CN212425682U - Cyaniding cadmium plating electroplating wastewater treatment system - Google Patents
Cyaniding cadmium plating electroplating wastewater treatment system Download PDFInfo
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- CN212425682U CN212425682U CN202020693405.9U CN202020693405U CN212425682U CN 212425682 U CN212425682 U CN 212425682U CN 202020693405 U CN202020693405 U CN 202020693405U CN 212425682 U CN212425682 U CN 212425682U
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Abstract
The utility model discloses a cyanide cadmium plating electroplating wastewater treatment system, which comprises a cyanide-cadmium wastewater adjusting tank, a cyanide breaking reaction tank, a tail gas absorption tower, a primary vulcanization aeration tank, a cadmium slag inclined plate precipitation tank, a cadmium slag filter press, a secondary vulcanization aeration tank, a zinc slag inclined plate precipitation tank, a zinc slag filter press, a ceramic membrane filter, an organic membrane filter and a pH adjusting tank, wherein a tail gas outlet at the top of the cyanide breaking reaction tank is connected with a tail gas inlet at the lower part of the tail gas absorption tower through a pipeline, and a stirring port of the cyanide breaking reaction tank is connected with a spraying device at the upper part of the tail gas absorption tower through a pipeline; the cyanogen breaking reaction tank is provided with a feeding port for chlorine dioxide and sodium hydroxide; aeration pipes are arranged at the bottoms of the primary vulcanization aeration tank and the secondary vulcanization aeration tank and are connected with a mixed gas input pipe of hydrogen sulfide gas and compressed air. Adopt the utility model discloses it is effectual to handle cyanogen cadmium waste water, the use and the acid dosage of reducible broken cyanogen oxidant, alkaline precipitant reduce salt content such as Na salt in the waste water, reduce wastewater discharge.
Description
Technical Field
The utility model relates to the technical field of electroplating wastewater treatment, in particular to a cyaniding cadmium plating electroplating wastewater treatment system.
Background
Cadmium is a high-harm toxic substance and a carcinogenic substance, water, air, soil and food polluted by cadmium seriously harm human bodies, and the pain disease occurs in Japan once because of cadmium poisoning. In China, cadmium is classified as a pollutant, and the highest allowable discharge concentration of the total cadmium in the electroplating wastewater is 0.05mg/L according to the discharge standard of GB21900-2008 electroplating pollutants.
In the electroplating industry, cadmium-plated layers are commonly used for elastic parts, threaded parts, standard parts, aerospace, shipbuilding, electronic and military products, and the like. Cyanide electroplating has been replaced by cyanide-free electroplating in the common electroplating industry, but no alternative process technology exists in the fields of aerospace systems and the like.
The common methods for treating the wastewater containing Cd mainly comprise a chemical precipitation method, an electrolysis method, an ion resin exchange method, a membrane separation method and the like. In industry, most cadmium ions in wastewater are removed by a chemical precipitation method, and then advanced treatment is performed by methods such as ion exchange and membrane treatment. The chemical precipitation method is classified into cadmium carbonate precipitation, hydroxide precipitation, cadmium phosphate precipitation, cadmium sulfide precipitation, bleaching powder precipitation, ferrite coprecipitation, and the like. The most common chemical precipitation method of cadmium-containing wastewater is hydroxide precipitation, the pH value of cadmium ions fully precipitated is 11-12, and the problems of high reaction pH value, excessive Na ions introduced, high salt content of effluent, difficult wastewater recycling, difficult treatment of precipitated products, limited application range, easy re-dissolution of other heavy metals and the like exist. The cyanide cadmium plating electroplating wastewater treated by the conventional technology is difficult to meet the increasingly strict environmental protection requirement.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem of providing a cyanide cadmium plating electroplating wastewater treatment system with good treatment effect and improved wastewater reuse rate.
The utility model discloses solve above-mentioned technical problem with following technical scheme:
the utility model relates to a cyanide cadmium plating electroplating wastewater treatment system, include by preceding to the cyanogen cadmium wastewater equalizing basin that connects gradually after to, broken cyanogen reaction tank, tail gas absorption tower, the aeration tank of once vulcanizing, cadmium sediment inclined plate precipitation tank, cadmium sediment pressure filter, the aeration tank of second vulcanizing, zinc sediment inclined plate precipitation tank, zinc sediment pressure filter, ceramic membrane filter, organic membrane filter and pH equalizing basin, broken cyanogen reaction tank top is equipped with the tail gas export, the lower part is equipped with broken cyanogen reaction tank stirring mouth, the tail gas export at broken cyanogen reaction tank top is connected with the tail gas entry of tail gas absorption tower lower part through the pipeline, broken cyanogen reaction tank stirring mouth of broken cyanogen reaction tank lower part is connected with the spray set on tail gas absorption tower upper portion through the pipeline; the top parts of the tail gas absorption tower, the primary vulcanization aeration tank, the secondary vulcanization aeration tank and the pH adjusting tank are all provided with discharge ports connected with discharge pipelines, and tail gas discharge fans are arranged on the discharge pipelines; the cyanogen breaking reaction tank is provided with a feeding port for chlorine dioxide and sodium hydroxide; aeration pipes are arranged at the bottoms of the primary vulcanization aeration tank and the secondary vulcanization aeration tank and are connected with a mixed gas input pipe of hydrogen sulfide gas and compressed air.
And a cyanogen breaking stirring pump is arranged at the lower part of the cyanogen breaking reaction tank, and the waste water discharged from a stirring port of the cyanogen breaking reaction tank returns to the cyanogen breaking reaction tank through the cyanogen breaking stirring pump to realize stirring action.
The height to diameter ratio of the primary vulcanization aeration tank to the secondary vulcanization aeration tank is 1.0-1.2: 1; the pH value of the wastewater detected by the pH meter is arranged in the primary vulcanization aeration tank and the secondary vulcanization aeration tank.
Be equipped with pH meter and agitating unit in the pH adjusting tank, agitating unit includes the puddler, establishes the stirring leaf on the puddler and is used for driving puddler pivoted driving motor.
The treatment system is applied to the treatment of the cyanide-containing cadmium plating wastewater, and has the following beneficial effects:
1. compared with the conventional sodium hypochlorite oxidation technology, the utility model discloses a chlorine dioxide breaks cyanogen, hydroxide and hydrogen sulfide and precipitates the heavy metal in coordination, and the cyanogen cadmium waste water treatment effect is good, and the use of reducible broken cyanogen oxidant, alkaline precipitant and the acid content of using of pH callback reduce salt content such as Na salt in the retrieval and utilization waste water, be favorable to the waste water retrieval and utilization, reduce waste water discharge, can satisfy the environmental protection requirement that tends to be strict day by day, reduce electroplating production's water cost.
2. The utility model discloses a deposit the combination that deposits with the sulphide with the hydroxide method, the pH value that electroplating effluent cadmium ion deposits is reduced to 10 ~ 11 by 11 ~ 12, reduces the sulphuric acid quantity that waste water treatment alkali lye and follow-up pH were reversed and is transferred, has reduced medicine use cost.
3. The utility model discloses be favorable to the waste water retrieval and utilization. Compared with sodium sulfide precipitation, Na ions are not introduced into the sodium sulfide precipitation; only a small amount of sodium hydroxide is used for fine adjustment of the pH value in the wastewater treatment, and the amount of the sodium hydroxide for precipitating cadmium ions is reduced. The utility model discloses reduce the enrichment of handling back waste water Na ion, be favorable to the waste water retrieval and utilization, reduce wastewater discharge, can satisfy the environmental protection requirement that becomes stricter day by day, also reduced the water cost of electroplating.
4. The pH value of the wastewater treated by the organic membrane is 8.5-9.5, and the wastewater can be directly reused for electroplating production, so that the water reuse rate is improved, and the alkali consumption of NaOH in electroplating production can be reduced.
Drawings
Fig. 1 is a schematic structural diagram of a processing system adopted in embodiment 1 of the present invention.
Fig. 2 is a schematic structural diagram of a processing system adopted in embodiment 2 of the present invention.
In the figure: 1-a cyanogen-cadmium wastewater adjusting tank, 2-a conveying pump A, 3-a cyanogen breaking reaction tank, 31-a cyanogen breaking reaction tank stirring port, 4-a cyanogen breaking stirring pump, 5-a tail gas absorption tower, 51-a first-stage spraying device, 52-a second-stage spraying device, 6-a tail gas absorption tower circulating pump, 7-a primary vulcanization aeration tank, 71-a primary vulcanization aeration pipe, 8-a conveying pump B, 9-a cadmium slag inclined plate settling tank, 10-a cadmium slag filter press pump, 11-a cadmium slag filter press, 111-a cadmium slag hopper, 12-a cadmium removal clear liquid tank and 13-a conveying pump C; 14-a secondary vulcanization aeration tank, 141-a secondary vulcanization aeration pipe, 15-a conveying pump D, 16-a zinc slag inclined plate settling tank, 17-a zinc slag filter press pump, 18-a zinc slag filter press, 181-a zinc slag hopper, 19-a zinc removal clear liquid tank, 20-a ceramic membrane filtration high-pressure pump, 21-a ceramic membrane filter, 22-a ceramic filtration liquid tank, 23-an organic membrane filtration high-pressure pump, 24-an organic membrane filter, 25-an organic membrane filtration liquid tank, 26-a conveying pump E, 27-a pH adjusting tank, 271-a stirring device, 28-a conveying pump F, 29-a tail gas discharge fan and 30-a hydrogen sulfide generator.
Detailed Description
The technical solution of the present invention will be further described with reference to the accompanying drawings and embodiments.
Example 1
As shown in figure 1, the utility model discloses a cyanide cadmium plating electroplating wastewater treatment system, including from the front to the back through the process pipeline sequentially connected cyanogen cadmium wastewater adjusting tank 1, broken cyanogen reaction tank 3, tail gas absorption tower 5, the aeration tank 7 of once vulcanizing, cadmium slag inclined plate precipitation tank 9, cadmium slag filter press 11, cadmium removal clear liquid tank 12, the aeration tank 14 of twice vulcanizing, zinc slag inclined plate precipitation tank 16, zinc slag filter press 18, zinc removal clear liquid tank 19, ceramic membrane filter 21, ceramic filter liquid tank 22, organic membrane filter 24, organic membrane filter clear liquid tank 25 and pH adjusting tank 27, be equipped with delivery pump A2 on the connecting tube between cyanogen cadmium wastewater adjusting tank 1 and broken cyanogen reaction tank 3, the top of broken cyanogen reaction tank 3 is equipped with the tail gas export, and be equipped with chlorine dioxide and sodium hydroxide's throwing mouth, the lower part of broken cyanogen reaction tank 3 is equipped with broken cyanogen reaction tank stirring mouth 31, the tail gas export on the top of broken cyanogen reaction tank is connected with the tail gas entry of tail gas absorption tower 5 lower part through the pipeline, a cyanogen-breaking reaction tank stirring port 31 of the cyanogen-breaking reaction tank 3 is connected with a secondary spraying device 52 on the upper part of a tail gas absorption tower 5 through a pipeline, the lower part of the tail gas absorption tower 5 is connected with a tail absorption tower circulating pump 6, partial spraying liquid of the tail gas absorption tower is conveyed to a primary spraying device 51 on the upper part of the tail gas absorption tower 5 through the tail absorption tower circulating pump 6 for circular circulating spraying, partial spraying liquid is conveyed to a primary vulcanization aeration tank 7, a primary vulcanization aeration pipe 71 is arranged at the bottom of the primary vulcanization aeration tank 7, a conveying pump B8 is arranged on a connecting pipeline between the bottom of the primary vulcanization aeration tank 7 and a feed inlet of a cadmium slag inclined plate sedimentation tank 9, a cadmium slag pressure filter 10 is arranged on a connecting pipeline between a discharge port at the bottom of the cadmium slag inclined plate sedimentation tank 9 and a feed inlet of the cadmium slag pressure filter 11, a cadmium slag hopper 111 is arranged at the bottom of the cadmium slag pressure filter 11, a liquid outlet of the cadmium slag pressure filter 11, the bottom of the cadmium removal clear liquid tank 12 is connected with a secondary vulcanization aeration tank 14 through a pipeline, the pipeline is provided with a delivery pump C13, the bottom of the secondary vulcanization aeration tank 14 is provided with a secondary vulcanization aeration pipe 141, a connecting pipeline between the bottom of the secondary vulcanization aeration tank 14 and a zinc slag inclined plate precipitation tank 16 is provided with a delivery pump D15, a connecting pipeline between the bottom of the zinc slag inclined plate precipitation tank 16 and a feed inlet of a zinc slag filter press 18 is provided with a zinc slag filter press pump 17, the bottom of the zinc slag filter press 18 is provided with a zinc slag hopper 181, a liquid outlet of the zinc slag filter press 18 and a liquid outlet of the zinc slag inclined plate precipitation tank 16 are connected with a zinc removal clear liquid tank 19 through pipelines, the bottom of the zinc removal clear liquid tank 19 is connected with an inlet of a ceramic membrane filter 21 through a pipeline, the pipeline is provided with a ceramic membrane filtration high-pressure pump 20, concentrated water of the ceramic membrane filter 21 returns to the zinc slag filter press 18 through a pipeline, the bottom of the ceramic filtered liquid pool 22 is connected with the inlet of the organic membrane filter 24 through a connecting pipeline, an organic membrane filtering high-pressure pump 23 is arranged on the connecting pipeline, concentrated water of the organic membrane filter 24 returns to the dezincification clear liquid pool 19 through a pipeline, clear liquid is conveyed to the organic membrane filtering clear liquid pool 25 through a pipeline, the bottom of the organic membrane filtered liquid pool 25 is connected with the inlet of the pH adjusting pool 27 or a pipeline of a recycling workshop through a connecting pipeline, a conveying pump E26 is arranged on the connecting pipeline, the top of the pH adjusting pool 27 is provided with a sulfuric acid adding port, a pH meter and a stirring device 271 are arranged in the pH adjusting pool 27, the stirring device 271 comprises a stirring rod, stirring blades arranged on the stirring rod and a driving motor used for driving the stirring rod to rotate, the bottom of the pH adjusting pool 27 is connected with a conveying pump F28, and standard-reaching wastewater is recycled or discharged through a conveying pump F.
And the top parts of the tail gas absorption tower 5, the primary vulcanization aeration tank 7, the secondary vulcanization aeration tank 14 and the pH adjusting tank 27 are respectively provided with a discharge port connected with a discharge pipeline, and a tail gas discharge fan 29 is arranged on the discharge pipeline.
The primary vulcanization aeration pipe 71 of the primary vulcanization aeration tank 7 and the secondary vulcanization aeration pipe 141 of the secondary vulcanization aeration tank 14 are both connected with a mixed gas input pipe of hydrogen sulfide gas and compressed air, and the hydrogen sulfide gas can come from the hydrogen sulfide generator 30 or can be canned hydrogen sulfide gas.
The lower part of the cyanogen breaking reaction tank 3 is connected with a cyanogen breaking stirring pump 4, and the wastewater discharged from a stirring port 31 of the cyanogen breaking reaction tank returns to the cyanogen breaking reaction tank 3 through the cyanogen breaking stirring pump 4 to realize stirring action.
The height to diameter ratio of the primary vulcanization aeration tank 7 to the secondary vulcanization aeration tank 14 is 1.0-1.2: 1; the pH value of the wastewater detected by the pH meter is arranged in the primary vulcanization aeration tank and the secondary vulcanization aeration tank.
The tail gas absorption tower 5 can adopt a multi-layer spraying empty tower form, and a tubular pressure distributor and a spray head are installed in the tower.
The operation steps of the cyanogen cadmium electroplating wastewater treatment system of the embodiment are as follows:
A. electroplating wastewater such as rinsing water of a cyaniding electroplating workshop is converged into the cyanogen-cadmium wastewater adjusting tank 1 to be uniformly mixed, so that the wastewater quality is stabilized;
B. conveying the wastewater in the cyanide wastewater adjusting tank 1 to a cyanogen breaking reaction tank 3 by using a conveying pump A2 for oxidation cyanogen breaking treatment: adding a small amount of sodium hydroxide to wasteAdjusting the pH value of water to 10.0-11.0 according to ClO2Adding chlorine dioxide into the wastewater at a mass ratio of CN < - > 2.70-3.00: 1, and starting a cyanogen breaking stirring pump 4 to stir for 45-60 min;
C. primary vulcanization of wastewater and tail gas absorption: the waste water after cyanogen breaking is conveyed to a secondary spraying device 52 of a tail gas absorption tower 5 through a cyanogen breaking stirring pump 4 by-pass, a tail gas absorption tower circulating pump 6 conveys the cyanogen breaking waste water at the bottom of the tail gas absorption tower to a primary spraying device 51 of the tail gas absorption tower 5, circulating liquid of the two-stage spraying device is in countercurrent contact with tail gas for primary vulcanization, and zinc and cadmium ions in the waste water and H in the tail gas are in countercurrent contact with each other2S, carrying out a vulcanization reaction to remove part of zinc and cadmium ions; h in the tail gas2Acid gases such as S and chlorine are absorbed and removed and then discharged after reaching the standard, the tail gas flow rate of the primary absorption tower is 1.8-2.2 m/S, and the total spray density is 45-55 m3/(m2.h)；
D. The cyanogen cadmium waste water after the primary sulfuration is sent into a primary sulfuration aeration tank 7 by a tail absorption tower circulating pump 6 through a bypass, hydrogen sulfide gas (can also adopt canned hydrogen sulfide gas) produced by a hydrogen sulfide generator 30 is mixed with compressed air used for aeration, the mixture is distributed into fine and uniform bubbles through a primary sulfuration aeration pipe 71 arranged at the bottom of the primary sulfuration aeration tank, and zinc and cadmium ions in the waste water and H aerated into the primary sulfuration aeration tank 72S, carrying out a vulcanization reaction to remove zinc and cadmium ions; the pH value can be automatically maintained to be 10.0-11.0 generally in the primary vulcanization aeration process, acid and alkali are not required to be added, and the primary vulcanization reaction time of the wastewater is 30-50 minutes;
E. the wastewater after the primary vulcanization aeration is conveyed to a cadmium slag inclined plate settling tank 9 through a conveying pump B8 for precipitation treatment, the precipitation underflow is conveyed to a cadmium slag filter press 11 through a cadmium slag filter press 10 for filter pressing, and the cadmium slag generated by the filter pressing is temporarily stored in a cadmium slag hopper 111 and then is conveyed for comprehensive utilization;
F. clear liquid produced by cadmium slag inclined plate sedimentation and filtrate produced by cadmium slag inclined plate sedimentation underflow filter pressing are collected to a cadmium-removing clear liquid pool 12, then are conveyed to a secondary vulcanization aeration tank 14 by a conveying pump C13, hydrogen sulfide gas (can also adopt canned hydrogen sulfide) produced by a hydrogen sulfide generator 30 is mixed with compressed air used for aeration, and then are arranged in the secondary vulcanization aeration tankThe secondary vulcanization aeration pipes 141 at the bottom of the secondary vulcanization aeration tank 14 are distributed into fine and uniform bubbles, and zinc ions in the wastewater and H aerated in the secondary vulcanization aeration tank 142S, carrying out a vulcanization reaction to remove zinc ions; the height/diameter ratio of the secondary vulcanization aeration tank 14 is 1.0-1.2; dropwise adding sulfuric acid in the secondary vulcanization aeration process to control the pH value to be 8.5-9.5, wherein the secondary vulcanization reaction time of the wastewater is 30-40 minutes;
G. conveying the wastewater subjected to secondary vulcanization aeration to a zinc slag inclined plate settling tank 16 by using a conveying pump D15 for precipitation treatment, conveying a precipitation underflow to a zinc slag filter press 18 by using a zinc slag filter press 17 for filter pressing, and comprehensively utilizing zinc slag produced by filter pressing;
H. the surface clear solution of the zinc slag sloping plate settling tank 16 and the filtrate of the zinc slag filter press 18 are converged and enter a zinc removal clear solution pool 19, then the mixture is conveyed to a ceramic membrane filter 21 for filtration by a ceramic membrane filtering high-pressure pump 20, the concentrated water returns to the zinc slag sloping plate settling tank 16 for precipitation, and the clear solution is conveyed to a ceramic filter liquid pool 22;
I. the clear liquid collected in the ceramic filtered liquid pool 22 is conveyed to an organic membrane filter 24 by an organic membrane filtering high-pressure pump 23 to remove zinc and cadmium ions deeply, the concentrated water obtained after the treatment of the organic membrane filter 24 returns to the ceramic membrane filter 21 for filtration, the clear liquid produced by the organic membrane filter 24 is conveyed to an organic membrane filtering clear liquid pool 25 and then conveyed to an electroplating system for reuse or a pH value adjusting pool 27 by a conveying pump E26;
J. adding sulfuric acid into a pH value adjusting tank 27, stirring for reaction, adjusting the pH value to be 7-9, and regulating Cd2+Stable to less than 0.05mg/L, Zn2+Less than or equal to 1.5mg/L, and less than or equal to 1.0mg/L of SS, so as to meet the discharge requirement of the discharge index of the electroplating wastewater; the treated wastewater can also be returned to the electroplating workshop for reuse.
The treatment effect is as follows:
the components of the cyaniding cadmium-containing electroplating wastewater before treatment are as follows (pH value is dimensionless):
| item | CN- | Cd2+ | Zn2+ | pH | Amount of water |
| Content mg/L | 600～1000 | 50～120 | 90～120 | ≥10 | 15m3/h |
The electroplating wastewater after treatment comprises the following components (pH value is dimensionless)
| Item | CN- | Cd2+ | Zn2+ | ClO2 | pH |
| Content mg/L | 0.009～0.030 | 0.03～0.04 | 1.0～1.2 | ＜2.0 | 7～9 |
Residual ClO in treated wastewater2Less than 2.0mg/L, and consumption of ClO in actual production216.95-28.2 kg/h; hydrogen sulfide-containing gas (containing H) produced by hydrogen sulfide generator is consumed in production2S 80％)0.6～0.7m3H; the treated wastewater contains CN-And Cd contained2+And Zn2+The concentration of the cadmium, the cyanide and the zinc in the electroplating wastewater is 0.009-0.030 mg/L, 0.03-0.04 mg/L and 1.0-1.2 mg/L respectively, the highest limit requirements of the highest allowable discharge concentrations of 0.05mg/L, 0.3mg/L and 1.5mg/L of the total cadmium, the total cyanide and the total zinc in the electroplating wastewater of GB21900-2008 electroplating pollutant discharge standard are completely met, and the electroplating wastewater can be recycled or discharged after reaching the standard.
Example 2:
as shown in fig. 2, the structure of the cyaniding cadmium plating electroplating wastewater treatment system of the present invention is basically the same as that adopted in embodiment 1, except that the tail gas absorption tower circulating pump 6 simultaneously conveys the spray liquid of the tail gas absorption tower to the first-stage spray device 51 and the second-stage spray device 52 for circular spraying.
The operation steps of the cyanogen cadmium electroplating wastewater treatment system of the embodiment are as follows:
A. electroplating wastewater such as rinsing water of a cyaniding electroplating workshop is converged into the cyanogen-cadmium wastewater adjusting tank 1 to be uniformly mixed, so that the wastewater quality is stabilized;
B. conveying the wastewater in the cyanide wastewater adjusting tank 1 to a cyanogen breaking reaction tank 3 by using a conveying pump A2 for oxidation cyanogen breaking treatment: adding a small amount of sodium hydroxide to adjust the pH value of the wastewater to 10.0-11.0 according to ClO2Adding chlorine dioxide into the wastewater at a mass ratio of CN < - > 2.70-3.00: 1, and starting a cyanogen breaking stirring pump 4 to stir for 45-60 min;
C. primary sulfurization of waste water and tail gasAbsorption: the waste water after cyanogen breaking is conveyed to a secondary spraying device 52 of a tail gas absorption tower 5 through a cyanogen breaking stirring pump 4 by-pass, the cyanogen breaking waste water at the bottom of the tail gas absorption tower is conveyed to a primary spraying device 51 and a secondary spraying device 52 of the tail gas absorption tower 5 through a tail gas absorption tower circulating pump 6, circulating liquid of the two-stage spraying device is in countercurrent contact with tail gas for primary vulcanization, and zinc and cadmium ions in the waste water and H in the tail gas2S, carrying out a vulcanization reaction to remove part of zinc and cadmium ions; h in the tail gas2Acid gases such as S and chlorine are absorbed and removed and then discharged after reaching the standard, the tail gas flow rate of the primary absorption tower is 1.8-2.2 m/S, and the total spray density is 45-55 m3/(m2H); the double-layer spraying device is adopted, so that the spraying density and the absorption effect of the secondary spraying device 52 can be better ensured;
D. the cyanogen cadmium waste water after the primary sulfuration is sent into a primary sulfuration aeration tank 7 by a tail absorption tower circulating pump 6 through a bypass, hydrogen sulfide gas (can also adopt canned hydrogen sulfide) produced by a hydrogen sulfide generator is mixed with compressed air used for aeration, the hydrogen sulfide gas is distributed into fine and uniform bubbles through a primary sulfuration aeration pipe 71 arranged at the bottom of the primary sulfuration aeration tank, and zinc and cadmium ions in the waste water and H aerated into the primary sulfuration aeration tank 72S, carrying out a vulcanization reaction to remove zinc and cadmium ions; the pH value can be automatically maintained to be 10.0-11.0 generally in the primary vulcanization aeration process, acid and alkali are not required to be added, and the primary vulcanization reaction time of the wastewater is 30-50 minutes;
E. the wastewater after the primary vulcanization aeration is conveyed to a cadmium slag inclined plate settling tank 9 through a conveying pump B8 for precipitation treatment, the precipitation underflow is conveyed to a cadmium slag filter press 11 through a cadmium slag filter press 10 for filter pressing, and the cadmium slag generated by the filter pressing is temporarily stored in a cadmium slag hopper 111 and then is conveyed for comprehensive utilization;
F. clear liquid produced by cadmium slag inclined plate sedimentation and filtrate produced by cadmium slag inclined plate sedimentation underflow filter pressing are collected to a cadmium-removing clear liquid pool 12, then are conveyed to a secondary vulcanization aeration tank 14 by a conveying pump C13, hydrogen sulfide gas (can also adopt canned hydrogen sulfide) produced by a hydrogen sulfide generator 30 is mixed with compressed air used for aeration, and then is distributed into fine and uniform bubbles through a secondary vulcanization aeration pipe 141 arranged at the bottom of the secondary vulcanization aeration tank 14, and zinc ions in the wastewater and the aeration enter the secondary vulcanization aeration tank 12H of the aeration tank 142S, carrying out a vulcanization reaction to remove zinc ions; the height/diameter ratio of the secondary vulcanization aeration tank 14 is 1.0-1.2; dropwise adding sulfuric acid in the secondary vulcanization aeration process to control the pH value to be 8.5-9.5, wherein the secondary vulcanization reaction time of the wastewater is 30-40 minutes;
G. conveying the wastewater subjected to secondary vulcanization aeration to a zinc slag inclined plate settling tank 16 by using a conveying pump D15 for precipitation treatment, conveying a precipitation underflow to a zinc slag filter press 18 by using a zinc slag filter press 17 for filter pressing, and comprehensively utilizing zinc slag produced by filter pressing;
H. the surface clear solution of the zinc slag sloping plate settling tank 16 and the filtrate of the zinc slag filter press 18 are converged and enter a zinc removal clear solution pool 19, then the mixture is conveyed to a ceramic membrane filter 21 for filtration by a ceramic membrane filtering high-pressure pump 20, the concentrated water returns to the zinc slag sloping plate settling tank 16 for precipitation, and the clear solution is conveyed to a ceramic filter liquid pool 22;
I. the clear liquid collected in the ceramic filtered liquid pool 22 is conveyed to an organic membrane filter 24 by an organic membrane filtering high-pressure pump 23 to remove zinc and cadmium ions deeply, the concentrated water obtained after the treatment of the organic membrane filter 24 returns to the ceramic membrane filter 21 for filtration, the clear liquid produced by the organic membrane filter 24 is conveyed to an organic membrane filtering clear liquid pool 25 and then conveyed to an electroplating system for reuse or a pH value adjusting pool 27 by a conveying pump E26;
J. adding sulfuric acid into a pH value adjusting tank 27, stirring for reaction, adjusting the pH value to be 7-9, and regulating Cd2+Stable to less than 0.05mg/L, Zn2+Less than or equal to 1.5mg/L, and less than or equal to 1.0mg/L of SS, and the electroplating wastewater is discharged after meeting the discharge index requirement of the electroplating wastewater; the treated wastewater can also be returned to the electroplating workshop for reuse.
The treatment effect is as follows:
the components of the cyaniding cadmium-containing electroplating wastewater before treatment are as follows (pH value is dimensionless):
| item | CN- | Cd2+ | Zn2+ | pH | Amount of water |
| Content mg/L | 1500～1800 | 120～150 | 150～180 | ≥10 | 12m3/h |
The electroplating wastewater after treatment comprises the following components (pH value is dimensionless)
| Item | CN- | Cd2+ | Zn2+ | ClO2 | pH |
| Content mg/L | 0.015～0.025 | 0.03～0.04 | 1.0～1.2 | ＜2.0 | 7～9 |
Residual ClO in treated wastewater2Less than 2.0mg/L, and consumption of ClO in actual production233.81-40.56 kg/h; hydrogen sulfide-containing gas (containing H) produced by hydrogen sulfide generator is consumed in production2S 80％)0.7～0.8m3H; the treated wastewater contains CN-And Cd contained2+And Zn2+The concentration of the cadmium, the cyanide and the zinc in the electroplating wastewater is 0.02-0.05 mg/L, 0.03-0.04 mg/L and 1.0-1.2 mg/L respectively, the maximum allowable discharge concentration requirements of 0.05mg/L, 0.3mg/L and 1.5mgL of the total cadmium, the total cyanide and the total zinc in the electroplating wastewater in GB21900-2008 electroplating pollutant discharge standard are completely met, and the electroplating wastewater can be recycled or discharged after reaching the standard.
The treatment system is adopted to treat the cyanided cadmium plating electroplating wastewater, not only can ensure the index of the treated wastewater, improve the water reuse rate and reduce the discharge of electroplating wastewater, but also can reduce the alkali consumption and the acid consumption of electroplating wastewater treatment, and is favorable for meeting the increasingly strict environmental protection requirements.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solutions of the present invention and not for limiting the same, and although the present invention is described in detail with reference to the preferred embodiments, those skilled in the art should understand that: the technical solution of the present invention can still be modified or replaced by other equivalent means, and the modified technical solution can not be separated from the spirit and scope of the technical solution of the present invention.
Claims (4)
1. A cyanide cadmium plating electroplating wastewater treatment system is characterized by comprising a cyanide-cadmium wastewater adjusting tank, a cyanide breaking reaction tank, a tail gas absorption tower, a primary vulcanization aeration tank, a cadmium slag inclined plate sedimentation tank, a cadmium slag pressure filter, a secondary vulcanization aeration tank, a zinc slag inclined plate sedimentation tank, a zinc slag pressure filter, a ceramic membrane filter, an organic membrane filter and a pH adjusting tank which are sequentially connected from front to back, wherein a tail gas outlet is arranged at the top of the cyanide breaking reaction tank, a cyanide breaking reaction tank stirring port is arranged at the lower part of the cyanide breaking reaction tank, the tail gas outlet at the top of the cyanide breaking reaction tank is connected with a tail gas inlet at the lower part of the tail gas absorption tower through a pipeline, and the cyanide breaking reaction tank stirring port at the lower part of the cyanide breaking reaction tank is connected with a spraying device at; the top parts of the tail gas absorption tower, the primary vulcanization aeration tank, the secondary vulcanization aeration tank and the pH adjusting tank are all provided with discharge ports connected with discharge pipelines, and tail gas discharge fans are arranged on the discharge pipelines; the cyanogen breaking reaction tank is provided with a feeding port for chlorine dioxide and sodium hydroxide; aeration pipes are arranged at the bottoms of the primary vulcanization aeration tank and the secondary vulcanization aeration tank and are connected with a mixed gas input pipe of hydrogen sulfide gas and compressed air.
2. The cyanide cadmium plating electroplating wastewater treatment system according to claim 1, wherein the cyanide breaking reaction tank is provided with a cyanide breaking stirring pump at the lower part thereof, and wastewater discharged from the stirring port of the cyanide breaking reaction tank is returned to the cyanide breaking reaction tank through the cyanide breaking stirring pump to realize stirring action.
3. The cyanide cadmium plating electroplating wastewater treatment system according to claim 1 or 2, wherein the height to diameter ratio of the primary sulfidation aeration tank to the secondary sulfidation aeration tank is 1.0-1.2: 1; the pH value of the wastewater detected by the pH meter is arranged in the primary vulcanization aeration tank and the secondary vulcanization aeration tank.
4. The cyanide cadmium plating electroplating wastewater treatment system according to claim 1 or 2, wherein a pH meter and a stirring device are arranged in the pH adjusting tank, and the stirring device comprises a stirring rod, a stirring blade arranged on the stirring rod and a driving motor for driving the stirring rod to rotate.
Priority Applications (1)
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