CN103833167A - Chromic acid wastewater treatment method and system - Google Patents
Chromic acid wastewater treatment method and system Download PDFInfo
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- CN103833167A CN103833167A CN201410093510.8A CN201410093510A CN103833167A CN 103833167 A CN103833167 A CN 103833167A CN 201410093510 A CN201410093510 A CN 201410093510A CN 103833167 A CN103833167 A CN 103833167A
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Abstract
The invention discloses a chromic acid wastewater treatment method which comprises the following steps: performing ion exchange on chromic acid wastewater and anion and cationic resins, and treating wastewater generated by backwashing and regenerating the anion and cationic resins with saturated exchange capacity in a diaphragm electrolytic cell. The invention also discloses a chromic acid wastewater treatment system used for treating the chromic acid wastewater generated in a production system. The chromic acid wastewater treatment system comprises an anode resin tank, a cathode resin tank, a regenerating and backwashing wastewater collection tank, a reclaimed water storage tank, the diaphragm electrolytic cell, a purification tank, a cathode regenerated liquid storage tank and an anode regenerated liquid storage tank, wherein the diaphragm electrolytic cell is used for performing electrolytic treatment on the mixed waste liquid and comprises a cell body, an ion diaphragm is arranged in the cell body, and the cell body is separated into an inner cell and an outer cell through the ion diaphragm; a cathode plate is arranged in the inner cell; an anode plate is arranged in the outer cell; the cathode regenerated liquid storage tank is used for storing a strong base solution; the liquid inlet of the production system is respectively connected with the regenerated water storage tank and the purification tank; the chromic acid wastewater outlet of the production system is respectively connected with each anode resin tank. The chromic acid wastewater treatment method and system are used for occasions of generating chromic acid wastewater in electroplating industry and the like.
Description
Technical field
The present invention relates to a kind for the treatment of process of chromic acid waste water, also relate to a kind for the treatment of system of chromic acid waste water.
Background technology
In prior art, much produce in process of production the industry of chromic acid waste water, the environmental issue that chromic acid wastewater treatment is grown is a hang-up urgently to be resolved hurrily always.
As in electroplating industry, the waste water that plating production process produces is mainly derived from plating piece cleaning, ground flushing, hanging tool and pole plate and rinses, discarded tank liquor replacing etc., electroplating wastewater comprises pre-treatment waste water, chromate waste water, contains chromium complex waste water, chromic acid waste water, comprehensive wastewater etc., the technique that generally adopts classification of waste to collect, process respectively.
Wherein chromic acid waste water is mainly containing the CrO4 existing with acid radical anion form
2-, sulfate radical and the metal ion that exists with simple positively charged ion form be as Ni
2+, Cu
2+, Cr
6+, Fe
3+deng, the treatment process of prior art mainly contains chemical reduction neutralization precipitation method and yin, yang ion-exchange resin.Process chromic acid waste water by chemical reduction neutralization precipitation method, need in chromic acid waste water, add precipitation agent and reductive agent, condensing dose, the chromic acid of processing 1 kilogram can produce the mud of 10 kilograms, treating processes produces a large amount of mud gives prominence to the environmental issue that blowdown causes.The moon of promoting at present, cation exchange resin, although emphasize to accomplish that waste water reclamation utilizes zero release, but the receptible degree of industrial community is low, because resin anion(R.A) has Sodium chromate, except Adsorption of Chromium acid group also must be through de-sodium processing, in the time that absorption makes chromic acid concentration higher, large to resin injury, and Sodium chromate to be cleaned up and needs a large amount of pure water, the accumulation volume of anode metal impurity is many, make cationic exchange resin adsorption deleterious, frequent back washing regeneration waste water resource, sulfuric acid and its purity requirement of sheet alkali of back washing regeneration use are high, the back washing molten sulfur Barbiturates of Sodium chromate and anode is made coating by some processing modes, but this mode need professional unified mechanism be processed, the concentration of the back washing liquid of the anode that obtains is not high, amount does not cause shipment and delivery cost relatively high very much yet, make for finishing sector operating cost high, make this method possible in theory, actual operation difficulty, and can not accomplish closed-loop operation, can not make chromic acid recycling waste water reclamation, therefore existing enterprise would rather select the outer row of mud to cause the chemical reduction neutralization precipitation method of secondary pollution.
Summary of the invention
First technical problem that the present invention solves is that a kind of chromic acid method of wastewater treatment of abandoning a large amount of mud and arranging, make chromic acid wastewater regenerating and recycling closed-loop operation is outward provided.
Second technical problem that the present invention solves is to provide a kind of chromic acid Waste Water Treatment that uses above-mentioned chromic acid method of wastewater treatment.
The technical scheme of first technical problem that the present invention solves is:
A kind of chromic acid method of wastewater treatment, comprises the following steps:
A. chromic acid waste water production system being produced is introduced successively and the anode resin storage tank of Zeo-karb is housed and is equipped with in the resin anion(R.A) groove of anionite-exchange resin, carry out ion-exchange, heavy metal ion and chromate ion in this chromic acid waste water are adsorbed, described chromic acid waste water forms reuse water, described reuse water input reuse water storage tanks, recycles or supplies in subsequent processes for production system;
B. after approaching through the exchange capacity of the Zeo-karb of ion-exchange or reaching capacity, stop to described anode resin storage tank input chromic acid waste water, and described Zeo-karb is carried out to manipulation of regeneration with strong acid solution, after the anode regeneration waste liquid in anode resin storage tank is discharged, carry out back washing processing with the reuse water obtaining in steps A, make described Zeo-karb recover to carry out recycling of next round after exchange capacity, described manipulation of regeneration and back washing are processed to the anode regeneration waste liquid and the anode back washing waste collection that produce pending;
After approaching through the exchange capacity of the anionite-exchange resin of ion-exchange or reaching capacity, stop to this cathode resin groove input chromic acid waste water, and this anionite-exchange resin is carried out to manipulation of regeneration with strong base solution, after the anode regeneration waste liquid in anode resin storage tank is discharged, carry out back washing processing with the reuse water obtaining in steps A, make this anionite-exchange resin recover to carry out recycling of next round after exchange capacity, manipulation of regeneration and back washing are processed to the negative electrode regeneration waste liquid and the negative electrode back washing waste collection that produce pending;
C. will in this anode regeneration waste liquid, anode back washing waste liquid, negative electrode regeneration waste liquid and negative electrode back washing waste liquid input diaphragm sell, carry out electrolysis treatment, the high density chromic acid mixing acid that electrolysis produces carries out inputting production system after purification process and carries out recycle, the high concentration basic solution that electrolysis produces cycling and reutilization during for this anionite-exchange resin manipulation of regeneration.
The beneficial effect of chromic acid method of wastewater treatment of the present invention is: mutually combine because technique scheme adopts yin, yang ion exchange method and membrane electrolysis, allow chromic acid waste water by carrying out ion-exchange with anion and cation exchange resin, chromic acid waste water is become and can again be back to use the reuse water in production system, to the moon, in the regeneration that Zeo-karb carries out and back washing subsequent disposal, use reuse water to replace the pure water of prior art, large quantities of equipment investments that pure water is produced are saved, reduce production cost, make whole production process and produce in subsequent process to form enclosed water cycle, reduce or remit the waste of water resources: in further subsequent disposal, anode regeneration waste liquid, anode back washing waste liquid, in negative electrode regeneration waste liquid and negative electrode back washing waste liquid input diaphragm sell, carry out electrolysis treatment, characteristic according to the free property of sodium ion much larger than other metal ions, the in the situation that of energising, sodium ion is easy to enter cathodic area, and the little metal ion of free property is as Fe
3+, Cr
6+, Ca
2+deng not being gathered in the surface by anode one side on ion diaphragm by the ion diaphragm of diaphragm sell, form oxide compound or oxyhydroxide, be attached in the side of barrier film near anode, be easy to remove with facing, and ion diaphragm by the negative electrode place of a side of negative electrode smoothly electrolysis go out alkali, the anode place of ion diaphragm opposite side can electrolysis go out acid.Utilize separating of ion diaphragm, can be easily sodium hydroxide, chromic acid, sulfuric acid and metallic impurity are separated, and schedule of operation is simple, operating cost is low, the throw out of unique generation is exactly a small amount of barium sulfate producing in the time of purification process, it can separate with chromic acid easily, through precipitation, collect, clean the product that also can become regeneration, and needn't arrange outward, 1 kilogram of chromic acid waste water of the every processing of precipitation neutralisation compared to existing technology produces the amount of 10 kilograms of sediment waste, the a small amount of barium sulfate producing when purification process seems very little, make superiority of the present invention obvious, on the other hand, membrane electrolysis has been removed cycling and reutilization while using high concentration basic solution that contingency question that ion-exchange-resin process produces: a, electrolysis produce for anionite-exchange resin manipulation of regeneration in prior art, has avoided due to the high production cost that improves of back washing regeneration sheet alkali purity requirement, can also further improve the concentration of chromic acid, as in electroplating industry, the concentration that improves chromic acid makes its concentration requirement that reaches plating tank to be back to use plating tank, make whole production process and produce in subsequent process to form the circulation of enclosed alkaline solution and the circulation of chromic acid solution, really accomplish air tight cycle production, without outer row, b, avoid, because the concentration of the back washing liquid of the anode that obtains in prior art is not high, causing and cannot being back to use in production system, measured also not quite, but looked for professional unified mechanism to process, caused shipment and delivery cost relatively high, made the problem high for finishing sector operating cost.
Main chemical reactions in ion exchange process between Zeo-karb and chromic acid waste water is: the Fe in chromic acid waste water
3+, Ni
2+, Cu
2+, Cr
6+exchange Deng the positively charged ion in positively charged ion and Zeo-karb; Cation exchange reaction formula is as follows:
Fe
3++3RH=FeR
3+3H
+
Ni
2++2RH=NiR
2+2H
+
Cu
2++2RH=Cu?R
2+2H
+
Cr
2++3RH=Cr?R
6+6H
+
Positively charged ion in each production industry in chromic acid waste water is different, as in electroplating industry, different and different according to the material of plated item, electroplate as given iron product, the positively charged ion of electroplating in chromic acid waste water is mainly iron ion, electroplates the positively charged ion of electroplating in chromic acid waste water to copper product and is mainly cupric ion.
After cationic exchange, the positively charged ion in chromic acid waste water enters in Zeo-karb, and the hydrogen in resin cation (R.C.) enters in chromic acid waste water, and the pH value of chromic acid waste water is reduced.By cationic exchange, the pH value of chromic acid waste water is further reduced, thereby make in chromic acid waste water, there is more H
+maintain Cr
2o
7 2-existence; In addition, lower pH value also can promote chromic acid waste water in the time carrying out ion-exchange with anionite-exchange resin the moon, is more conducive to the absorption of chromate negatively charged ion.Main chemical reactions in steps A in the process of anionresin is: the Cr in chromic acid waste water
2o
7 2-, CrO
4 2-, CrO
4 2-, SO
4 2-exchange Deng the positive negatively charged ion in negatively charged ion and anionite-exchange resin; Anion exchange reaction formula is as follows:
Cr
2O
7 2-+2ROH=R
2Cr
2O
7+2OH-
CrO
4 2-+2ROH=R
2CrO
4+2OH-
SO
4 2-+2ROH=R
2SO
4+2OH-
From reaction, can find out, when Adsorption of Chromium acid radical anion, the anionite-exchange resin Cr of as much
2o
7 2-exchange capacity be CrO
4 2-the twice of exchange capacity,
As a concrete scheme of technique scheme, the step of in step B, Zeo-karb being carried out to manipulation of regeneration is specially: in anode resin storage tank, adding strong acid solution is that concentration is the sulphuric acid soln of 1～4wt%, and Zeo-karb soak time is exceeded to 24 hours;
Or the step of in step B, anionite-exchange resin being carried out to manipulation of regeneration is specially: in cathode resin groove, adding strong base solution is that concentration is the sodium hydroxide solution of 1～4wt%, and anionite-exchange resin soak time is exceeded to 24 hours;
The reaction of Zeo-karb regeneration is as follows:
2FeR
3+3H
2SO
4=Fe
2（SO
4）
3+6RH
NiR
2+H
2SO
4=Ni?SO
4+2RH
CuR
2+H
2SO
4=Cu?SO
4+2RH
CrR
6+3H
2SO
4=Cr（SO
4）
3+6RH
Anionite-exchange resin regenerative response is as follows:
R
2Cr
2O
7+2NaOH=Na
2Cr
2O
7+2ROH
R
2CrO
4+2NaOH=Na
2CrO
4+2ROH
R
2SO
4+2NaOH=Na
2SO
4+2ROH
Anion regeneration is processed the product producing and is mainly Na
2cr
2o
7and Na
2sO
4.
As the further improvement to technique scheme, soak time is between 24 hours to 48 hours.This time length ratio is more reasonable, has both made Zeo-karb regeneration or anionite-exchange resin regeneration completely, is controlled at again in the scope of enhancing productivity to greatest extent.
As a concrete scheme of technique scheme, diaphragm sell in step C is divided into water jacket and inside groove by ion diaphragm, the inside groove of ion diaphragm inner side is negative electrode, the water jacket in ion diaphragm outside is anode, this anode regeneration waste liquid, anode back washing waste liquid, in negative electrode regeneration waste liquid and negative electrode back washing waste liquid input water jacket, carry out before electrolysis, add reuse water toward inside groove, and in the reuse water of inside groove hydrogen injecting sodium hydroxide solution, make the concentration of sodium hydroxide solution in inside groove reach 1wt%, reuse water liquid level in inside groove is consistent with water jacket liquid level, current density for electrolysis is 2～5A/d ㎡, voltage is 15～30V, in electrolytic reaction process, in inside groove, naoh concentration raises gradually, in the time that naoh concentration is more than or equal to 4wt%, concentration processing is fallen in sodium hydroxide solution in inside groove: shift out in part inside groove sodium hydroxide solution for the regeneration process of the anionite-exchange resin in step B, the liquid level causing declines by adding pure water or reuse water to supplement to negative electrode one side, makes the concentration of sodium hydroxide solution in inside groove be reduced to 1wt% left and right from 4wt%, regularly the metal ion oxide compound being deposited on ion diaphragm is rejected, when electrolysis, in water jacket, generate chromic acid mixing acid, along with chromic acid increasing mixed acid concentration raises, after regularly the high density chromic acid mixing acid in water jacket being drawn to water jacket and carried out purification process, input is produced to unite and is carried out recycle, inputs anode regeneration waste liquid, anode back washing waste liquid, negative electrode regeneration waste liquid and negative electrode back washing waste liquid and supplement when anode water level declines, purification process in step C is: first stop anode regeneration waste liquid, anode back washing waste liquid, negative electrode regeneration waste liquid and negative electrode back washing waste liquid and enter in diaphragm sell, determine that again sodium ion almost dissociates in negative electrode, this can be bordering on zero for standard, the high density then anode electrolysis being gone out from electric current trend
The high density chromic acid mixing acid that anode electrolysis is gone out, adds barium carbonate, standing separation after stirring, and upper solution becomes pure chromic acid, uses continuing in defeated time production system of described pure chromic acid.This concrete scheme makes production operation management process simple, as long as regularly concentration processing is fallen in the sodium hydroxide solution of inside groove, regularly concentration processing falls in the chromic acid mixed acid solution of external groove, and regularly strike off the metal oxide or the oxyhydroxide that are attached on ion diaphragm, keep on post without waste of manpower.
In electrolysis treatment process, at ion diaphragm by the reaction at the negative electrode place of a side of negative electrode be:
H
2O=2H
++OH-
Na
++OH-=NaOH
Cathodic electricity solves alkali, can be recovered and continue to use.
At ion diaphragm by the reaction of a side of anode be:
Fe
3++OH-=Fe（OH）
3↓
As other metallic cations of iron class are deposited in the surface of ion diaphragm by anode one side, can regularly be struck off.
At ion diaphragm by the reaction at the anode place of anode one side be:
H
2O=2H
++OH-
Cr
2O
7 2-+H
+=H
2Cr
2O
7
SO
4 2-+H
+=H
2SO
4
The chromic acid mixing acid that anode electrolysis goes out can add production system to continue to use after removing sulfuric acid after by purifying.
Purification process in step C is that the high density chromic acid mixing acid that anode electrolysis is gone out is inputted in purifying groove, adds barium carbonate, and standing separation after stirring is got upper solution and added continuation in production system to use.
Purification reaction is:
BaCO3+H
2SO
4=B
aSO
4↓+H
2O+CO
2↑
Sulfuric acid generates barium sulfate precipitate, and the purity of chromic acid is increased.
As the further improvement to technique scheme, pure chromic acid is through the concentrated concentration requirement that reaches production system of heating.
The technical scheme of second technical problem that the present invention solves is:
A kind of chromic acid Waste Water Treatment, processes for the chromic acid waste water that production system is produced, and comprising:
Anode resin storage tank, this anode resin storage tank has P cover, P >=1, each anode resin storage tank parallel join, in anode resin storage tank, Zeo-karb is housed, for carrying out ion-exchange with chromic acid waste water, and for Zeo-karb being carried out to manipulation of regeneration and back washing processing;
Cathode resin groove, this cathode resin groove has Q cover, Q >=1, each cathode resin groove parallel join, in resin anion(R.A) groove, anionite-exchange resin is housed, for carrying out ion-exchange with chromic acid waste water, and for anionite-exchange resin being carried out to manipulation of regeneration and back washing processing;
Regeneration and back washing waste water collection tank, for collecting anode regeneration waste liquid and the anode back washing waste liquid that each anode resin storage tank is discharged, also collect negative electrode regeneration waste liquid and negative electrode back washing waste liquid that each cathode resin groove is discharged, the liquid in regeneration and back washing waste water collection tank becomes mixed waste liquor;
Reuse water holding tank, the reuse water of discharging for collecting each cathode resin groove;
Diaphragm sell, for mixed waste liquor is carried out to electrolysis treatment, diaphragm sell comprises cell body, is also provided with ion diaphragm in this cell body, cell body is divided into inside groove and water jacket by this ion diaphragm; In this inside groove, be provided with a negative plate, in this water jacket, be provided with positive plate;
Purifying groove, the fluid inlet of this purifying groove is connected with this water jacket;
Negative electrode regenerated liquid storage tanks, for storing strong base solution, the liquid outlet of this negative electrode regenerated liquid storage tanks is connected with each cathode resin groove respectively, and the fluid inlet of this negative electrode regenerated liquid storage tanks is connected with inside groove;
Anode regenerated liquid storage tanks, for storing strong acid solution, the liquid outlet of this anode regenerated liquid storage tanks is connected with each anode resin storage tank respectively;
The fluid inlet of production system is connected with reuse water storage tanks, purifying groove respectively, and the chromic acid waste water liquid outlet of production system is connected with each anode resin storage tank respectively;
The fluid inlet of reuse water storage tanks is connected with each cathode resin groove respectively; The liquid outlet of reuse water holding tank is also connected with cathode resin groove, anode resin storage tank, inside groove respectively;
The fluid inlet of regeneration and back washing waste water collection tank is connected with each anode resin storage tank, each cathode resin groove respectively, and liquid outlet is connected with the water jacket in diaphragm sell;
This is connected to be and is equipped with controlled connection of pipeline valve, has liquid level poor or be provided with pump between each groove.
The beneficial effect of chromic acid Waste Water Treatment of the present invention is: because technique scheme adopts Q cover cathode resin groove and the controlled connection of P cover anode each parallel outfit pipeline valve of resin storage tank, the running of system is only undertaken by by-pass valve control, chromic acid Waste Water Treatment uses together with production system, without carry out links material shift time carrying, save manpower, reduced production cost.
Concrete operations are as follows, work as P=1, when Q=1, whole chromic acid Waste Water Treatment intermittent type running, first start the pipeline valve that the chromic acid waste water liquid outlet of production system is connected with anode resin storage tank, make chromic acid waste water enter anode resin storage tank, then enter cathode resin groove, chromic acid waste water is become enter reuse water storage tanks after reuse water for subsequent use, when Zeo-karb and anionite-exchange resin saturated or approach saturated after, close the pipeline valve that the chromic acid waste water liquid outlet of production system is connected with anode resin storage tank, and close the pipeline valve between cathode resin groove and reuse water storage tanks, then open the pipeline valve between liquid outlet and the anode resin storage tank of anode regenerated liquid storage tanks, make the strong base solution input anode resin storage tank of anode regenerated liquid storage tanks, after reaching liquid level requirement, close this valve, pipeline valve between liquid outlet and the cathode resin groove of unlatching negative electrode regenerated liquid storage tanks, make the strong acid solution input cathode resin groove of negative electrode regenerated liquid storage tanks, after reaching liquid level requirement, close this valve, to Zeo-karb, anionite-exchange resin carries out manipulation of regeneration, complete after manipulation of regeneration, open respectively anode resin storage tank, pipeline valve between the fluid inlet of cathode resin groove and regeneration and back washing waste water collection tank, after emptying anode regeneration waste liquid and negative electrode regeneration waste liquid, open liquid outlet and the cathode resin groove of reuse water holding tank, pipeline valve between anode resin storage tank, make reuse water respectively to Zeo-karb, anionite-exchange resin carries out back washing, the anode back washing waste liquid producing and negative electrode back washing waste liquid continue to arrange into regeneration and back washing waste water collection tank, complete after back washing emptying waste liquid, close anode resin storage tank, pipeline valve between the fluid inlet of cathode resin groove and regeneration and back washing waste water collection tank, the pipeline valve that the chromic acid waste water liquid outlet of startup production system is connected with anode resin storage tank, carry out the next round circulation of chromic acid wastewater treatment.Mixed waste liquor processing to regeneration and back washing waste water collection tank: open the pipeline valve between regeneration and back washing waste water collection tank liquid outlet and the water jacket of diaphragm sell, make in mixed waste liquor input water jacket, open the pipeline valve between liquid outlet and the inside groove of reuse water holding tank, toward inside groove input reuse water, and in the reuse water of inside groove hydrogen injecting sodium hydroxide solution, make the concentration of sodium hydroxide solution in inside groove reach 1wt%, the reuse water liquid level in inside groove is consistent with water jacket liquid level, in electrolytic reaction process, in inside groove, naoh concentration raises gradually, in the time that naoh concentration is more than or equal to 4wt%, concentration processing is fallen in sodium hydroxide solution in inside groove: open the pipeline valve between inside groove and the fluid inlet of negative electrode regenerated liquid storage tanks, make sodium hydroxide solution part in inside groove be input to negative electrode regenerated liquid storage tanks, then close this valve, and open the pipeline valve between inside groove and reuse water storage tanks, reuse water adds to inside groove, make inside groove liquid level remain consistent with water jacket liquid level, in inside groove, the concentration of sodium hydroxide solution is reduced to 1wt% left and right from 4wt%, regularly the metal ion oxide compound being deposited on ion diaphragm is rejected, when electrolysis, in water jacket, generate chromic acid mixing acid, when chromic acid increasing mixed acid concentration be increased to can be for the concentration of plating tank after, open the pipeline valve between water jacket and purifying groove, high density chromic acid mixing acid in water jacket is inputted to purifying groove and closed this valve, open again the pipeline valve between regeneration and back washing waste water collection tank liquid outlet and water jacket, input mixed waste liquor supplements that to maintain the liquid level of water jacket consistent with inside groove, high density chromic acid mixing acid is after purification process, open the pipeline valve between purifying groove liquid outlet and production system fluid inlet, purified high density chromic acid input production system is carried out to recycle.
As P > 1, when Q > 1, the running of chromic acid Waste Water Treatment and above-mentioned running are basic identical, its difference is, Q is overlapped to cathode resin groove and P cover anode resin storage tank and be divided into two groups or more, each running only starts wherein the pipeline valve between the chromic acid waste water liquid outlet of one group of anode resin storage tank and cathode resin groove and production system, close the pipeline valve between other groups and the chromic acid waste water liquid outlet of production system, until that group starting process chromic acid waste water self reach capacity or approach saturated after, close pipeline valve and stop entering of chromic acid waste water, start the pipeline valve between other groups and the chromic acid waste water liquid outlet of production system simultaneously, so carry out on duty by turns, make saturated or approach that saturated group regenerate and back washing in, system is to chromic acid wastewater treatment operate continuously, do not need batch operation.
As the further improvement to technique scheme, also comprise heating thickener, fluid inlet, the liquid outlet of this heating thickener are connected in series with the fluid inlet of purifying groove and production system respectively.This improvement makes chromic acid Waste Water Treatment adjustable to the concentration of the pure chromic acid obtaining from purifying groove, can reach the requirement of production system.
As to technique scheme concrete scheme, cell body is plastic groove, this ion diaphragm is N boccaro cylinder, N >=1, and this boccaro cylinder is that volume is that 60～100L, water-permeable are that 0.01～0.05ml/d ㎡ days, sintering temperature are the boccaro cylinder of 1000～1200 ℃; The current density for electrolysis loading between the positive plate being somebody's turn to do and negative plate is that 2～5A/d ㎡, voltage are 15～30V; This negative plate is cylindrical stainless steel cylinder, and this positive plate is chromium plating stereotype, on this cylindrical stainless steel cylinder, is covered with the aperture that radially runs through barrel wall.Boccaro cylinder, because containing quantitative quartz sand, is possessed certain water-permeable under high temperature sintering, than the more etch of ability chromic acid of general pottery; Even under the condition of life-time service, its water-permeable still remains unchanged; In the time that multiple boccaro cylinders connect use, the distribution of electric current is still even, makes electrolytic regeneration effective.Because negative plate is made cylindrical, can make it reach low current and distribution of current is even, make the catholyte can be free toward anode with the form of chromate, and make ferric chromate precipitation, reach and effectively remove fast metallic impurity.
Accompanying drawing explanation
Fig. 1 is the cathode hydrogen sodium oxide concentration curve of the embodiment bis-of the treatment process of chromic acid waste water of the present invention;
Fig. 2 is the cathode hydrogen sodium oxide concentration curve of the embodiment tri-of the treatment process of chromic acid waste water of the present invention;
Fig. 3 is the block diagram of the embodiment mono-of the treatment system of chromic acid waste water of the present invention;
Fig. 4 is the structural representation of chromic acid electrolytic film groove in the embodiment mono-for the treatment of system of chromic acid waste water of the present invention;
Fig. 5 is the negative plate front view of chromic acid electrolytic film groove in the embodiment mono-for the treatment of system of chromic acid waste water of the present invention;
Fig. 6 is the vertical view of Fig. 5;
Fig. 7 is the block diagram of the embodiment bis-of the treatment system of chromic acid waste water of the present invention;
Fig. 8 is the block diagram of the embodiment bis-another kind of states of the treatment system of chromic acid waste water of the present invention.
Embodiment
Below in conjunction with drawings and Examples, the present invention is further described.
The embodiment mono-of the treatment process of chromic acid waste water of the present invention
First the anode resin storage tank that the injection of chromic acid waste water is equipped with to Zeo-karb carries out ion-exchange, and then will inject the resin anion(R.A) groove that anionite-exchange resin is housed from the chromic acid waste water of anode resin storage tank outflow, chromic acid waste water becomes the reuse water that meets emission standard, and reuse water input reuse water storage tanks is for subsequent use; After approaching through the exchange capacity of the Zeo-karb of ion-exchange or reaching capacity, stop anode resin storage tank input chromic acid waste water, and the sulphuric acid soln that is 1～4wt% by concentration by Zeo-karb exceedes 48 hours to Zeo-karb soak time, now sulphuric acid soln has become anode regeneration waste liquid, anode regeneration waste liquid is collected pending, Zeo-karb is carried out to back washing with reuse water, the anode back washing waste collection that back washing is produced is pending; Zeo-karb recovers to carry out recycling of next round after exchange capacity.
After approaching through the exchange capacity of the anionite-exchange resin of ion-exchange or reaching capacity, stop to cathode resin groove input chromic acid waste water, and the sodium hydroxide solution that is 1～4wt% by concentration by anionite-exchange resin exceedes 48 hours to Zeo-karb soak time, now sodium hydroxide solution has become negative electrode regeneration waste liquid, negative electrode regeneration waste liquid is collected pending, anionite-exchange resin is carried out to back washing with reuse water, the negative electrode back washing waste collection that back washing is produced is pending; Anionite-exchange resin recovers to carry out recycling of next round after exchange capacity.
The cell body of diaphragm sell is divided into water jacket and inside groove by the ceramic cylinder of two built-in each 60L of volume, ceramic cylinder is as ion diaphragm, ceramic cylinder inner side is negative electrode, and the water jacket in ceramic cylinder outside is anode, is that 2～5A/d ㎡, voltage are 15～30V for the current density of electrolysis; Temperature is 50 ℃.
Anode regeneration waste liquid, anode back washing waste liquid, negative electrode regeneration waste liquid are become to mixed waste liquor together with negative electrode back washing waste collection, mixed waste liquor is inputted in water jacket, in ceramic cylinder, add reuse water, and inject NaoH solution in reuse water in ceramic cylinder, making the reuse water in ceramic cylinder is 1wt% left and right containing the concentration of NaoH, and the reuse water liquid level in ceramic cylinder is consistent with water jacket liquid level.
In electrolytic reaction process, in ceramic cylinder, naoh concentration raises gradually, in the time that naoh concentration is more than or equal to 4wt%, concentration processing is fallen in sodium hydroxide solution in ceramic cylinder: it is for subsequent use to shift out in part ceramic cylinder sodium hydroxide solution storage, the liquid level causing declines by adding reuse water to supplement to negative electrode one side, makes the concentration of sodium hydroxide solution in ceramic cylinder be reduced to 1wt% left and right from 4wt%; Regularly the precipitation by metallic ion thing being deposited on ceramic cylinder outer wall is rejected; When electrolysis, in water jacket, generate chromic acid mixing acid, in the time that the rising of chromic acid increasing mixed acid concentration reaches production system service requirements, high density chromic acid mixing acid in water jacket is drawn to water jacket and carried out purification process, purification process is by high density chromic acid mixing acid, add barium carbonate, standing separation after stirring, upper solution becomes pure chromic acid, use continuing in defeated pure chromic acid time production system, when anode water level declines, input mixed waste liquor and supplement; The sodium hydroxide solution shifting out from ceramic cylinder, for the regeneration process of step anionite-exchange resin.
The embodiment bis-of the treatment process of chromic acid waste water of the present invention
The embodiment mono-of the treatment process of the present embodiment and chromic acid waste water is basic identical, its difference is, the electrolysis procedure of diaphragm sell: the water jacket of getting Sodium chromate that negative electrode back washing liquid 500L includes 10g/L and put into diaphragm sell, in ceramic cylinder, add reuse water, and in reuse water in ceramic cylinder, to inject 1% NaoH solution be 6.33g/L through titrimetry NaoH concentration, reuse water liquid level in ceramic cylinder is consistent with water jacket liquid level, operational condition: temperature: 50 ℃.Electrolysis is carried out in energising, and in 120 hours processes of electrolysis, water jacket increases mixed waste liquor 240L, ceramic cylinder compensation regeneration water 40L.As time goes on, the NaoH strength of solution in ceramic cylinder changes, and its changing value and electrolysis time corresponding lists are as follows:
| Time h | Concentration g/ |
| 0 | 6.33 |
| 8 | 6.5 |
| 16 | 8 |
| 24 | 9.8 |
| 32 | 11.6 |
| 40 | 12.4 |
| 48 | 15.2 |
| 56 | 16.3 |
| 64 | 17.1 |
| 72 | 18 |
| 80 | 18.3 |
| 88 | 18.5 |
| 96 | 18.9 |
| 104 | 19.1 |
| 112 | 19.3 |
| 120 | 19.3 |
| 128 | 19.3 |
Gained cathode hydrogen sodium oxide concentration curve is referring to Fig. 1.
While just starting electrolysis, electric current is very little, because temperature is lower, along with the time of electrolysis increases, temperature constantly raises, and the naoh concentration that has just started ceramic cylinder only has 1%, but to after 16 hours, electric current increase is very fast, and naoh concentration also sharply increases, but to just significantly decline of after-current in 72 hours, it is also slack-off that naoh concentration gathers way, arrive after 96hr, electric current almost drops to zero, and the bubble that negative plate produces is also very little, and this represents that negative and positive the two poles of the earth have reached equilibrium state.
The embodiment tri-of the treatment process of chromic acid waste water of the present invention
The embodiment bis-of the treatment process of the present embodiment and chromic acid waste water is basic identical, its difference is, the electrolysis procedure of diaphragm sell: the water jacket of mixed waste liquor 500L being put into diaphragm electrolysis, As time goes on, NaoH strength of solution in ceramic cylinder changes, and its changing value and electrolysis time corresponding lists are as follows:
| Time h | Concentration g/ |
| 0 | 3.1 |
| 8 | 3.2 |
| 16 | 3.9 |
| 24 | 4.5 |
| 32 | 5.2 |
| 40 | 5.7 |
| 48 | 6.4 |
| 56 | 6.8 |
| 64 | 7.2 |
| 72 | 7.5 |
| 80 | 7.8 |
| 88 | 8.2 |
| 96 | 8.6 |
| 104 | 8.8 |
| 112 | 8.9 |
| 120 | 9.1 |
| 128 | 9.3 |
| 136 | 9.3 |
Gained cathode hydrogen sodium oxide concentration curve is referring to Fig. 2.
Ceramic cylinder outer wall adheres to a lot of oxide compounds, and result is as follows by analysis:
Relatively, maximum difference is that the ceramic cylinder outer wall of the present embodiment produces a large amount of dirt settlings, can strike off easily to the embodiment bis-of the treatment process of the present embodiment and chromic acid waste water.
The embodiment of the treatment process of three chromic acid waste water shows, when operation, only pay close attention to the degree of ionization of the sodium hydroxide of inside groove, detect the naoh concentration of inside groove to determine whether do the operation of falling concentration, when the naoh concentration of negative electrode exceedes 4%, do sodium hydroxide and fall the operation of concentration; The chromic acid mixing acid that water jacket produces and the metallic impurity that are attached to ceramic cylinder outer wall neither must be as the references of operation, until reaching electrodepositable concentration, the concentration of the chromic acid mixing acid of water jacket just must measure sulfuric acid concentration, in the present embodiment, the concentration of chromic acid mixing acid reaches 20～50g/L or when above, sulfuric acid falls with barium carbonate, improve dense chromic acid degree with thickening equipment again, and metallic impurity can be attached to ceramic cylinder periphery.
The embodiment mono-of the treatment system of chromic acid waste water of the present invention
Referring to Fig. 3, the production system in the present embodiment is plating tank, and chromic acid Waste Water Treatment is processed for the chromic acid waste water that plating tank is produced, and comprising:
1 cover anode resin storage tank, is equipped with Zeo-karb in anode resin storage tank, for carrying out ion-exchange with chromic acid waste water, and for Zeo-karb being carried out to manipulation of regeneration and back washing processing;
1 cover cathode resin groove, is equipped with anionite-exchange resin in resin anion(R.A) groove, for carrying out ion-exchange with chromic acid waste water, and for anionite-exchange resin being carried out to manipulation of regeneration and back washing processing;
Regeneration and back washing waste water collection tank, for collecting anode regeneration waste liquid and the anode back washing waste liquid that anode resin storage tank is discharged, also collect negative electrode regeneration waste liquid and negative electrode back washing waste liquid that cathode resin groove is discharged, the liquid in regeneration and back washing waste water collection tank becomes mixed waste liquor;
Reuse water holding tank, the reuse water of discharging for collecting cathode resin groove;
Diaphragm sell, for mixed waste liquor is carried out to electrolysis treatment, diaphragm sell comprises cell body, is also provided with ion diaphragm in cell body, cell body is divided into inside groove and water jacket by ion diaphragm; In inside groove, be provided with a negative plate, in this water jacket, be provided with positive plate; Referring to Fig. 4, the plastic groove 11 that electrolytic cell body is acid and alkali-resistance, is provided with the chromium plating stereotype 12 as positive plate in plastic groove 11; In plastic groove 11, be also provided with 4 boccaro cylinders 13 as barrier film, the cylinder body inner sleeve of each boccaro cylinder 13 has a cylindrical stainless steel cylinder 14 as negative plate.Boccaro cylinder 13 for volume be that 60～100L, water-permeable are that 0.01～0.05ml/d ㎡ days, sintering temperature are the boccaro cylinder of 1000～1200 ℃.The current density for electrolysis wherein loading between positive plate and negative plate is that 2～5A/d ㎡, voltage are 15～30V.
Referring to Fig. 5, Fig. 6, on cylindrical stainless steel cylinder 14, be covered with the aperture 141 that radially runs through barrel along cylindrical shell, cylinder inboard wall arranges a cathode connection terminal 142.When use, aperture 141 on cylindrical stainless steel cylinder 14 can increase the contact area with liquid, make cylindrical stainless steel cylinder 14 surfaces externally and internallies all and liquid reactions, and the chromate of cylindrical stainless steel cylinder 14 interior generations can be free by aperture anode, accelerates electrolysis
Review Fig. 4, the fluid inlet of purifying groove is connected with this water jacket;
Negative electrode regenerated liquid storage tanks, for storing strong base solution, the liquid outlet of this negative electrode regenerated liquid storage tanks is connected with cathode resin groove respectively, and the fluid inlet of negative electrode regenerated liquid storage tanks is connected with inside groove;
Anode regenerated liquid storage tanks, for storing strong acid solution, the liquid outlet of anode regenerated liquid storage tanks is connected with anode resin storage tank;
The fluid inlet of production system is connected with reuse water storage tanks respectively, and the chromic acid waste water liquid outlet of plating tank is connected with anode resin storage tank; Fluid inlet, the liquid outlet of heating thickener are connected in series with the fluid inlet of purifying groove and production system respectively.
The fluid inlet of reuse water storage tanks is connected with cathode resin groove; The liquid outlet of reuse water holding tank is also connected with cathode resin groove, anode resin storage tank, inside groove respectively;
The fluid inlet of regeneration and back washing waste water collection tank is connected with anode resin storage tank, cathode resin groove, and liquid outlet is connected with the water jacket in diaphragm sell;
The above-mentioned connected controlled connection that is equipped with pipeline valve that is, has liquid level poor or be provided with pump between each groove.
Concrete operations are as follows, first start the chromic acid waste water liquid outlet and the pipeline valve that anode resin storage tank is connected of plating tank, make chromic acid waste water enter anode resin storage tank, then enter cathode resin groove, chromic acid waste water become enter reuse water storage tanks after reuse water for subsequent use, when Zeo-karb and anionite-exchange resin saturated or approach saturated after, close the pipeline valve that the chromic acid waste water liquid outlet of plating tank is connected with anode resin storage tank, and close the pipeline valve between cathode resin groove and reuse water storage tanks, then open the pipeline valve between liquid outlet and the anode resin storage tank of anode regenerated liquid storage tanks, make the strong base solution input anode resin storage tank of anode regenerated liquid storage tanks, after reaching liquid level requirement, close this valve, pipeline valve between liquid outlet and the cathode resin groove of unlatching negative electrode regenerated liquid storage tanks, make the strong acid solution input cathode resin groove of negative electrode regenerated liquid storage tanks, after reaching liquid level requirement, close this valve, to Zeo-karb, anionite-exchange resin carries out manipulation of regeneration, complete after manipulation of regeneration, open respectively anode resin storage tank, pipeline valve between the fluid inlet of cathode resin groove and regeneration and back washing waste water collection tank, after emptying anode regeneration waste liquid and negative electrode regeneration waste liquid, open liquid outlet and the cathode resin groove of reuse water holding tank, pipeline valve between anode resin storage tank, make reuse water respectively to Zeo-karb, anionite-exchange resin carries out back washing, the anode back washing waste liquid producing and negative electrode back washing waste liquid continue to arrange into regeneration and back washing waste water collection tank, complete after back washing emptying waste liquid, close anode resin storage tank, pipeline valve between the fluid inlet of cathode resin groove and regeneration and back washing waste water collection tank, the pipeline valve that the chromic acid waste water liquid outlet of startup plating tank is connected with anode resin storage tank, carry out the next round circulation of chromic acid wastewater treatment.Mixed waste liquor processing to regeneration and back washing waste water collection tank: open the pipeline valve between regeneration and back washing waste water collection tank liquid outlet and the water jacket of diaphragm sell, make in mixed waste liquor input water jacket, open the pipeline valve between liquid outlet and the inside groove of reuse water holding tank, toward inside groove input reuse water, and in the reuse water of inside groove hydrogen injecting sodium hydroxide solution, make the concentration of sodium hydroxide solution in inside groove reach 1wt%, the reuse water liquid level in inside groove is consistent with water jacket liquid level, in electrolytic reaction process, in inside groove, naoh concentration raises gradually, in the time that naoh concentration is more than or equal to 4wt%, concentration processing is fallen in sodium hydroxide solution in inside groove: open the pipeline valve between inside groove and the fluid inlet of negative electrode regenerated liquid storage tanks, make sodium hydroxide solution part in inside groove be input to negative electrode regenerated liquid storage tanks, then close this valve, and open the pipeline valve between inside groove and reuse water storage tanks, reuse water adds to inside groove, make inside groove liquid level remain consistent with water jacket liquid level, in inside groove, the concentration of sodium hydroxide solution is reduced to 1wt% left and right from 4wt%, regularly the metal ion oxide compound being deposited on ion diaphragm is rejected, when electrolysis, in water jacket, generate chromic acid mixing acid, when chromic acid increasing mixed acid concentration be increased to can be for the concentration of plating tank after, open the pipeline valve between water jacket and purifying groove, high density chromic acid mixing acid in water jacket is inputted to purifying groove and closed this valve, open again the pipeline valve between regeneration and back washing waste water collection tank liquid outlet and water jacket, input mixed waste liquor supplements that to maintain the liquid level of water jacket consistent with inside groove, high density chromic acid mixing acid is after purification process, open the valve between purifying groove liquid outlet and the fluid inlet of heating thickener, make purified high density chromic acid further concentrated, then open the pipeline valve between liquid outlet and the plating tank fluid inlet that heats thickener, purified high density chromic acid input plating tank is carried out to recycle.
The embodiment bis-of the treatment system of chromic acid waste water of the present invention
The embodiment mono-of the treatment system of the present embodiment and chromic acid waste water is basic identical, its difference is, referring to Fig. 7, anode resin storage tank has two covers, respectively anode resin storage tank 1 and anode resin storage tank 2, two cover anode resin storage tank parallel joins, cathode resin groove has two covers, respectively cathode resin groove 1 and cathode resin groove 2, two cover cathode resin groove parallel joins, when running, pipeline valve between the chromic acid waste water liquid outlet of starting cathode resin storage tank 1 and cathode resin groove 1 and plating tank, close the pipeline valve between the chromic acid waste water liquid outlet of anode resin storage tank 2 and cathode resin groove 2 and plating tank, at this moment, can antianode resin storage tank 2 and Zeo-karb and the anionite-exchange resin of cathode resin groove 2 carry out back washing or manipulation of regeneration, wait and enter replacement on duty by turns when completing after back washing or manipulation of regeneration, until the exchange capacity of the Zeo-karb in anode resin storage tank 1 and cathode resin groove 1 and anionite-exchange resin reach capacity or approach saturated after, referring to Fig. 8, close the pipeline valve between the chromic acid waste water liquid outlet of anode resin storage tank 1 and cathode resin groove 1 and plating tank, stop entering of chromic acid waste water, pipeline valve between the chromic acid waste water liquid outlet of starting cathode resin storage tank 2 and cathode resin groove 2 and plating tank simultaneously, and Zeo-karb and anionite-exchange resin to antianode resin storage tank 1 and cathode resin groove 1 carries out back washing or manipulation of regeneration, so carry out on duty by turns, make saturated or approach saturated anode resin storage tank 1 and cathode resin groove 1 regenerate and back washing in, system does not need to stop to chromic acid wastewater treatment.
Claims (8)
1. a chromic acid method of wastewater treatment, is characterized in that, comprises the following steps:
A. chromic acid waste water production system being produced is introduced successively and the anode resin storage tank of Zeo-karb is housed and is equipped with in the resin anion(R.A) groove of anionite-exchange resin, carry out ion-exchange, heavy metal ion and chromate ion in described chromic acid waste water are adsorbed, described chromic acid waste water forms reuse water, described reuse water input reuse water storage tanks, recycles or supplies in subsequent processes for production system;
B. after approaching through the exchange capacity of the Zeo-karb of ion-exchange or reaching capacity, stop to described anode resin storage tank input chromic acid waste water, and described Zeo-karb is carried out to manipulation of regeneration with strong acid solution, after the anode regeneration waste liquid in anode resin storage tank is discharged, carry out back washing processing with the reuse water obtaining in steps A, make described Zeo-karb recover to carry out recycling of next round after exchange capacity, described manipulation of regeneration and back washing are processed to the anode regeneration waste liquid and the anode back washing waste collection that produce pending;
After approaching through the exchange capacity of the anionite-exchange resin of ion-exchange or reaching capacity, stop to described cathode resin groove input chromic acid waste water, and described anionite-exchange resin is carried out to manipulation of regeneration with strong base solution, after the anode regeneration waste liquid in anode resin storage tank is discharged, carry out back washing processing with the reuse water obtaining in steps A, make described anionite-exchange resin recover to carry out recycling of next round after exchange capacity, described manipulation of regeneration and back washing are processed to the negative electrode regeneration waste liquid and the negative electrode back washing waste collection that produce pending;
C. will in described anode regeneration waste liquid, anode back washing waste liquid, negative electrode regeneration waste liquid and negative electrode back washing waste liquid input diaphragm sell, carry out electrolysis treatment, the high density chromic acid mixing acid that electrolysis produces carries out inputting production system after purification process and carries out recycle, and the high concentration basic solution that electrolysis produces carries out cycling and reutilization during for described anionite-exchange resin manipulation of regeneration.
2. chromic acid method of wastewater treatment according to claim 1, is characterized in that:
The step of in step B, Zeo-karb being carried out to manipulation of regeneration is specially: in anode resin storage tank, adding strong acid solution is that concentration is the sulphuric acid soln of 1～4wt%, and Zeo-karb soak time is exceeded to 24 hours;
Or the step of in step B, anionite-exchange resin being carried out to manipulation of regeneration is specially: in cathode resin groove, adding strong base solution is that concentration is the sodium hydroxide solution of 1～4wt%, and anionite-exchange resin soak time is exceeded to 24 hours.
3. chromic acid method of wastewater treatment according to claim 2, is characterized in that: described soak time is between 24 hours to 48 hours.
4. chromic acid method of wastewater treatment according to claim 1, is characterized in that:
Diaphragm sell described in step C is divided into water jacket and inside groove by ion diaphragm, the inside groove of ion diaphragm inner side is negative electrode, the water jacket in ion diaphragm outside is anode, described anode regeneration waste liquid, anode back washing waste liquid, negative electrode regeneration waste liquid and negative electrode back washing waste liquid are inputted in described water jacket, carry out before electrolysis, add described reuse water toward described inside groove, and in the reuse water of described inside groove hydrogen injecting sodium hydroxide solution, make the concentration of sodium hydroxide solution in described inside groove reach 1wt%, reuse water liquid level in described inside groove is consistent with described water jacket liquid level, current density for electrolysis is 2～5A/d ㎡, voltage is 15～30V,
In electrolytic reaction process, in described inside groove, naoh concentration raises gradually, in the time that naoh concentration is more than or equal to 4wt%, concentration processing is fallen in sodium hydroxide solution in described inside groove: shift out in the described inside groove of part sodium hydroxide solution for the regeneration process of the anionite-exchange resin in step B, the liquid level causing declines by adding pure water or reuse water to supplement to negative electrode one side, makes the concentration of sodium hydroxide solution in described inside groove be reduced to 1wt% left and right from 4wt%; Regularly the metal ion oxide compound being deposited on ion diaphragm is rejected; Described in when electrolysis, in water jacket, generate chromic acid mixing acid, along with described chromic acid increasing mixed acid concentration raises, after regularly the high density chromic acid mixing acid in described water jacket being drawn to described water jacket and carried out purification process, input is produced to unite and is carried out recycle, inputs anode regeneration waste liquid, anode back washing waste liquid, negative electrode regeneration waste liquid and negative electrode back washing waste liquid and supplement when anode water level declines;
Purification process described in step C is the high density chromic acid mixing acid that anode electrolysis is gone out, and adds barium carbonate, standing separation after stirring, and upper solution becomes pure chromic acid, uses continuing in defeated time production system of described pure chromic acid.
5. chromic acid method of wastewater treatment according to claim 4, is characterized in that: described pure chromic acid is through the concentrated concentration requirement that reaches production system of heating.
6. a chromic acid Waste Water Treatment, processes for the chromic acid waste water that production system is produced, and it is characterized in that, comprising:
Anode resin storage tank, described anode resin storage tank has P cover, P >=1, anode resin storage tank parallel join described in each, in described anode resin storage tank, Zeo-karb is housed, for carrying out ion-exchange with described chromic acid waste water, and for described Zeo-karb being carried out to manipulation of regeneration and back washing processing;
Cathode resin groove, described cathode resin groove has Q cover, Q >=1, cathode resin groove parallel join described in each, in described resin anion(R.A) groove, anionite-exchange resin is housed, for carrying out ion-exchange with described chromic acid waste water, and for described anionite-exchange resin being carried out to manipulation of regeneration and back washing processing;
Regeneration and back washing waste water collection tank, for collecting anode regeneration waste liquid and the anode back washing waste liquid that each described anode resin storage tank is discharged, also collect negative electrode regeneration waste liquid and negative electrode back washing waste liquid that each described cathode resin groove is discharged, the liquid in described regeneration and back washing waste water collection tank becomes mixed waste liquor;
Reuse water holding tank, the reuse water of discharging for collecting each described cathode resin groove;
Diaphragm sell, for described mixed waste liquor is carried out to electrolysis treatment, described diaphragm sell comprises cell body, is also provided with ion diaphragm in described cell body, cell body is divided into inside groove and water jacket by described ion diaphragm; In described inside groove, be provided with negative plate, in described water jacket, be provided with positive plate;
Purifying groove, the fluid inlet of described purifying groove is connected with described water jacket;
Negative electrode regenerated liquid storage tanks, for storing strong base solution, the liquid outlet of described negative electrode regenerated liquid storage tanks is connected with each described cathode resin groove respectively, and the fluid inlet of described negative electrode regenerated liquid storage tanks is connected with inside groove;
Anode regenerated liquid storage tanks, for storing strong acid solution, the liquid outlet of described anode regenerated liquid storage tanks is connected with each described anode resin storage tank respectively;
The fluid inlet of described production system is connected with reuse water storage tanks, purifying groove respectively, and the chromic acid waste water liquid outlet of described production system is connected with each anode resin storage tank respectively;
The fluid inlet of described reuse water storage tanks is connected with described each cathode resin groove respectively; The liquid outlet of reuse water holding tank is also connected with described cathode resin groove, described anode resin storage tank, described inside groove respectively;
The fluid inlet of described regeneration and back washing waste water collection tank is connected with each anode resin storage tank, each cathode resin groove respectively, and liquid outlet is connected with the described water jacket of diaphragm sell;
Described be connected to be equipped with the controlled connection of pipeline valve, between described groove, have liquid level poor or be provided with pump.
7. a kind of chromic acid Waste Water Treatment according to claim 6, is characterized in that, also comprises heating thickener, and fluid inlet, the liquid outlet of described heating thickener are connected in series with the fluid inlet of described purifying groove and described production system respectively.
8. a kind of chromic acid Waste Water Treatment according to claim 6, is characterized in that,
Described cell body is plastic groove, and described ion diaphragm is N boccaro cylinder, N >=1, and described boccaro cylinder is that volume is that 60～100L, water-permeable are that 0.01～0.05ml/d ㎡ days, sintering temperature are the boccaro cylinder of 1000～1200 ℃;
The current density for electrolysis loading between described positive plate and negative plate is that 2～5A/d ㎡, voltage are 15～30V;
Described negative plate is cylindrical stainless steel cylinder, and described positive plate is chromium plating stereotype;
On described cylindrical stainless steel cylinder, be covered with the aperture that radially runs through barrel wall.
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| CN104355365A (en) * | 2014-10-31 | 2015-02-18 | 武汉钢铁(集团)公司 | Chromium-containing wastewater treatment method capable of realizing zero emission of pollutants |
| CN104860453A (en) * | 2015-05-08 | 2015-08-26 | 青岛锻艺金属有限公司 | Method for treating heavy metal wastewater during machining process |
| CN105314758A (en) * | 2014-07-15 | 2016-02-10 | 苏州林源自动化设备有限公司 | Novel reclaimed water processing and reusing device |
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