CN103833167B - Chromic acid method of wastewater treatment and treatment system - Google Patents
Chromic acid method of wastewater treatment and treatment system Download PDFInfo
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- CN103833167B CN103833167B CN201410093510.8A CN201410093510A CN103833167B CN 103833167 B CN103833167 B CN 103833167B CN 201410093510 A CN201410093510 A CN 201410093510A CN 103833167 B CN103833167 B CN 103833167B
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Abstract
The present invention discloses a kind of chromic acid method of wastewater treatment, comprises after chromic acid waste water and anions and canons resin are carried out ion-exchange, and anions and canons resin back washing and the waste water produced of living again after exchange capacity is saturated process in diaphragm sell; Also disclose a kind of chromic acid Waste Water Treatment, process for the chromic acid waste water that production system is produced, comprise anode resin groove; Cathode resin groove; Regeneration and back washing waste water collection tank; Reuse water holding tank; Diaphragm sell, for mixed waste liquor is carried out electrolysis treatment, diaphragm sell comprises groove body, is also provided with ion diaphragm in this groove body, and groove body is divided into inside groove and outer groove by this ion diaphragm; This inside groove is provided with a negative plate, this outer groove is provided with positive plate; Purifying groove; Cathode regenerative liquid storage tanks, for storing strong base solution; Anode regenerated liquid storage tanks; 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 groove respectively. The present invention is used for the occasion that electroplating industry etc. produces chromic acid waste water.
Description
Technical field
The present invention relates to the treatment process of a kind of chromic acid waste water, also relate to the treatment system of a kind of chromic acid waste water.
Background technology
In prior art, much producing the industry of chromic acid waste water in process of production, the environmental issue that chromic acid wastewater treatment is grown is a big difficult problem 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 is rinsed, hang tool and pole plate rinses, discarded groove fluid exchange etc., electroplating wastewater comprises pre-treatment waste water, chromate waste water, containing chromium complex waste water, chromic acid waste water, comprehensive wastewater etc., generally adopts the technique that classification of waste is collected, processed respectively.
Wherein chromic acid waste water is mainly containing the CrO4 existed with acid radical anion form2-, sulfate radical and with simple positively charged ion form exist metal ion such as Ni2+��Cu2+��Cr6+��Fe3+Deng, the treatment process of prior art mainly contains chemical reduction moderate water-cut stage and anions and canons exchange resin method. process chromic acid waste water with chemical reduction moderate water-cut stage, it is necessary to add in chromic acid waste water precipitation agent and reductive agent, condensing dose, chromic acid process 1 kilogram can produce the mud of 10 kilograms, and it is outstanding that treating processes produces the environmental issue that a large amount of mud makes blowdown cause. the moon promoted at present, cation exchange resin, although emphasizing to accomplish that waste water reclamation utilizes zero release, but the degree that industrial community can accept is low, because resin anion(R.A) has Sodium chromate, except absorption chromate also must through de-sodium process, when absorption makes chromic acid concentration higher, resin injury is big, and Sodium chromate is cleaned a large amount of pure water of clean needs, the accumulation volume of anode metal impurity is many, make cationic exchange resin adsorption deleterious, frequent back washing regeneration waste water resource, the sulfuric acid of back washing regeneration and its purity of sheet alkali require high, the back washing liquid Sulfates of Sodium chromate and anode is made coating by some processing modes, but this kind of mode need professional unified mechanism process, the concentration of the back washing liquid being obtained anode is not high, amount does not cause shipment and delivery cost relatively high very much yet, make for finishing sector operating cost height, make this method possible in theory, actual operation difficulty, and closed-loop operation can not be accomplished, chromic acid recycling waste water reclamation can not be made, therefore the chemical reduction moderate water-cut stage causing secondary pollution is arranged, outside would rather selecting mud, by existing enterprise.
Summary of the invention
First technical problem that the present invention solves is, it is provided that a kind of abandon a large amount of mud outside arrange, make chromic acid wastewater regenerating and recycling and the chromic acid method of wastewater treatment of closed-loop operation.
The 2nd technical problem that the present invention solves is to provide a kind of chromic acid Waste Water Treatment using 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. the chromic acid waste water that production system produces is introduced anode resin groove that Zeo-karb is housed successively and it is equipped with in the cathode resin 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 for production system or supplies in subsequent processes;
B. when the Zeo-karb through ion-exchange exchange capacity close to or after reaching capacity, stop inputting chromic acid waste water to described anode resin groove, and described Zeo-karb strong acid solution is carried out manipulation of regeneration, after the anode regeneration waste liquid in anode resin groove is discharged, back washing process is carried out with the reuse water obtained in steps A, making described Zeo-karb recover to carry out after exchange capacity, next takes turns recycles, and the anode regeneration waste liquid and the anode back washing waste collection that produce described manipulation of regeneration and back washing process are pending;
When the anionite-exchange resin through ion-exchange exchange capacity close to or after reaching capacity, stop inputting chromic acid waste water to this cathode resin groove, and this anionite-exchange resin strong base solution is carried out manipulation of regeneration, after the cathode regenerative waste liquid in cathode resin groove is discharged, back washing process is carried out with the reuse water obtained in steps A, making this anionite-exchange resin recover to carry out after exchange capacity, next takes turns recycles, and the cathode regenerative waste liquid and the negative electrode back washing waste collection that produce manipulation of regeneration and back washing process are pending;
C. electrolysis treatment is carried out by this anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid and negative electrode back washing waste liquid input diaphragm sell, the high density chromic acid mixing acid that electrolysis produces inputs production system after carrying out purification process and carries out recycle, cycling and reutilization when the high concentration basic solution that electrolysis produces is used for this anionite-exchange resin manipulation of regeneration;
Diaphragm sell in step C is divided into outer groove and inside groove by ion diaphragm, inside groove inside ion diaphragm is negative electrode, outer groove outside ion diaphragm is anode, in this anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid and the negative electrode back washing waste liquid outer groove of input, before carrying out electrolysis, reuse water is added toward inside groove, and inject sodium hydroxide solution in the reuse water of inside groove, the concentration of sodium hydroxide solution in inside groove is made to reach 1wt%, reuse water liquid level in inside groove is consistent with outer groove liquid level, and the current density for electrolysis is 2��5A/dm2, voltage be 15��30V; In electrolytic reaction process, in inside groove, naoh concentration raises gradually, when naoh concentration is more than or equal to 4wt%, sodium hydroxide solution in inside groove is fallen concentration process: move out of in part inside groove sodium hydroxide solution for the regeneration process of the anionite-exchange resin in step B, the liquid level decline caused, by adding pure water or reuse water supplements to negative electrode side, makes the concentration of sodium hydroxide solution in inside groove be reduced to 1wt% from 4wt%; Regularly the metal ion oxide compound being deposited on ion diaphragm is rejected; During electrolysis, outer groove generates chromic acid mixing acid, along with chromic acid increasing mixed acid concentration raises, after regularly the high density chromic acid mixing acid in outer groove being drawn outer groove and carrying out purification process, input production system carries out recycle, inputs anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid and negative electrode back washing waste liquid and supplement during anode water level decreasing;Purification process in step C is: first stops anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid and negative electrode back washing waste liquid and enters in diaphragm sell, determine that sodium ion almost dissociates in negative electrode again, this can be bordering on zero for standard from electric current trend, the high density then gone out by anode electrolysis
The high density chromic acid mixing acid gone out by anode electrolysis, adds barium carbonate, standing separation after stirring, and upper solution becomes pure chromic acid, and described pure chromic acid is produced for defeated time the continuous use of System relays.
The useful effect of chromic acid method of wastewater treatment of the present invention is: owing to technique scheme adopts anions and canons exchange method and membrane electrolysis to be combined with each other, allow chromic acid waste water by carrying out ion-exchange with anion and cation exchange resin, make chromic acid waste water turn into the reuse water that can be again back to use in production system, to the moon, in the regeneration that Zeo-karb carries out and back washing subsequent disposal, reuse water is used to replace the pure water of prior art, save large quantities of equipment investments that pure water is produced, 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, cathode regenerative waste liquid and negative electrode back washing waste liquid input diaphragm sell carry out electrolysis treatment, free property according to sodium ion is much larger than the characteristic of other metal ions, when being energized, sodium ion is easy to enter cathodic area, and the little metal ion of free property is such as Fe3+��Cr6+��Ca2+Deng not being gathered on ion diaphragm by the ion diaphragm of diaphragm sell by the surface of anode side, form oxide compound or oxyhydroxide, it is attached to barrier film on the side of anode, is easy to remove by scraping method, and ion diaphragm electrolysis can go out alkali smoothly by the negative electrode place of side of negative electrode, the anode place of another side of ion diaphragm electrolysis can go out acid. utilize separating of ion diaphragm, can easily sodium hydroxide, chromic acid, sulfuric acid and metallic impurity are separated, and schedule of operation is simple, operating cost is low, unique throw out produced is exactly a small amount of barium sulfate produced when purification process, it can be separated with chromic acid easily, through precipitation, collect, cleaning can also become the product of regeneration, and need not arrange outward, precipitation neutralisation compared to existing technology often processes the amount that 1 kilogram of chromic acid waste water produces 10 kilograms of sediment waste, the a small amount of barium sulfate produced during purification process seems very little, make superiority of the present invention obvious, on the other hand, membrane electrolysis relieves and uses ion-exchange-resin process to be produced contingency question in prior art: cycling and reutilization when the high concentration basic solution that a, electrolysis produce is used for anionite-exchange resin manipulation of regeneration, avoids and improves production cost owing to back washing regeneration sheet alkali purity requires high, the concentration of chromic acid can also be improved further, as in electroplating industry, the concentration improving chromic acid makes its concentration requirement reaching 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, it is not necessary to arrange outward, b, the concentration avoiding the back washing liquid owing to being obtained anode in prior art are not high, cause and cannot be back to use in production system, and amount is also little, but look for the unified mechanism process of specialty, cause shipment and delivery cost relatively high, make the problem high for finishing sector operating cost. the program makes production operation management process simple, as long as regularly concentration process being fallen in the sodium hydroxide solution of inside groove, the chromic acid mixed acid solution of regular external groove carries out falling concentration process, and regularly strike off the metal oxide or oxyhydroxide being attached on ion diaphragm, it is not necessary to waste of manpower is kept on post.
In electrolysis treatment process, at ion diaphragm by the reaction at negative electrode place of the side of negative electrode it is:
H2O=2H++OH-
Na++OH-=NaOH
Catholyte goes out alkali, it is possible to is recovered and continues to use.
At ion diaphragm by the reaction of side of anode it is:
Fe3++OH-=Fe (OH)3��
Other metallic cations such as iron class are deposited in the surface of ion diaphragm by anode side, it is possible to regularly struck off.
At ion diaphragm by the reaction at anode place of anode side it is:
H2O=2H++OH-
Cr2O7 2-+H+=H2Cr2O7
SO4 2-+H+=H2SO4
By adding after removing sulfuric acid after purifying, production system continues to use the chromic acid mixing acid that anode electrolysis goes out.
Purification process in step C is in the high density chromic acid mixing acid input purifying groove gone out by anode electrolysis, adds barium carbonate, standing separation after stirring, gets upper solution and add the use of production system resume.
Purification reaction is:
BaCO3+H2SO4=BaSO4��+H2O+CO2��
Sulfuric acid generates barium sulfate precipitate so that the purity of chromic acid increases.
The main chemical reactions in ion exchange process between Zeo-karb and chromic acid waste water is: the Fe in chromic acid waste water3+��Ni2+��Cu2+��Cr6+Exchange Deng the positively charged ion in positively charged ion and Zeo-karb; Cation exchange reaction formula is as follows:
Fe3++ 3RH=FeR3+3H+
Ni2++ 2RH=NiR2+2H+
Cu2++ 2RH=CuR2+2H+
Cr2++ 3RH=CrR6+6H+
In each production industry, the positively charged ion in chromic acid waste water is different, as in electroplating industry, material according to plated item is different and different, as given the plating of iron product, the positively charged ion then electroplated in chromic acid waste water is mainly iron ion, carries out electroplating to copper product, and the positively charged ion in plating chromic acid waste water 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 reduced further, thus make chromic acid waste water has more H+Maintain Cr2O7 2-Existence; In addition, lower PH value also can promote that chromic acid waste water is when carrying out ion-exchange with anionite-exchange resin the moon, is more conducive to the absorption of chromate negatively charged ion. In steps A, the main chemical reactions in the process of anionresin is: the Cr in chromic acid waste water2O7 2-, CrO4 2-��CrO4 2-��SO4 2-Exchange Deng the positive negatively charged ion in negatively charged ion and anionite-exchange resin; Anion exchange reaction formula is as follows:
Cr2O7 2-+ 2ROH=R2Cr2O7+2OH-
CrO4 2-+ 2ROH=R2CrO4+2OH-
SO4 2-+ 2ROH=R2SO4+2OH-
From reaction it may be seen that when adsorbing chromate negatively charged ion, the anionite-exchange resin Cr of as much2O7 2-Exchange capacity be CrO4 2-The twice of exchange capacity,
As a concrete scheme of technique scheme, the step that Zeo-karb carries out in step B manipulation of regeneration is specially: to add strong acid solution in anode resin groove be concentration is the sulphuric acid soln of 1��4wt%, to Zeo-karb soak time more than 24 hours;
Or the step that anionite-exchange resin carries out in step B manipulation of regeneration is specially: to add strong base solution in cathode resin groove be concentration is the sodium hydroxide solution of 1��4wt%, to anionite-exchange resin soak time more than 24 hours;
The reaction of Zeo-karb regeneration is as follows:
2FeR3+3H2SO4=Fe2(SO4)3+6RH
NiR2+H2SO4=NiSO4+2RH
CuR2+H2SO4=CuSO4+2RH
CrR6+3H2SO4=Cr (SO4)3+6RH
Anionite-exchange resin regenerative response is as follows:
R2Cr2O7+ 2NaOH=Na2Cr2O7+2ROH
R2CrO4+ 2NaOH=Na2CrO4+2ROH
R2SO4+ 2NaOH=Na2SO4+2ROH
The product that anion regeneration process produces is mainly Na2Cr2O7And Na2SO4��
As the further improvement to technique scheme, soak time is little between 48 hours 24. This time length ratio is relatively reasonable, had both made Zeo-karb regeneration or anionite-exchange resin regeneration completely, and had controlled again in the scope improving production efficiency to greatest extent.
As the further improvement to technique scheme, soak time is little between 48 hours 24. This time length ratio is relatively reasonable, had both made Zeo-karb regeneration or anionite-exchange resin regeneration completely, and had controlled again in the scope improving production efficiency to greatest extent.
As the further improvement to technique scheme, pure chromic acid is through the concentrated concentration requirement reaching production system of heating.
The technical scheme of the 2nd technical problem that the present invention solves is:
A kind of chromic acid Waste Water Treatment, processes for chromic acid waste water production system produced, comprising:
Anode resin groove, this anode resin groove has P to overlap, P >=1, each anode resin groove parallel join, anode resin groove, built with Zeo-karb, for carrying out ion-exchange with chromic acid waste water, and processes for Zeo-karb carries out manipulation of regeneration and back washing;
Cathode resin groove, this cathode resin groove has Q to overlap, Q >=1, each cathode resin groove parallel join, cathode resin groove, built with anionite-exchange resin, for carrying out ion-exchange with chromic acid waste water, and processes for anionite-exchange resin carries out manipulation of regeneration and back washing;
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 groove is discharged, also collect cathode regenerative waste liquid and negative electrode back washing waste liquid that each cathode resin groove is discharged, regeneration and back washing waste water collection tank in liquid become mixed waste liquor;
Reuse water holding tank, for collecting the reuse water that each cathode resin groove is discharged;
Diaphragm sell, for mixed waste liquor is carried out electrolysis treatment, diaphragm sell comprises groove body, is also provided with ion diaphragm in this groove body, and groove body is divided into inside groove and outer groove by this ion diaphragm; This inside groove is provided with a negative plate, this outer groove is provided with positive plate; Purifying groove, the fluid inlet of this purifying groove groove outer with this is connected;
Cathode regenerative liquid storage tanks, for storing strong base solution, the liquid outlet of this cathode regenerative liquid storage tanks is connected with each cathode resin groove respectively, and the fluid inlet of this cathode regenerative 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 groove 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 groove 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 groove, inside groove respectively;
The fluid inlet of regeneration and back washing waste water collection tank is connected with each anode resin groove, each cathode resin groove respectively, and liquid outlet is connected with the outer groove in diaphragm sell;
This controlled connection being connected and being and be equipped with pipeline valve, has liquid level difference or is provided with pump between each groove.
The useful effect of chromic acid Waste Water Treatment of the present invention is: owing to technique scheme adopts Q to overlap cathode resin groove and each outfit controlled connection of pipeline valve parallel of P cover anode resin groove, the running of system is carried out by means of only control valve, chromic acid Waste Water Treatment uses together with production system, without the need to carrying out carrying when each link material shifts, save manpower, reduce production cost.
Concrete operation is as follows, work as P=1, during Q=1, whole chromic acid Waste Water Treatment intermittent type operates, first the pipeline valve that the chromic acid waste water liquid outlet of production system is connected is started with anode resin groove, make chromic acid waste water enter anode resin groove, then enter cathode resin groove, enter reuse water storage tanks after making chromic acid waste water become reuse water for subsequent use;When Zeo-karb and anionite-exchange resin is saturated or close to after saturated, close the pipeline valve that the chromic acid waste water liquid outlet of production system is connected with anode resin groove, and close the pipeline valve between cathode resin groove and reuse water storage tanks, then the pipeline valve between the liquid outlet of anode regenerated liquid storage tanks and anode resin groove is opened, make the strong base solution input anode resin groove of anode regenerated liquid storage tanks, this valve is closed after reaching liquid level requirement, open the pipeline valve between the liquid outlet of cathode regenerative liquid storage tanks and cathode resin groove, make the strong acid solution input cathode resin groove of cathode regenerative liquid storage tanks, this valve is closed after reaching liquid level requirement, to Zeo-karb, anionite-exchange resin carries out manipulation of regeneration, after completing manipulation of regeneration, open anode resin groove respectively, 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 cathode regenerative waste liquid, open liquid outlet and the cathode resin groove of reuse water holding tank, pipeline valve between anode resin groove, make reuse water respectively to Zeo-karb, anionite-exchange resin carries out back washing, the anode back washing waste liquid produced and negative electrode back washing waste liquid continue to arrange into regeneration and back washing waste water collection tank, complete back washing and after emptying waste liquid, close anode resin groove, pipeline valve between the fluid inlet of cathode resin groove and regeneration and back washing waste water collection tank, start the pipeline valve that the chromic acid waste water liquid outlet of production system is connected with anode resin groove, next carrying out chromic acid wastewater treatment takes turns circulation. to the mixed waste liquor process of regeneration and back washing waste water collection tank: open regeneration and the pipeline valve between back washing waste water collection tank liquid outlet and the outer groove of diaphragm sell, make in the mixed waste liquor outer groove of input, open the pipeline valve between the liquid outlet of reuse water holding tank and inside groove, toward inside groove input reuse water, and inject sodium hydroxide solution in the reuse water of inside groove, making the concentration of sodium hydroxide solution in inside groove reach 1wt%, the reuse water liquid level in inside groove is consistent with outer groove liquid level, in electrolytic reaction process, in inside groove, naoh concentration raises gradually, when naoh concentration is more than or equal to 4wt%, sodium hydroxide solution in inside groove is fallen concentration process: open the pipeline valve between the fluid inlet of inside groove and cathode regenerative liquid storage tanks, sodium hydroxide solution part in inside groove is made to be input to cathode regenerative liquid storage tanks, then this valve is closed, and open the pipeline valve between inside groove and reuse water storage tanks, reuse water adds to inside groove, inside groove liquid level is made to remain consistent with outer groove liquid level, in inside groove, the concentration of sodium hydroxide solution is reduced to 1wt% from 4wt%, regularly the metal ion oxide compound being deposited on ion diaphragm is rejected, during electrolysis, outer groove generates chromic acid mixing acid, when chromic acid increasing mixed acid concentration be increased to can for the concentration of plating tank after, open the pipeline valve between outer groove and purifying groove, high density chromic acid mixing acid in outer groove is inputted purifying groove and closes this valve, open regeneration and the pipeline valve between back washing waste water collection tank liquid outlet and outer groove again, it is consistent with inside groove that input mixed waste liquor carries out supplementing the liquid level maintaining outer 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, high density chromic acid input production system through purifying is carried out recycle.
As P > 1, during Q > 1, the running of chromic acid Waste Water Treatment is substantially identical with above-mentioned running, its difference is, Q overlaps cathode resin groove and P overlap anode resin groove and be divided into two groups or more, running only starts the pipeline valve between the chromic acid waste water liquid outlet of wherein one group of anode resin groove and cathode resin groove and production system every time, close the pipeline valve between the chromic acid waste water liquid outlet of other groups and production system, until that group started self reaches capacity or close to after saturated at process chromic acid waste water, closing duct valve stops entering of chromic acid waste water, start the pipeline valve between the chromic acid waste water liquid outlet of other groups and production system simultaneously, so carry out on duty by turns, make saturated or close to that saturated group carrying out regenerating and when back washing, system is to chromic acid wastewater treatment operate continuously, do not need batch operation.
As the further improvement to technique scheme, also comprising 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 that the concentration of the pure chromic acid obtained from purifying groove is adjustable, can reach the requirement of production system.
As a concrete scheme to technique scheme, groove body is plastic groove, and this ion diaphragm is N number of boccaro cylinder, N >=1, and this boccaro cylinder to be volume be 60��100L, water-permeable are 0.01��0.05ml/dm2My god, sintering temperature be the boccaro cylinder of 1000��1200 DEG C; The current density for electrolysis loaded between the positive plate being somebody's turn to do and negative plate is 2��5A/dm2, voltage be 15��30V; This negative plate is cylindrical stainless steel cylinder, and this positive plate is chromium plating stereotype, and this cylindrical stainless steel cylinder is covered with the aperture radially running through barrel wall. Boccaro cylinder because containing quantitative quartz sand, possessing certain water-permeable under high temperature sintering, than the etch of general pottery more ability chromic acid; Even if when life-time service, its water-permeable still remains unchanged; When multiple boccaro cylinder connects use, the distribution of electric current is still even so that electrolytic regeneration is effective. Because negative plate is made cylindrical, it can be made to reach low current and distribution of current even, catholyte can be dissociated toward anode with the form of chromate, and ferric chromate is precipitated, reach and effectively remove metallic impurity fast.
Accompanying drawing explanation
Fig. 1 is the cathode hydrogen sodium oxide concentration curve of the embodiment two of the treatment process of the chromic acid waste water of the present invention;
Fig. 2 is the cathode hydrogen sodium oxide concentration curve of the embodiment three of the treatment process of the chromic acid waste water of the present invention;
Fig. 3 is the block diagram of the embodiment one of the treatment system of the chromic acid waste water of the present invention;
Fig. 4 be the treatment system of the chromic acid waste water of the present invention embodiment one in the structural representation of chromic acid electrolytic film groove;
Fig. 5 be the treatment system of the chromic acid waste water of the present invention embodiment one in the negative plate front view of chromic acid electrolytic film groove;
Fig. 6 is the vertical view of Fig. 5;
Fig. 7 is the block diagram of the embodiment two of the treatment system of the chromic acid waste water of the present invention;
Fig. 8 is the block diagram of embodiment two another kind of state of the treatment system of the chromic acid waste water of the present invention.
Embodiment
Below in conjunction with drawings and Examples, the utility model is illustrated further.
The embodiment one of the treatment process of the chromic acid waste water of the present invention
First chromic acid waste water is injected the anode resin groove that Zeo-karb is housed and carries out ion-exchange, and then the chromic acid waste water flowed out from anode resin groove is injected the cathode resin groove that anionite-exchange resin is housed, chromic acid waste water becomes the reuse water meeting emission standard, and reuse water input reuse water storage tanks is for subsequent use; When the Zeo-karb through ion-exchange exchange capacity close to or after reaching capacity, stop anode resin storage tank input chromic acid waste water, and by Zeo-karb concentration be the sulphuric acid soln of 1��4wt% to Zeo-karb soak time more than 48 hours, now sulphuric acid soln becomes anode regeneration waste liquid, anode regeneration waste liquid is collected pending, with reuse water, Zeo-karb being carried out back washing, anode back washing waste collection back washing produced is pending;Zeo-karb recovers to carry out after exchange capacity that next takes turns recycles.
When the anionite-exchange resin through ion-exchange exchange capacity close to or after reaching capacity, stop inputting chromic acid waste water to cathode resin groove, and by anionite-exchange resin concentration be the sodium hydroxide solution of 1��4wt% to Zeo-karb soak time more than 48 hours, now sodium hydroxide solution becomes cathode regenerative waste liquid, by pending for cathode regenerative waste collection, with reuse water, anionite-exchange resin being carried out back washing, negative electrode back washing waste collection back washing produced is pending; Anionite-exchange resin recovers to carry out after exchange capacity that next takes turns recycles.
The groove body of diaphragm sell is divided into outer groove and inside groove by the ceramic cylinder of built-in two each 60L of volume, and ceramic cylinder, as ion diaphragm, is negative electrode inside ceramic cylinder, and the outer groove outside ceramic cylinder is anode, and the current density for electrolysis is 2��5A/dm2, voltage be 15��30V; Temperature is 50 DEG C.
Anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid are become mixed waste liquor together with negative electrode back washing waste collection, mixed waste liquor is inputted in outer groove, reuse water is added in ceramic cylinder, and reuse water in ceramic cylinder injects NaoH solution, making the reuse water in ceramic cylinder be about 1wt% containing the concentration of NaoH, the reuse water liquid level in ceramic cylinder is consistent with outer groove liquid level.
In electrolytic reaction process, in ceramic cylinder, naoh concentration raises gradually, when naoh concentration is more than or equal to 4wt%, sodium hydroxide solution in ceramic cylinder is fallen concentration process: move out of sodium hydroxide solution in part ceramic cylinder and store for subsequent use, the liquid level decline caused supplements to negative electrode side by adding reuse water, makes the concentration of sodium hydroxide solution in ceramic cylinder be reduced to about 1wt% from 4wt%; Regularly the precipitation by metallic ion thing being deposited on ceramic cylinder outer wall is rejected; During electrolysis, outer groove generates chromic acid mixing acid, when the rising of chromic acid increasing mixed acid concentration reaches production system service requirements, high density chromic acid mixing acid in outer groove is drawn outer groove and carries out purification process, purification process is by high density chromic acid mixing acid, adding barium carbonate, standing separation after stirring, upper solution becomes pure chromic acid, defeated for pure chromic acid time is produced the continuous use of System relays, inputs mixed waste liquor during anode water level decreasing and supplement; The sodium hydroxide solution moved out from ceramic cylinder, for the regeneration process of step anionite-exchange resin.
The embodiment two of the treatment process of the chromic acid waste water of the present invention
The embodiment one of the treatment process of the present embodiment and chromic acid waste water is substantially identical, its difference is, the electrolysis procedure of diaphragm sell: get the outer groove that the Sodium chromate that negative electrode back washing liquid 500L includes 10g/L puts into diaphragm sell, reuse water is added in ceramic cylinder, and the NaoH solution injecting 1% in reuse water in ceramic cylinder is 6.33g/L through titrimetry NaoH concentration, reuse water liquid level in ceramic cylinder is consistent with outer groove liquid level, operational condition: temperature: 50 DEG C. Energising carries out electrolysis, and electrolysis 120 hours period China and foreign countries groove increases mixed waste liquor 240L, and ceramic cylinder supplements reuse 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/L |
| 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 see Fig. 1.
When just having started electrolysis, electric current is very little, because temperature is lower, along with the time of electrolysis increases, temperature constantly raises, the naoh concentration just having started ceramic cylinder only 1%, but to after 16 hours, electric current increase is very fast, and naoh concentration also sharply increases, but to the just significantly decline of electric current after 72 hours, naoh concentration increases speed and also becomes slow, after having arrived 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 three of the treatment process of the chromic acid waste water of the present invention
The embodiment two of the treatment process of the present embodiment and chromic acid waste water is substantially identical, its difference is, the electrolysis procedure of diaphragm sell: the outer groove that mixed waste liquor 500L is 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/L 8--> |
| 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 see Fig. 2.
Ceramic cylinder outer wall adheres to a lot of oxide compounds, and result is as follows by analysis:
Ca:6%Cu:1.2%
Si:4.1%Pb:1.0
Mg:2%Ni:400ppm
Cr:1.5%Zn:200ppm
The present embodiment compares with the embodiment two of the treatment process of chromic acid waste water, and maximum difference is that the ceramic cylinder outer wall of the present embodiment produces a large amount of dirt settlings, it is possible to strike off easily.
The embodiment of the treatment process of three chromic acid waste water shows, the ionization concentration of the sodium hydroxide of inside groove is only paid close attention to during operation, whether the naoh concentration of detection inside groove does, to determine, the operation falling concentration, when the naoh concentration of negative electrode is more than 4%, does the operation that concentration falls in sodium hydroxide; The chromic acid mixing acid that outer groove produces and the metallic impurity being attached to ceramic cylinder outer wall all need not as the references of operation, until the concentration of the chromic acid mixing acid of outer groove reaches electrodepositable concentration just must measure sulfuric acid concentration, in the present embodiment, when the concentration of chromic acid mixing acid reaches 20��50g/L or more, with barium carbonate, sulfuric acid falls, dense chromic acid degree is improved again, and metallic impurity can be attached to ceramic cylinder periphery with thickening equipment.
The embodiment one of the treatment system of the chromic acid waste water of the present invention
See Fig. 3, the production system in the present embodiment is plating tank, chromic acid Waste Water Treatment, processes for the chromic acid waste water produced by plating tank, comprising:
1 cover anode resin groove, anode resin groove, built with Zeo-karb, for carrying out ion-exchange with chromic acid waste water, and processes for Zeo-karb carries out manipulation of regeneration and back washing;
1 cover cathode resin groove, cathode resin groove, built with anionite-exchange resin, for carrying out ion-exchange with chromic acid waste water, and processes for anionite-exchange resin carries out manipulation of regeneration and back washing;
Regeneration and back washing waste water collection tank, for collecting anode regeneration waste liquid and the anode back washing waste liquid that anode resin groove is discharged, also collecting the cathode regenerative waste liquid discharged of cathode resin groove and negative electrode back washing waste liquid, the liquid in regeneration and back washing waste water collection tank becomes mixed waste liquor;
Reuse water holding tank, for collecting the reuse water that cathode resin groove is discharged;
Diaphragm sell, for mixed waste liquor is carried out electrolysis treatment, diaphragm sell comprises groove body, is also provided with ion diaphragm in groove body, and groove body is divided into inside groove and outer groove by ion diaphragm; Inside groove is provided with a negative plate, this outer groove is provided with positive plate;See Fig. 4, electrolytic cell body is the plastic groove 11 of acid and alkali-resistance, is provided with the chromium plating stereotype 12 as positive plate in plastic groove 11; Also being provided with as barrier film 4 boccaro cylinders 13 in plastic groove 11, the cylinder body inner sleeve of each boccaro cylinder 13 has a cylindrical stainless steel cylinder 14 as negative plate. Boccaro cylinder 13 is 0.01��0.05ml/dm for volume is 60��100L, water-permeable2My god, sintering temperature be the boccaro cylinder of 1000��1200 DEG C. The current density for electrolysis wherein loaded between positive plate and negative plate is 2��5A/dm2, voltage be 15��30V.
See Fig. 5, Fig. 6, cylindrical stainless steel cylinder 14 being covered with the aperture 141 running through barrel along cylinder radial direction, cylinder inboard wall arranges a cathode connection terminal 142. During use, aperture 141 on cylindrical stainless steel cylinder 14 can increase the contact area with liquid, make in cylindrical stainless steel cylinder 14 outside surface all and liquid reactions, and the chromate produced in cylindrical stainless steel cylinder 14 dissociates by aperture anode, accelerates electrolysis
Reviewing Fig. 4, the fluid inlet of purifying groove groove outer with this is connected;
Cathode regenerative liquid storage tanks, for storing strong base solution, the liquid outlet of this cathode regenerative liquid storage tanks is connected with cathode resin groove respectively, and the fluid inlet of cathode regenerative 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 groove;
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 groove; 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 groove, inside groove respectively;
The fluid inlet of regeneration and back washing waste water collection tank is connected with anode resin groove, cathode resin groove, and liquid outlet is connected with the outer groove in diaphragm sell;
The above-mentioned connected controlled connection being outfit pipeline valve, has liquid level difference or is provided with pump between each groove.
Concrete operation is as follows, first starts the pipeline valve that the chromic acid waste water liquid outlet of plating tank is connected with anode resin groove, makes chromic acid waste water enter anode resin groove, then enter cathode resin groove, enters reuse water storage tanks for subsequent use after making chromic acid waste water become reuse water, when Zeo-karb and anionite-exchange resin is saturated or close to after saturated, close the pipeline valve that the chromic acid waste water liquid outlet of plating tank is connected with anode resin groove, and close the pipeline valve between cathode resin groove and reuse water storage tanks, then the pipeline valve between the liquid outlet of anode regenerated liquid storage tanks and anode resin groove is opened, make the strong acid solution input anode resin groove of anode regenerated liquid storage tanks, this valve is closed after reaching liquid level requirement, open the pipeline valve between the liquid outlet of cathode regenerative liquid storage tanks and cathode resin groove, make the strong base solution input cathode resin groove of cathode regenerative liquid storage tanks, this valve is closed after reaching liquid level requirement, to Zeo-karb, anionite-exchange resin carries out manipulation of regeneration, after completing manipulation of regeneration, open anode resin groove respectively, 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 cathode regenerative waste liquid, open liquid outlet and the cathode resin groove of reuse water holding tank, pipeline valve between anode resin groove, make reuse water respectively to Zeo-karb, anionite-exchange resin carries out back washing, the anode back washing waste liquid produced and negative electrode back washing waste liquid continue to arrange into regeneration and back washing waste water collection tank, complete back washing and after emptying waste liquid, close anode resin groove, pipeline valve between the fluid inlet of cathode resin groove and regeneration and back washing waste water collection tank, start the pipeline valve that the chromic acid waste water liquid outlet of plating tank is connected with anode resin groove, next carrying out chromic acid wastewater treatment takes turns circulation. to the mixed waste liquor process of regeneration and back washing waste water collection tank: open regeneration and the pipeline valve between back washing waste water collection tank liquid outlet and the outer groove of diaphragm sell, make in the mixed waste liquor outer groove of input, open the pipeline valve between the liquid outlet of reuse water holding tank and inside groove, toward inside groove input reuse water, and inject sodium hydroxide solution in the reuse water of inside groove, making the concentration of sodium hydroxide solution in inside groove reach 1wt%, the reuse water liquid level in inside groove is consistent with outer groove liquid level,In electrolytic reaction process, in inside groove, naoh concentration raises gradually, when naoh concentration is more than or equal to 4wt%, sodium hydroxide solution in inside groove is fallen concentration process: open the pipeline valve between the fluid inlet of inside groove and cathode regenerative liquid storage tanks, sodium hydroxide solution part in inside groove is made to be input to cathode regenerative liquid storage tanks, then this valve is closed, and open the pipeline valve between inside groove and reuse water storage tanks, reuse water adds to inside groove, inside groove liquid level is made to remain consistent with outer groove liquid level, in inside groove, the concentration of sodium hydroxide solution is reduced to about 1wt% from 4wt%, regularly the metal ion oxide compound being deposited on ion diaphragm is rejected, during electrolysis, outer groove generates chromic acid mixing acid, when chromic acid increasing mixed acid concentration be increased to can for the concentration of plating tank after, open the pipeline valve between outer groove and purifying groove, high density chromic acid mixing acid in outer groove is inputted purifying groove and closes this valve, open regeneration and the pipeline valve between back washing waste water collection tank liquid outlet and outer groove again, it is consistent with inside groove that input mixed waste liquor carries out supplementing the liquid level maintaining outer groove, high density chromic acid mixing acid is after purification process, open the valve between the fluid inlet of purifying groove liquid outlet and heating thickener, high density chromic acid through purifying is concentrated further, then the pipeline valve between the liquid outlet of heating thickener and plating tank fluid inlet is opened, high density chromic acid input plating tank through purifying is carried out recycle.
The embodiment two of the treatment system of the chromic acid waste water of the present invention
The embodiment one of the treatment system of the present embodiment and chromic acid waste water is substantially identical, its difference is, see Fig. 7, anode resin groove has two covers, it is anode resin groove 1 and anode resin groove 2 respectively, two cover anode resin groove parallel joins, cathode resin groove has two covers, it is cathode resin groove 1 and cathode resin groove 2 respectively, two cover cathode resin groove parallel joins, during running, start the pipeline valve between the chromic acid waste water liquid outlet of anode resin groove 1 and cathode resin groove 1 and plating tank, close the pipeline valve between the chromic acid waste water liquid outlet of anode resin groove 2 and cathode resin groove 2 and plating tank, at this moment, Zeo-karb and the anionite-exchange resin of antianode resin storage tank 2 and cathode resin groove 2 can carry out back washing or manipulation of regeneration, wait after completing back washing or manipulation of regeneration and enter replacement on duty by turns, until the exchange capacity of Zeo-karb in anode resin groove 1 and cathode resin groove 1 and anionite-exchange resin reaches capacity or close to after saturated, see Fig. 8, close the pipeline valve between the chromic acid waste water liquid outlet of anode resin groove 1 and cathode resin groove 1 and plating tank, stop entering of chromic acid waste water, start the pipeline valve between the chromic acid waste water liquid outlet of anode resin groove 2 and cathode resin groove 2 and plating tank simultaneously, and Zeo-karb and the anionite-exchange resin of antianode resin storage tank 1 and cathode resin groove 1 is carried out back washing or manipulation of regeneration, so carry out on duty by turns, make saturated or close to saturated anode resin groove 1 and cathode resin groove 1 carrying out regenerating and when back washing, chromic acid wastewater treatment is not needed to stop by system.
Claims (7)
1. a chromic acid method of wastewater treatment, it is characterised in that, comprise the following steps:
A. the chromic acid waste water that production system produces is introduced anode resin groove that Zeo-karb is housed successively and it is equipped with in the cathode resin 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 for production system or supplies in subsequent processes;
B. when the Zeo-karb through ion-exchange exchange capacity close to or after reaching capacity, stop inputting chromic acid waste water to described anode resin groove, and described Zeo-karb strong acid solution is carried out manipulation of regeneration, after the anode regeneration waste liquid in anode resin groove is discharged, back washing process is carried out with the reuse water obtained in steps A, making described Zeo-karb recover to carry out after exchange capacity, next takes turns recycles, and the anode regeneration waste liquid and the anode back washing waste collection that produce described manipulation of regeneration and back washing process are pending;
When the anionite-exchange resin through ion-exchange exchange capacity close to or after reaching capacity, stop inputting chromic acid waste water to described cathode resin groove, and described anionite-exchange resin strong base solution is carried out manipulation of regeneration, after the cathode regenerative waste liquid in cathode resin groove is discharged, back washing process is carried out with the reuse water obtained in steps A, making described anionite-exchange resin recover to carry out after exchange capacity, next takes turns recycles, and the cathode regenerative waste liquid and the negative electrode back washing waste collection that produce described manipulation of regeneration and back washing process are pending;
C. electrolysis treatment is carried out by described anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid and negative electrode back washing waste liquid input diaphragm sell, the high density chromic acid mixing acid that electrolysis produces inputs production system after carrying out purification process and carries out recycle, carries out cycling and reutilization when the high concentration basic solution that electrolysis produces is used for described anionite-exchange resin manipulation of regeneration, described diaphragm sell is divided into outer groove and inside groove by ion diaphragm, inside groove inside ion diaphragm is negative electrode, outer groove outside ion diaphragm is anode, described anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid and negative electrode back washing waste liquid input in described outer groove, before carrying out electrolysis, described reuse water is added toward described inside groove, and inject sodium hydroxide solution in the reuse water of described inside groove, the concentration of sodium hydroxide solution in described inside groove is made to reach 1wt%, reuse water liquid level in described inside groove is consistent with described outer groove 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, when naoh concentration is more than or equal to 4wt%, sodium hydroxide solution in described inside groove is fallen concentration process: move out of 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 decline caused, by adding pure water or reuse water supplements to negative electrode side, makes the concentration of sodium hydroxide solution in described inside groove be reduced to about 1wt% from 4wt%; Regularly the metal ion oxide compound being deposited on ion diaphragm is rejected; During electrolysis, described outer groove generates 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 outer groove being drawn described outer groove and carrying out purification process, input production system carries out recycle, inputs anode regeneration waste liquid, anode back washing waste liquid, cathode regenerative waste liquid and negative electrode back washing waste liquid and supplement during anode water level decreasing;
Purification process described in step C is the high density chromic acid mixing acid gone out by anode electrolysis, adds barium carbonate, standing separation after stirring, and upper solution becomes pure chromic acid, and described pure chromic acid is produced for defeated time the continuous use of System relays.
2. chromic acid method of wastewater treatment according to claim 1, it is characterised in that:
The step that Zeo-karb carries out in step B manipulation of regeneration is specially: to add strong acid solution in anode resin groove be concentration is the sulphuric acid soln of 1��4wt%, to Zeo-karb soak time more than 24 hours;
Or the step that anionite-exchange resin carries out in step B manipulation of regeneration is specially: to add strong base solution in cathode resin groove be concentration is the sodium hydroxide solution of 1��4wt%, to anionite-exchange resin soak time more than 24 hours.
3. chromic acid method of wastewater treatment according to claim 2, it is characterised in that: described soak time is little between 48 hours 24.
4. chromic acid method of wastewater treatment according to claim 1, it is characterised in that: described pure chromic acid is through the concentrated concentration requirement reaching production system of heating.
5. a chromic acid Waste Water Treatment, processes for chromic acid waste water production system produced, it is characterised in that, comprising:
Anode resin groove, described anode resin groove has P to overlap, P >=1, anode resin groove parallel join described in each, described anode resin groove, built with Zeo-karb, for carrying out ion-exchange with described chromic acid waste water, and processes for described Zeo-karb carries out manipulation of regeneration and back washing;
Cathode resin groove, described cathode resin groove has Q to overlap, Q >=1, cathode resin groove parallel join described in each, described cathode resin groove, built with anionite-exchange resin, for carrying out ion-exchange with described chromic acid waste water, and processes for described anionite-exchange resin carries out manipulation of regeneration and back washing;
Regeneration and back washing waste water collection tank, for collecting anode regeneration waste liquid and the anode back washing waste liquid that anode resin groove described in each is discharged, the liquid also collected in the cathode regenerative waste liquid and negative electrode back washing waste liquid, described regeneration and back washing waste water collection tank that cathode resin groove described in each discharges becomes mixed waste liquor;
Reuse water holding tank, for collecting the reuse water that cathode resin groove described in each is discharged;
Diaphragm sell, for described mixed waste liquor is carried out electrolysis treatment, described diaphragm sell comprises groove body, is also provided with ion diaphragm in described groove body, and groove body is divided into inside groove and outer groove by described ion diaphragm; Described inside groove is provided with negative plate, described outer groove is provided with positive plate;
Purifying groove, the fluid inlet of described purifying groove is connected with described outer groove;
Cathode regenerative liquid storage tanks, for storing strong base solution, the liquid outlet of described cathode regenerative liquid storage tanks is connected with cathode resin groove described in each respectively, and the fluid inlet of described cathode regenerative 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 anode resin groove described in each 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 groove respectively;
The fluid inlet of described reuse water storage tanks is connected with each cathode resin groove described respectively; The liquid outlet of reuse water holding tank is also connected with described cathode resin groove, described anode resin groove, described inside groove respectively;
The fluid inlet of described regeneration and back washing waste water collection tank is connected with each anode resin groove, each cathode resin groove respectively, and liquid outlet is connected with the described outer groove of diaphragm sell;
The described controlled connection being connected and being and be equipped with pipeline valve, has liquid level difference or is provided with pump between described groove.
6. a kind of chromic acid Waste Water Treatment according to claim 5, it is characterised in that, also comprise heating thickener, 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.
7. a kind of chromic acid Waste Water Treatment according to claim 6, it is characterised in that,
Described groove body is plastic groove, and described ion diaphragm is N number of boccaro cylinder, N >=1, the boccaro cylinder that described boccaro cylinder to be volume be 60��100L, water-permeable are 0.01��0.05ml/d days, sintering temperature is 1000��1200 DEG C;
The current density for electrolysis loaded between described positive plate and negative plate is 2��5A/d, voltage is 15��30V;
Described negative plate is cylindrical stainless steel cylinder, and described positive plate is chromium plating stereotype;
Described cylindrical stainless steel cylinder is covered with the aperture radially running through barrel wall.
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| 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 |
| CN104355365B (en) * | 2014-10-31 | 2016-08-24 | 武汉钢铁(集团)公司 | The processing method of chromate waste water zero release of pollutant |
| 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 |
| CN105463555A (en) * | 2015-12-09 | 2016-04-06 | 无锡市晨源建筑器材有限公司 | Electroplating bath equipment with electroplating effluent treatment device |
| CN106630009B (en) * | 2017-01-19 | 2019-10-22 | 沈阳艾柏瑞环境科技有限公司 | High-concentration ammonia nitrogenous wastewater ion exchange-electrolytic regeneration treatment process device and method |
| CN106966469A (en) * | 2017-04-10 | 2017-07-21 | 中国铝业股份有限公司 | A kind of processing method of containing sulfate radicals waste water |
| CN107840496A (en) * | 2017-11-22 | 2018-03-27 | 沈阳艾柏瑞环境科技有限公司 | A kind of biochemical tailrace advanced handling process device and method of percolate |
| CN110078282A (en) * | 2019-04-19 | 2019-08-02 | 苏州希图环保科技有限公司 | A kind of heavy metal waste water treatment process |
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