CN109502824A - A kind of anolyte recovery and processing system and method - Google Patents
A kind of anolyte recovery and processing system and method Download PDFInfo
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- CN109502824A CN109502824A CN201811602152.3A CN201811602152A CN109502824A CN 109502824 A CN109502824 A CN 109502824A CN 201811602152 A CN201811602152 A CN 201811602152A CN 109502824 A CN109502824 A CN 109502824A
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- separation equipment
- water
- anolyte
- permeate
- concentrator
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- 238000011084 recovery Methods 0.000 title claims abstract description 30
- 238000012545 processing Methods 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 94
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 75
- 239000012466 permeate Substances 0.000 claims abstract description 47
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 79
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 38
- 239000012141 concentrate Substances 0.000 claims description 33
- 238000010612 desalination reaction Methods 0.000 claims description 26
- 239000002253 acid Substances 0.000 claims description 23
- 238000002386 leaching Methods 0.000 claims description 16
- 229910001453 nickel ion Inorganic materials 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 15
- 238000004070 electrodeposition Methods 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 abstract description 16
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 229910000029 sodium carbonate Inorganic materials 0.000 abstract description 9
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 229910052759 nickel Inorganic materials 0.000 description 10
- 238000009854 hydrometallurgy Methods 0.000 description 7
- 229910000008 nickel(II) carbonate Inorganic materials 0.000 description 7
- ZULUUIKRFGGGTL-UHFFFAOYSA-L nickel(ii) carbonate Chemical compound [Ni+2].[O-]C([O-])=O ZULUUIKRFGGGTL-UHFFFAOYSA-L 0.000 description 6
- 239000004615 ingredient Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 238000010790 dilution Methods 0.000 description 4
- 239000012895 dilution Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
Abstract
The present invention relates to a kind of anolyte recovery and processing system and method, system includes the first separation equipment, the second separation equipment, sour concentrator and water-adding system；Sour concentrator is connected to the first water outlet of the first water outlet of the first separation equipment and the second separation equipment respectively；Water-adding system is connected to the water inlet of the water inlet of the first separation equipment and the second separation equipment respectively；First seperation film is set in the first separation equipment, for carrying out first time separation to anolyte；Second seperation film is set in the second separation equipment, is separated for carrying out second to anolyte；The water inlet of second separation equipment is connected to the second water outlet of the first separation equipment；Sour concentrator is used for the second permeate collecting the first permeate separated in the first separation equipment and separating in the second separation equipment, and the first permeate and the second permeate are concentrated；Using the above scheme, sodium carbonate use can be reduced, production cost is reduced, reduces disposal of pollutants.
Description
Technical field
The invention belongs to metallurgy and galvanic anode liquid recovery technology fields；More particularly to a kind of anolyte recovery and processing system
And method.
Background technique
In the production of the industries metal recovery such as hydrometallurgy and plating, a large amount of anolytes can be generated in electrodeposition process section, all
Reuse will cause the imbalance in production system；By taking nickel fibers as an example, part reuse is mainly used at present, and another part uses
Na2CO3Neutralizing acid and production NiCO3Precipitating；PH of the sodium carbonate reuse to adjust cell liquid, the supernatant discharge after precipitating
To sewage treatment plant；This method need to consume a large amount of Na2CO3To the sulfuric acid in neutralization system, to reach acid balance in electrolytic cell,
It produces 1 ton of nickel product and consumes 1.6 tons of Na2CO3；It generates simultaneously largely containing the high-salt wastewater of heavy metal, unfavorable shadow is caused to environment
It rings.
Summary of the invention
The present invention devises a kind of anolyte recovery and processing system and method, and which solve the recovery processings of existing anolyte to deposit
The problem of pollution, wasting.
In order to solve above-mentioned technical problem, present invention employs following scheme:
A kind of anolyte recovery and processing system, including the first separation equipment, the second separation equipment, sour concentrator and plus water system
System；Sour concentrator is connected to the first water outlet of the first water outlet of the first separation equipment and the second separation equipment respectively；Add
Water system is connected to the water inlet of the water inlet of the first separation equipment and the second separation equipment respectively；It is equipped in first separation equipment
First seperation film, the first seperation film are used to carry out first time separation to the anolyte in the first separation equipment；Second separation equipment
It is inside equipped with the second seperation film, the second seperation film is used to carry out second to the anolyte in the second separation equipment to separate；Second point
Water inlet from equipment is connected to the second water outlet of the first separation equipment；Sour concentrator is for collecting in the first separation equipment
The first permeate separated and the second permeate separated in the second separation equipment, and to the first permeate and second
Permeate is concentrated.
Further, the first water outlet of sour concentrator is connected to by circulation loop with water-adding system；Sour concentrator
The desalination water after concentration is delivered to water-adding system by circulation loop.
It further, further include leaching system；First water outlet of sour concentrator passes through leach circuit and leaching system
Connection；Acid solution after concentration is delivered to leaching system by leach circuit by sour concentrator.
It further, further include Winning cell；Winning cell is connected to the second water outlet of the second separation equipment；Winning cell is used for
Collect the second concentrate separated in the second separation equipment.
Further, anolyte includes nickel ion and sulfuric acid；First seperation film and the second seperation film are used to separation anode
Nickel ion and sulfuric acid in liquid, to obtain permeate and concentrate.
Correspondingly, the present invention also provides a kind of anolyte recovery and treatment methods, applied to sun described in the claims 1
Pole liquid recovery and processing system；It is further comprising the steps of:
S1: anolyte is diluted with water 1 times by water-adding system first；
S2: the anolyte after first time is diluted is separated by the first separation equipment, is penetrated with obtaining the first concentrate and first
Liquid；It include nickel ion and sulfuric acid in first concentrate；It include sulfuric acid in first permeate；
S3: the first concentrate is diluted with water 1 times by water-adding system；
S4: the anolyte after second is diluted is separated by the second separation equipment, to obtain the second permeate；Second permeate
In include sulfuric acid；
S5: the first permeate and the second permeate are collected to sour concentrator and are concentrated, to obtain desalination water and the concentrated sulfuric acid.
Further, in S1 step and S4 step, water-adding system is diluted by addition desalination water or is removed by addition
Salt water is diluted；Desalination water is the desalination water after sour concentrator concentration.
Further, in S2 step, the first concentrate and the first permeate volume are equal；In S4 step, in S4 step, sun
Pole liquid further includes obtaining the second concentrate after being separated by the second separation equipment；Second concentrate is directly drained to Winning cell and returns
With.
Further, the first separation equipment highest operating pressure is 4.1MPa, and the first separation equipment maximum operating temperature is
70°C；And/or second separation equipment highest operating pressure be 4.1MPa, the second separation equipment maximum operating temperature be 70 °C.
Further, in S5 step, the mixed liquor of the first permeate and the second permeate is concentrated into 4 times by sour concentrator
More than, to obtain the desalination water of the concentrated sulfuric acid and not more than 1.5 times volumes less than 0.5 times of volume；Desalination water is through through circulation loop
It is delivered to water-adding system, the concentrated sulfuric acid is delivered to leaching system through leach circuit.
The anolyte recovery and processing system and method have the advantages that
The first, scheme provided by the invention, can by anolyte that hydrometallurgy electrolytic cell generates sulfuric acid and metallic nickel from
Son efficiently separates, and neutralizes instead of sodium carbonate in the prior art, reduces sodium carbonate usage amount, can reduce production cost；
The second, the scheme that provides of invention, can be by the sulfuric acid and metallic nickel ions in anolyte that hydrometallurgy electrolytic cell generates
It efficiently separates, the pH value of electrolytic cell tank liquor is adjusted by concentrate reuse, reaches and uses no or little nickelous carbonate, reduce nickelous carbonate
Output, while reducing the discharge of supernatant effluent when nickelous carbonate production；
The scheme that third, invention provide, can be by the sulfuric acid and metallic nickel ions in anolyte that hydrometallurgy electrolytic cell generates
It efficiently separates, the concentrated rear reuse of the dilute sulfuric acid in permeate to leaching section, desalination water reuse, effectively save resource is reduced
Disposal of pollutants.
Detailed description of the invention
A kind of Fig. 1: anolyte recovery and processing system schematic diagram of the present invention；
A kind of Fig. 2: anolyte recovery and treatment method flow chart of the present invention.
Specific embodiment
With reference to the accompanying drawing, the present invention will be further described:
Fig. 1 shows a kind of anolyte recovery and processing system, including separation equipment, sour concentrator and water-adding system；Separation
Seperation film is equipped in equipment, seperation film is nanofiltration membrane, and for filtering nickel ion in anolyte, sulfuric acid can pass through seperation film；Point
It include the first separation equipment and the second separation equipment from equipment；Seperation film includes the first seperation film and the second seperation film；Acid concentration
Equipment is connected to the first water outlet of the first water outlet of the first separation equipment and the second separation equipment respectively；Water-adding system difference
It is connected to the water inlet of the water inlet of the first separation equipment and the second separation equipment；First seperation film is set to the first separation equipment
Interior, the first seperation film is used to carry out first time separation to the anolyte in the first separation equipment；Second seperation film is set to second
In separation equipment, the second seperation film is used to carry out second to the anolyte in the second separation equipment to separate；Second separation equipment
Water inlet be connected to the second water outlet of the first separation equipment；First separation equipment is for collecting anolyte and carrying out adding water dilute
It releases；Second separation equipment is for collecting filtered first concentrate of the first separation equipment and being diluted with water；Acid concentration is set
It is saturating to be ready for use on second for collecting the first permeate separated in the first separation equipment and separating in the second separation equipment
Liquid is crossed, and the first permeate and the second permeate are concentrated, to obtain desalination water and acid solution；Using the above scheme, energy
Enough nickel and acid by anolyte separates, and carries out recycling and Treatment for Reuse, and the nickeliferous concentrate acid content reduction isolated can
Direct reuse, reuse after the acid solution isolated is concentrated；And after anolyte is separated, reuse is concentrated, total volume is no more than original
Volume 150%, meets manufacturing technique requirent, reduces Na in entire smelting process2CO3Dosage reduces production cost, while also reducing
Waste water outlet.
Preferably, in conjunction with above scheme, as shown in Figure 1, the first water outlet of sour concentrator is by following in the present embodiment
Loop back path is connected to water-adding system；Desalination water after concentration is delivered to water-adding system by circulation loop by sour concentrator, with
It is reused, to avoid wasting.
Preferably, in conjunction with above scheme, as shown in Figure 1, anolyte recovery and processing system further includes leaching in the present embodiment
System；First water outlet of sour concentrator is connected to by leach circuit with leaching system；Sour concentrator passes through leach circuit
Acid solution after concentration is delivered to leaching system, to carry out reuse, to avoid pollution.
Preferably, in conjunction with above scheme, as shown in Figure 1, anolyte recovery and processing system further includes electrodeposition in the present embodiment
Slot；Winning cell is connected to the second water outlet of the second separation equipment；Winning cell is separated for collecting in the second separation equipment
The second concentrate, to carry out reuse.
Preferably, in conjunction with above scheme, in the present embodiment, anolyte includes nickel ion and sulfuric acid；First seperation film and
Two seperation films are used to nickel ion and sulfuric acid in separation anolyte, to obtain permeate and concentrate.
Correspondingly, in conjunction with above scheme, as shown in Fig. 2, the present invention also provides a kind of anolyte recovery and treatment method, application
In anolyte recovery and processing system described above；It is further comprising the steps of:
S1: anolyte is diluted with water 1 times by water-adding system first；
S2: the anolyte after first time is diluted is separated by the first separation equipment, is penetrated with obtaining the first concentrate and first
Liquid；It include nickel ion and sulfuric acid in first concentrate；It include sulfuric acid in first permeate；
S3: the first concentrate is added water into 1 times of dilution by water-adding system；
S4: the anolyte after second is diluted is separated by the second separation equipment, to obtain the second permeate；Second permeate
In include sulfuric acid；
S5: the first permeate and the second permeate are collected to sour concentrator and are concentrated, to obtain desalination water and the concentrated sulfuric acid.
Preferably, in conjunction with above scheme, in the present embodiment, in S1 step and S4 step, water-adding system passes through addition desalination
Water is diluted or is diluted by adding demineralized water；Desalination water is the desalination water after sour concentrator concentration.
Preferably, in conjunction with above scheme, in the present embodiment, in S2 step, the first concentrate and the first permeate volume phase
Deng；In S4 step, the anolyte after second is diluted also obtains the second concentrate by the separation of the second separation equipment；Described
Two concentrates are drained to Winning cell reuse.
Preferably, in conjunction with above scheme, in the present embodiment, the first separation equipment highest operating pressure is 4.1MPa, first
Separation equipment maximum operating temperature is 70 °C；And/or second separation equipment highest operating pressure be 4.1MPa, second separation set
Standby maximum operating temperature is 70 °C.
Preferably, in conjunction with above scheme, in the present embodiment, in S5 step, sour concentrator is by the first permeate and second
The mixed liquor of permeate is concentrated into 4 times or more, with obtain less than the concentrated sulfuric acid of 0.5 times of volume and not more than 1.5 times of volumes it is light
Change water；For desalination water through being delivered to water-adding system through circulation loop, the concentrated sulfuric acid is delivered to leaching system through leach circuit.
Preferably, in conjunction with above scheme, in the present embodiment, the nickeliferous 40g/L of anolyte, sulfuric acid 20g/L；Concrete operations are such as
Under:
Firstly, nickeliferous 40g/L, sulfuric acid 20g/L or so anolyte are diluted with water 1 times, material liquid component becomes nickel 20g/L, sulfuric acid
10g/L or so；First operation uses demineralized water, after water-adding system puts into operation, using the desalination water after acid concentration；Anode after dilution
Liquid makes sulfuric acid through the first seperation film by the first separation equipment, and nickel ion cannot penetrate；It is concentrated into former anode liquid product, this
When the first concentrate ingredient for generating be nickel 40g/L, sulfuric acid 10g/L or so, the first permeate ingredient is sulfuric acid 10g/L or so,
Nickel is less than 3g/L；First concentrate and the first permeate volume are equal；The operation of first separation equipment uses circulation pattern, highest fortune
Row pressure 4.1MPa, 70 °C of maximum operating temperature；
Then, the first concentrate is continued to dilute 1 times with desalination water, desalination water insufficient section is supplemented using demineralized water, after dilution
Ingredient becomes nickel 20g/L, sulfuric acid 5g/L or so, is separated by the second separation equipment, makes sulfuric acid through the second seperation film, nickel
Ion cannot penetrate, and be concentrated into original volume, at this moment generate the second concentrate, and ingredient is nickel 40g/L, sulfuric acid 5g/L or so, meet
Produce reuse index direct reuse；Second permeate ingredient is sulfur acid 5g/L or so, and nickel is less than 3g/L；Second separation equipment fortune
It goes and uses circulation pattern, highest operating pressure 4.1MPa, 70 °C of maximum operating temperature；
Finally, the first permeate and the second permeate are mixed, mixed liquor is sulfur acid 7.5g/L, and nickel is less than 3g/L, and volume is
2 times of former anode liquid product, mixed liquor is concentrated using sour concentrator, and sour concentrator uses electric drive, and it is mixed to will transmit through liquid
It closes liquid and is concentrated 4 times or more, generate concentrated acid (sulfuric acid concentration 30g/L) reuse less than 0.5 times of volume to leaching system workshop section, generate
The desalination solution reuse anolyte of not more than 1.5 times volumes and the dilution of the first concentrate use, total after handling whole processing technology
Volume is no more than the 150% of former anolyte, and whole processing technology does not generate outer draining.
Anolyte recovery and processing system provided by the invention and method have the advantages that
The first, scheme provided by the invention, can by anolyte that hydrometallurgy electrolytic cell generates sulfuric acid and metallic nickel from
Son efficiently separates, and neutralizes instead of sodium carbonate in the prior art, reduces sodium carbonate usage amount, can reduce production cost；
The second, the scheme that provides of invention, can be by the sulfuric acid and metallic nickel ions in anolyte that hydrometallurgy electrolytic cell generates
It efficiently separates, the pH value of electrolytic cell tank liquor is adjusted by concentrate reuse, reaches and uses no or little nickelous carbonate, reduce nickelous carbonate
Output, while reducing the discharge of supernatant effluent when nickelous carbonate production；
The scheme that third, invention provide, can be by the sulfuric acid and metallic nickel ions in anolyte that hydrometallurgy electrolytic cell generates
It efficiently separates, the concentrated rear reuse of the dilute sulfuric acid in permeate to leaching section, desalination water reuse, effectively save resource is reduced
Disposal of pollutants.
Above in conjunction with attached drawing, an exemplary description of the invention, it is clear that realization of the invention is not by aforesaid way
Limitation, as long as use the inventive concept and technical scheme of the present invention carry out various improvement, or it is not improved will be of the invention
Conception and technical scheme directly apply to other occasions, be within the scope of the invention.
Claims (10)
1. a kind of anolyte recovery and processing system, which is characterized in that including the first separation equipment, the second separation equipment, acid concentration
Equipment and water-adding system；The acid concentrator respectively with the first water outlet of first separation equipment and second point described
The first water outlet connection from equipment；The water-adding system respectively with the water inlet of first separation equipment and second point described
Water inlet connection from equipment；The first seperation film is equipped in first separation equipment, first seperation film is used for described
Anolyte in first separation equipment carries out first time separation；It is equipped with the second seperation film in second separation equipment, described the
Two seperation films are used to carry out second to the anolyte in second separation equipment to separate；The water inlet of second separation equipment
Mouth is connected to the second water outlet of first separation equipment；The acid concentrator is for collecting in first separation equipment
The first permeate separated and the second permeate separated in second separation equipment, and penetrated to described first
Liquid and second permeate are concentrated.
2. anolyte recovery and processing system according to claim 1, which is characterized in that the first of the acid concentrator goes out
The mouth of a river is connected to by circulation loop with the water-adding system；The acid concentrator will be light after concentration by the circulation loop
Change water and is delivered to the water-adding system.
3. anolyte recovery and processing system according to claim 1, which is characterized in that further include leaching system；The acid
First water outlet of concentrator is connected to by leach circuit with the leaching system；The acid concentrator passes through the leaching
Acid solution after concentration is delivered to the leaching system by circuit.
4. anolyte recovery and processing system according to claim 1, which is characterized in that further include Winning cell；The electrodeposition
Slot is connected to the second water outlet of second separation equipment；The Winning cell separates in second separation equipment for collecting
The second concentrate out.
5. anolyte recovery and processing system according to any one of claims 1 to 4, which is characterized in that the anolyte packet
Include nickel ion and sulfuric acid；First seperation film and second seperation film be used to separate nickel ion in the anolyte and
Sulfuric acid, to obtain permeate and concentrate.
6. a kind of anolyte recovery and treatment method, which is characterized in that at anolyte recycling described in the claims 1
Reason system；It is further comprising the steps of:
S1: anolyte is diluted with water 1 times by water-adding system first；
S2: the anolyte after first time is diluted is separated by the first separation equipment, is penetrated with obtaining the first concentrate and first
Liquid；It include nickel ion and sulfuric acid in first concentrate；It include sulfuric acid in first permeate；
S3: first concentrate is diluted with water 1 times by water-adding system；
S4: the anolyte after second is diluted is separated by the second separation equipment, to obtain the second permeate；Described second thoroughly
Crossing includes sulfuric acid in liquid；
S5: first permeate and second permeate are collected to sour concentrator and is concentrated, to obtain desalination water
And the concentrated sulfuric acid.
7. anolyte recovery and treatment method according to claim 6, which is characterized in that the S1 step and the S4 step
In, the water-adding system is diluted by addition desalination water or is diluted by adding demineralized water；The desalination water is institute
Desalination water after stating sour concentrator concentration.
8. anolyte recovery and treatment method according to claim 6, which is characterized in that in the S2 step, described first
Concentrate and the first permeate volume are equal；In the S4 step, the anolyte passes through second separation equipment point
It further include obtaining the second concentrate from after；Second concentrate is directly drained to Winning cell reuse.
9. anolyte recovery and treatment method according to claim 6, which is characterized in that the first separation equipment highest fortune
Row pressure is 4.1MPa, and the first separation equipment maximum operating temperature is 70 °C；And/or the second separation equipment highest
Operating pressure is 4.1MPa, and the second separation equipment maximum operating temperature is 70 °C.
10. anolyte recovery and treatment method according to claim 6, which is characterized in that in the S5 step, the acid is dense
The mixed liquor of first permeate and second permeate is concentrated into 4 times or more by contracting equipment, is less than 0.5 times of body to obtain
The desalination water of the long-pending concentrated sulfuric acid and not more than 1.5 times volumes；The desalination water is delivered to the water-adding system, institute through circulation loop
It states the concentrated sulfuric acid and is delivered to the leaching system through leach circuit.
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| CN201811602152.3A CN109502824A (en) | 2018-12-26 | 2018-12-26 | A kind of anolyte recovery and processing system and method |
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| CN201811602152.3A CN109502824A (en) | 2018-12-26 | 2018-12-26 | A kind of anolyte recovery and processing system and method |
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| CN106241960A (en) * | 2016-08-31 | 2016-12-21 | 湖南凯天重金属污染治理工程有限公司 | A kind of processing method of acid heavy metal wastewater |
| CN209456209U (en) * | 2018-12-26 | 2019-10-01 | 北京大井易通科技发展有限公司 | A kind of anolyte recovery and processing system |
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