CN112063844A - Method for treating electroplating sludge and electroplating waste liquid - Google Patents
Method for treating electroplating sludge and electroplating waste liquid Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
- C22B7/007—Wet processes by acid leaching
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0065—Leaching or slurrying
- C22B15/0067—Leaching or slurrying with acids or salts thereof
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- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0084—Treating solutions
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0084—Treating solutions
- C22B15/0089—Treating solutions by chemical methods
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- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
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- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
- C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/38—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
- C22B3/384—Pentavalent phosphorus oxyacids, esters thereof
- C22B3/3846—Phosphoric acid, e.g. (O)P(OH)3
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/40—Mixtures
- C22B3/402—Mixtures of acyclic or carbocyclic compounds of different types
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Abstract
The invention provides a method for treating electroplating sludge and electroplating waste liquid, which belongs to the field of sludge wastewater treatment and comprises the following steps: (1) mixing and soaking electroplating sludge and electroplating waste liquid, adding hydrogen peroxide solution for oxidation reaction, cooling and filtering, and filtering to obtain filtrate A; (2) extracting the leaching solution A by using a copper extractant to obtain an extraction solution B and a raffinate C, and extracting the raffinate C by using a nickel extractant to obtain an extraction solution D; (3) carrying out back extraction and delamination on the extract B by using an acid solution, preheating the obtained back extract, and carrying out evaporative crystallization to obtain copper salt crystals; (4) and (4) carrying out back extraction and delamination on the extract liquid D by using an acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain the nickel salt crystal. The method for treating the electroplating sludge and the electroplating waste liquid is simple to operate, can save a large amount of medicament cost, and has high purity of the recovered heavy metal salt.
Description
Technical Field
The invention relates to a method for treating electroplating sludge and waste liquid, in particular to a method for treating electroplating sludge and electroplating waste liquid.
Background
The electroplating sludge is solid waste generated when electroplating wastewater or waste liquid is treated by electroplating enterprises, and contains a large amount of heavy metal elements, such as copper, iron, nickel, chromium and other heavy metals. Common disposal methods for electroplating sludge include immobilization treatment, thermochemical treatment, hydrometallurgical treatment, etc., but these methods extract a small amount of heavy metals and have low utility value.
(1) The solidification and stabilization technology of the electroplating sludge is to add common curing agents such as cement, asphalt, glass, water glass and the like, mix the common curing agents with the sludge and solidify the common curing agents and the sludge, so that harmful substances in the sludge are sealed in a solidified body and are not leached out, and the purpose of pollution relief is achieved.
(2) Thermochemical treatment techniques (such as incineration, ion arc, microwave, and the like) decompose waste at high temperatures to reduce the toxicity of some highly toxic components, achieve rapid and significant volume reduction, and utilize useful components of the waste.
(3) Hydrometallurgy refers to soaking and extraction by using acid and alkali. The acid leaching method is the most widely used method in the solid waste leaching method, and the specific acid adopted for leaching depends on the properties of the solid waste. Sulfuric acid is the most effective leaching agent for the treatment of electroplating, casting, smelting and other industrial wastes, and is widely used due to its characteristics of low price, low volatility, difficult decomposition and the like. Although technologies for extracting metals by ammonia leaching have a certain history, the treatment of electroplating sludge by ammonia leaching is relatively less than that by acid leaching. The ammonia leaching method generally adopts an ammonia water solution as a leaching agent because the ammonia water has the advantages of moderate alkalinity, convenient use, recyclability and the like.
When electroplating sludge is treated by acid leaching or ammonia leaching, the total recovery rate of valuable metals and the difficulty of separation from other impurities are mainly controlled by the leaching rate of the valuable metals and the selectivity of leaching solution to the valuable metals and the impurities in the leaching process. The acid leaching method is mainly characterized in that the leaching effect on valuable metals such as copper, zinc, nickel and the like is good, but the selectivity on impurities is low, particularly the selectivity on impurities such as chromium, iron and the like is poor; the ammonia leaching method has high selectivity on impurities such as chromium, iron and the like, but has low leaching rate on copper, zinc, nickel and the like.
The immobilization treatment method does not recover useful resources, the thermochemical treatment method can effectively recover resources, but the energy consumption is high, and the hydrometallurgy method can also recover resources but consumes a large amount of acid and alkali.
The electroplating sludge is obtained by neutralizing and coagulating electroplating wastewater or waste liquid, common coagulant comprises PAC, PAM, ferric salt and ferrous salt, and sludge obtained by precipitation contains Cu (OH)2、Ni(OH)2、Fe(OH)2And Fe (OH)3Etc., which are soluble under acidic conditions. The plating waste liquid is generally acidic and contains Cu2+、Ni2+、Fe2+And Fe3+The electroplating sludge can be dissolved, and if the cooperative treatment can be realized, the cost of a large amount of agents can be saved, and certain benefits can be created.
Disclosure of Invention
Based on the defects in the prior art, the invention aims to provide a method for treating electroplating sludge and electroplating waste liquid. The method utilizes the synergistic mixing leaching of the electroplating waste liquid and the electroplating sludge, and then the subsequent high-temperature oxidation method, extraction method and crystallization method are used for treatment, and finally the solid-liquid treatment of the waste and the recovery of metal salt are realized.
In order to achieve the purpose, the invention adopts the technical scheme that:
a method for treating electroplating sludge and electroplating waste liquid comprises the following steps:
(1) mixing and soaking electroplating sludge and electroplating waste liquid, adding hydrogen peroxide solution for oxidation reaction, cooling and filtering, and filtering to obtain filtrate A;
(2) extracting the leaching solution A by using a copper extractant to obtain an extraction solution B and a raffinate C, and extracting the raffinate C by using a nickel extractant to obtain an extraction solution D;
(3) carrying out back extraction on the extract B by using an acid solution, preheating the obtained back-extraction liquid, and carrying out evaporative crystallization to obtain copper salt crystals;
(4) and (4) carrying out back extraction on the extraction liquid D by using an acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain the nickel salt crystal.
In the method for treating the electroplating sludge and the electroplating waste liquid, the acid in the electroplating waste liquid is used for dissolving useful metal ions in the electroplating sludge, a hydrogen peroxide oxidation method is adopted for removing iron ions, a step-by-step extraction method is adopted for extracting copper and nickel, and after back extraction, metal salt solution is evaporated, concentrated, crystallized and separated to form metal salt crystals for recycling. The adopted technical process fully utilizes the electroplating waste liquid, saves the cost of acid for soaking, adopts extraction and evaporative crystallization to carry out concentration crystallization on the metal salt solution, obtains copper salt crystals and nickel salt crystals with high purity and crystallinity, and effectively recovers heavy metal copper and nickel salt while saving a large amount of medicament cost for treating electroplating sludge and waste liquid.
Preferably, in the step (1), the mass ratio of the electroplating sludge to the electroplating waste liquid is 1: 4-5, and the soaking time is 12-24 hours. The electroplating sludge and the electroplating waste liquid can be fully mixed in the mass proportion and the reaction time, and the local dissolution and re-precipitation of the electroplating sludge can be effectively avoided.
Preferably, in the step (1), the concentration of hydrogen peroxide in a hydrogen peroxide solution is 9-11 mol/L, the mass of the hydrogen peroxide solution accounts for 4-5% of the mass of the electroplating sludge, the temperature of the oxidation reaction is 250-260 ℃, the pressure is 3.5-4.0 MPa, and the time is 1-2 h. The hydrogen peroxide has strong oxidizing property within the limited range, can effectively and completely convert iron ions in the electroplating sludge and the waste liquid into ferric oxide precipitate, does not introduce new metal ions after decomposition of the hydrogen peroxide, and can effectively separate ferric salt when ensuring the purity of subsequent copper and nickel salt recovery.
Preferably, in step (2), the copper extractant comprises nonylsalicylaldoxime, TXIB ester and kerosene; the mass ratio of the nonyl salicylaldoxime to the TXIB ester to the kerosene is nonyl salicylaldoxime: TXIB esters: kerosene is 4-6: 2-4: 2-5; the nickel extracting agent is 2-ethylhexyl phosphate monoester. The two extracting agents are selected to respectively extract the copper ions and the nickel ions, so that the extraction rate can reach more than 99 percent.
Preferably, the volume ratio of the leaching solution A to the copper extractant is 0.5-2: 1, and the standing and layering time is 5-10 min; the volume ratio of the raffinate C to the nickel extracting agent is 0.5-2: 1, and the standing and layering time is 5-10 min.
Preferably, in the step (3) and the step (4), the acid solution used for back extraction of the extract B and the extract E is at least one of a sulfuric acid solution and a hydrochloric acid solution, the concentration of the sulfuric acid solution is 6-9 mol/L, and the concentration of hydrogen chloride in the hydrochloric acid solution is 3-5 mol/L. More preferably, in the step (3) and the step (4), both the acid solution used for back extraction are hydrochloric acid solutions, and the concentration of hydrogen chloride in the hydrochloric acid solutions is 3-5 mol/L. In the back extraction process, the acid solution has higher affinity to metal ions, and the metal salt in the organic phase extraction liquid can be back extracted into the aqueous phase acid solution, wherein the back extraction effect of the hydrochloric acid solution is better.
Preferably, in the step (3), the molar ratio of the copper ions in the extract B to the hydrogen ions in the acid solution is 1: 2.2-2.5, and the standing and layering time is 30-40 min.
Preferably, in the step (4), the molar ratio of the nickel ions in the extraction liquid D to the hydrogen ions in the acid solution is 1: 2.2-2.5, and the standing and layering time is 30-40 min.
Preferably, in the step (3) and the step (4), the preheating temperature is 80-90 ℃, the evaporation crystallization temperature is 90-110 ℃, and the pressure is-0.01 MPa.
Preferably, the evaporative crystallization process is performed by using a steam mechanical recompression system, and the steam mechanical recompression system comprises a preheater, a heater, a gas-liquid separator, a steam compressor and a vacuum pump. By adopting the system to evaporate and crystallize the solution to be treated, the generated steam can be recycled, latent heat can be recovered, and only a heat source needs to be supplemented for the first time, so that the heat utilization efficiency is improved.
The method has the beneficial effects that the electroplating waste liquid and the electroplating waste liquid are cooperatively treated to dissolve useful metal ions in the electroplating sludge, the iron ions in the leachate are removed by adopting a high-temperature oxidation method, copper ions and nickel ions are extracted by adopting an extraction method, and after back extraction, a metal salt solution is evaporated, concentrated, crystallized and separated to form a metal salt crystal for recycling. The adopted technical process steps are simple to operate, and the technical parameters can be regulated and controlled according to the actual conditions; the acid in the electroplating waste liquid can replace the acid for soaking, so that a large amount of medicament cost is saved; the extractant in the extraction process can be recycled, the metal salt solution can be concentrated and crystallized by adopting evaporative crystallization, and the purity of the crystallized heavy metal nickel and copper salt is high (the crystallization content is more than 95%).
Drawings
FIG. 1 is a flow chart of the treatment method of electroplating sludge and electroplating waste liquid according to the present invention.
Detailed Description
In order to better illustrate the objects, technical solutions and advantages of the present invention, the present invention will be further described with reference to specific examples and comparative examples, which are intended to be understood in detail, but not intended to limit the invention. All other embodiments obtained by a person skilled in the art without making any inventive step are within the scope of protection of the present invention. The experimental reagents and instruments designed for the practice of the present invention and the comparative examples are common reagents and instruments unless otherwise specified.
The copper extractant used in the examples and comparative examples of the present invention is an N-902 copper extractant produced by shanghai leiya chemical company ltd, and the nickel extractant used is a P-507 nickel extractant produced by shanghai leiya chemical company ltd.
Example 1
The flow of the treatment method of the electroplating sludge and the electroplating waste liquid is shown in figure 1, and the treatment method comprises the following steps:
(1) mixing, stirring and soaking the electroplating sludge and the electroplating waste liquid for 18 hours, adding 10mol/L hydrogen peroxide solution for mixing, carrying out oxidation reaction, cooling, filtering and precipitating to obtain filtrate A; the mass ratio of the electroplating sludge to the electroplating waste liquid is 1: 4.5; the content of the hydrogen peroxide solution accounts for 4.5% of the mass of the electroplating sludge, the temperature of the oxidation reaction is 255 ℃, the pressure is 4.0MPa, and the time is 1.5 h;
(2) extracting the leaching solution A by using a copper extractant to obtain an extraction solution B and a raffinate C, and extracting and layering the raffinate C by using a nickel extractant to obtain an extraction solution D; the volume ratio of the leaching solution A to the copper extractant is 1.2:1, and the standing and layering time is 8 min; the volume ratio of the raffinate C to the nickel extractant is 1.2:1, and the standing and layering time is 8 min;
(3) carrying out back extraction on the extract B by using a 4mol/L hydrochloric acid solution, preheating the obtained back-extraction solution, and carrying out evaporative crystallization to obtain copper salt crystals; the molar ratio of copper ions in the extract B to hydrogen ions in the acid solution is 1:2.4, and the standing and layering time is 35 min;
(4) and (3) carrying out back extraction on the extract liquid D by using a 4mol/L hydrochloric acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain the nickel salt crystal. The molar ratio of nickel ions in the extraction liquid D to hydrogen ions in the acid solution is 1:2.4, and the standing and layering time is 35 min.
Example 2
The treatment method of the electroplating sludge and the electroplating waste liquid comprises the following steps:
(1) mixing, stirring and soaking the electroplating sludge and the electroplating waste liquid for 24 hours, adding 9mol/L hydrogen peroxide solution for mixing, carrying out oxidation reaction, cooling, filtering and precipitating to obtain filtrate A; the mass ratio of the electroplating sludge to the electroplating waste liquid is 1: 4; the content of the hydrogen peroxide solution accounts for 4% of the mass of the electroplating sludge, the temperature of the oxidation reaction is 255 ℃, the pressure is 4.0MPa, and the time is 2 h;
(2) extracting the leaching solution A by using a copper extractant to obtain an extraction solution B and a raffinate C, and extracting and layering the raffinate C by using a nickel extractant to obtain an extraction solution D; the volume ratio of the leaching solution A to the copper extractant is 1.2:1, and the standing and layering time is 8 min; the volume ratio of the raffinate C to the nickel extractant is 1.2:1, and the standing and layering time is 8 min;
(3) carrying out back extraction on the extract B by using a 5mol/L hydrochloric acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain copper salt crystals; the molar ratio of copper ions in the extract B to hydrogen ions in the acid solution is 1:2.2, and the standing and layering time is 40 min;
(4) and (3) carrying out back extraction on the extract liquid D by using a 3mol/L hydrochloric acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain the nickel salt crystal. The molar ratio of nickel ions in the extraction liquid D to hydrogen ions in the acid solution is 1:2.5, and the standing and layering time is 30 min.
Example 3
The treatment method of the electroplating sludge and the electroplating waste liquid comprises the following steps:
(1) mixing, stirring and soaking the electroplating sludge and the electroplating waste liquid for 15 hours, adding 9mol/L hydrogen peroxide solution for mixing, carrying out oxidation reaction, cooling, filtering and precipitating to obtain filtrate A; the mass ratio of the electroplating sludge to the electroplating waste liquid is 1: 5; the content of the hydrogen peroxide solution accounts for 4% of the mass of the electroplating sludge, the temperature of the oxidation reaction is 255 ℃, the pressure is 4.0MPa, and the time is 1 h;
(2) extracting the leaching solution A by using a copper extractant to obtain an extraction solution B and a raffinate C, and extracting and layering the raffinate C by using a nickel extractant to obtain an extraction solution D; the volume ratio of the leaching solution A to the copper extractant is 1.2:1, and the standing and layering time is 8 min; the volume ratio of the raffinate C to the nickel extractant is 1.2:1, and the standing and layering time is 8 min;
(3) carrying out back extraction on the extract B by using 3mol/L hydrochloric acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain copper salt crystals; the molar ratio of copper ions in the extract B to hydrogen ions in the acid solution is 1:2.5, and the standing and layering time is 40 min;
(4) and (3) carrying out back extraction on the extract liquid D by using a 5mol/L hydrochloric acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain the nickel salt crystal. The molar ratio of nickel ions in the extraction liquid D to hydrogen ions in the acid solution is 1:2.2, and the standing and layering time is 30 min.
Example 4
Example 4 differs from example 1 only in that: the concentrations of ions in the used electroplating sludge and electroplating waste liquid are different; and (4) in the step (3), the acid solution used for back extraction of the extract B is a 7.5mol/L sulfuric acid solution, and the standing and layering time is 35 min.
Example 5
Example 5 differs from example 1 only in that: the concentrations of ions in the used electroplating sludge and electroplating waste liquid are different; and (4) in the step (4), the acid solution used for back extraction of the extract D is a 7.5mol/L sulfuric acid solution, and the standing and layering time is 35 min.
Example 6
Example 6 differs from example 1 only in that: the concentrations of ions in the used electroplating sludge and electroplating waste liquid are different; in the step (3), the acid solution used for back extraction of the extract B is a 6mol/L sulfuric acid solution, and the standing and layering time is 35 min; and (4) in the step (4), the acid solution used for back extraction of the extract D is 9mol/L sulfuric acid solution, and the standing and layering time is 35 min.
Example 7
The present embodiment differs from embodiment 1 only in that: the mass ratio of the electroplating sludge to the electroplating waste liquid is 1: 3.
Example 8
The present embodiment differs from embodiment 1 only in that: the time for mixing, stirring and soaking the electroplating sludge and the electroplating waste liquid is 10 hours.
Example 9
The present embodiment differs from embodiment 1 only in that: the concentration of hydrogen peroxide in the hydrogen peroxide solution is 6 mol/L.
The concentrations of iron, copper and nickel ions of the solution in each stage of the treatment process in the examples 1-9 are detected by GB/T11911-1989, GB/T7475-1987 and GB/T11912-1989, and the purities of the corresponding copper salt crystals and nickel salt crystals in each implementation/comparison are detected, and the results are shown in tables 1-3.
TABLE 1
Injecting: the soaked mixed liquor is the mixed liquor obtained by mixing, stirring and soaking the electroplating sludge and the electroplating waste liquor in the step (1) in each implementation/comparative example; the copper extraction raffinate is raffinate C; the nickel extraction raffinate is raffinate obtained by extracting and layering raffinate C by adopting a nickel extracting agent
TABLE 2
Injecting: as in Table 1
TABLE 3
Injecting: as in Table 1
As is apparent from the concentrations of iron, copper and nickel ions in the solutions in the stages shown in tables 1 to 3, in the embodiments 1 to 6, after the cooperative treatment of the electroplating sludge and the electroplating waste liquid, the concentration of iron ions in the water body after the treatment can be effectively controlled to be lower than 1g/L, the concentration of copper ions to be lower than 10mg/L and the concentration of nickel ions to be lower than 40 mg/L; copper salt crystals and nickel salt crystals with the purity of more than 95 percent can be effectively obtained after evaporation crystallization. The treatment methods used in examples 7 to 9 do not use optimized technical parameters, have poor iron removal effect, and can effectively perform solvent electroplating on metals in sludge only when a proper amount of acid is contained in the waste liquid, thereby realizing subsequent extraction and solid-liquid conversion.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the protection scope of the present invention, and although the present invention is described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions can be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.
Claims (10)
1. The method for treating the electroplating sludge and the electroplating waste liquid is characterized by comprising the following steps of:
(1) mixing and soaking electroplating sludge and electroplating waste liquid, adding hydrogen peroxide solution for oxidation reaction, cooling and filtering, and filtering to obtain filtrate A;
(2) extracting the leaching solution A by using a copper extractant to obtain an extraction solution B and a raffinate C, and extracting the raffinate C by using a nickel extractant to obtain an extraction solution D;
(3) carrying out back extraction on the extract B by using an acid solution, preheating the obtained back-extraction liquid, and carrying out evaporative crystallization to obtain copper salt crystals;
(4) and (4) carrying out back extraction on the extraction liquid D by using an acid solution, preheating the obtained back extraction liquid, and carrying out evaporative crystallization to obtain the nickel salt crystal.
2. The method for treating electroplating sludge and electroplating waste liquid according to claim 1, wherein in the step (1), the mass ratio of the electroplating sludge to the electroplating waste liquid is 1: 4-5, and the soaking time is 12-24 h.
3. The method according to claim 1, wherein in the step (1), the concentration of hydrogen peroxide in the hydrogen peroxide solution is 9 to 11mol/L, and the mass of the hydrogen peroxide solution is 4 to 5% of the mass of the electroplating sludge.
4. The method for treating electroplating sludge and electroplating waste liquid according to claim 1, wherein in the step (1), the temperature of the oxidation reaction is 250-260 ℃, the pressure is 3.5-4.0 MPa, and the time is 1-2 h.
5. The method for treating electroplating sludge and electroplating effluent according to claim 1, wherein in the step (2), the copper extractant comprises nonylsalicylaldoxime, TXIB ester and kerosene; the mass ratio of the nonyl salicylaldoxime to the TXIB ester to the kerosene is nonyl salicylaldoxime: TXIB esters: kerosene is 4-6: 2-4: 2-5; the nickel extracting agent is 2-ethylhexyl phosphate monoester.
6. The method for treating electroplating sludge and electroplating waste liquid according to claim 1, wherein in the step (2), the volume ratio of the leaching solution A to the copper extractant is 0.5-2: 1, and the standing and layering time is 5-10 min; the volume ratio of the raffinate C to the nickel extracting agent is 0.5-2: 1, and the standing and layering time is 5-10 min.
7. The method for treating electroplating sludge and electroplating waste liquid according to claim 1, wherein in the step (3) and the step (4), the acid solution used for back extraction of the extraction liquid B and the extraction liquid E is at least one of a sulfuric acid solution and a hydrochloric acid solution, the concentration of the sulfuric acid solution is 6-9 mol/L, and the concentration of hydrogen chloride in the hydrochloric acid solution is 3-5 mol/L.
8. The method for treating electroplating sludge and electroplating waste liquid according to claim 7, wherein in the step (3) and the step (4), the acid solution used for back extraction is hydrochloric acid solution, and the concentration of hydrogen chloride in the hydrochloric acid solution is 3-5 mol/L.
9. The method for treating electroplating sludge and electroplating waste liquid according to claim 1, wherein in the step (3), the molar ratio of copper ions in the extract B to hydrogen ions in the acid solution is 1: 2.2-2.5, and the standing and layering time is 30-40 min; in the step (4), the molar ratio of nickel ions in the extraction liquid D to hydrogen ions in the acid solution is 1: 2.2-2.5, and the standing and layering time is 30-40 min.
10. The method for treating electroplating sludge and electroplating waste liquid according to claim 1, wherein in the step (3) and the step (4), the preheating temperature is 80-90 ℃, the evaporation crystallization temperature is 90-110 ℃, and the pressure is-0.01 MPa.
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