described second reactor (12) is located at the top of described second reactor, and described the
The junction point of two overflow pipes (15) and described three reactor (13) is located at the bottom of described three reactor (13).
9. a kind of cyanide wastewater described in claim 1 process and reuse the device used by method it is characterised in that：Including according to
Secondary connected chlorine dioxide broken cyanide device (1), chlorine dioxide water sprayer (2), cyanide wastewater processing pond and film filter (9), institute
State the first oxidation reaction pond (4) that cyanide wastewater processing pond includes being sequentially communicated, the second oxidation reaction pond (5), flocculation basin (6) and
Sedimentation tank (8), described sedimentation tank (8) is also connected with filter press (7)；Described cyanide wastewater is processed and the device of reuse also wraps
Include circulating pump (3), the entrance of described circulating pump (3) is connected with the bottom in described first oxidation reaction pond (4), described circulating pump
(3) outlet is connected with the entrance of described chlorine dioxide water sprayer (2)；The upper entrance of described filter press (7) with described
The lower part outlet of sedimentation tank (8) is connected, and the lower part outlet of described filter press (7) connects sludge outlet pipeline (701)；Described
The entrance of film filter (9) is connected with the outlet of sedimentation tank (8), the outlet of described film filter (9) and wastewater outlet reuse pipe
Road (901) is connected.
10. cyanide wastewater according to claim 9 process and reuse the device used by method it is characterised in that：Institute
State in the first oxidation reaction pond (4), described second oxidation reaction pond (5) and described flocculation basin (6) and be provided with agitating device
(10)；The outlet of described chlorine dioxide water sprayer (2) connects described first oxidation reaction pond (4) by the first pipeline (201)
Entrance, described first pipeline (201) extend into the bottom in described first oxidation reaction pond (4)；；Described first oxidation reaction pond
(4) top is connected with waste water inlet pipeline (401) and sodium hydroxide inlet ductwork (402) respectively, described second oxidation reaction
The top in pond (5) is connected with sodium hypochlorite inlet's pipeline (501), the top of described flocculation basin (6) respectively with PAC inlet ductwork
(601) it is connected with PAM inlet ductwork (602).
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