CN113265547A - Comprehensive recovery process for zinc hydrometallurgy organic purification cobalt slag - Google Patents
Comprehensive recovery process for zinc hydrometallurgy organic purification cobalt slag Download PDFInfo
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Abstract
The invention discloses a comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag. The comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag comprises the following steps of firstly slurrying, medium-temperature neutral leaching and washing of the purification cobalt slag, merging the leaching solution into a zinc hydrometallurgy sponge cadmium precipitation working section, slurrying and high-temperature high-acid leaching of the leaching slag, returning the leaching solution to the cobalt slag for medium-temperature neutral leaching, washing the leaching slag, returning washing water to the cobalt slag for leaching and high-leaching size mixing, slurrying and alkali leaching desiliconization of the washing slag, merging the alkali desiliconization solution into a sodium alum method iron removal working section to serve as a Na source and a neutralizing agent, washing the alkali leaching slag, returning the washing water to the alkali leaching size mixing, roasting the washing slag at medium temperature, burning off organic matters in the slag, realizing the secondary enrichment of cobalt in the purification cobalt slag, and achieving the requirement of cobalt smelting enterprises on the grade of the raw material cobalt.
Description
Technical Field
The invention belongs to the technical field of metallurgy, further belongs to the technical field of wet metallurgy, and particularly relates to a comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag.
Background
The zinc hydrometallurgy mainly takes zinc blende or zinc oxide ore as raw materials, wherein a certain amount of minerals containing cobalt are often associated, cobalt is dissolved into a solution during zinc leaching, the cobalt has great influence on the zinc electrolysis process, the zinc electrolysis current efficiency is obviously reduced after the cobalt reaches a certain concentration, and the zinc electrolysis is caused to burn a plate seriously to hinder the production operation. Based on the influence of cobalt in the wet-process zinc smelting process, zinc leaching solution needs deep purification for cobalt removal, the common cobalt removal process is replacement cobalt removal by activated zinc powder of antimony salt and arsenic salt, and as the cost of zinc powder purification for cobalt removal is high, organic cobalt removal reagents such as xanthate and beta-naphthol are also applied to the purification for cobalt removal by wet-process zinc smelting, a plurality of organic cobalt removal reagents are developed on the market on the basis of the organic cobalt removal reagents, and the cost of cobalt removal purification and the field production environment have obvious advantages compared with xanthate and beta-naphthol, so that the zinc leaching solution is popularized and applied in part of wet-process zinc smelting plants at present.
With the popularization of the new energy strategy of China, the battery industry is developing at a high speed, the lithium battery is developed rapidly as a battery product with excellent performance at present, materials related to the lithium battery are also high with water, cobalt is used as a part of raw materials of the lithium battery, the demand of the cobalt material is gradually increased under the background, the cobalt resource of China is deficient and mainly depends on import, so that purified cobalt slag generated by zinc hydrometallurgy is comprehensively recovered, on one hand, harmless recycling application of the cobalt slag is realized, on the other hand, the raw materials for cobalt smelting are also increased, and the high economic value and social benefit are achieved.
Disclosure of Invention
The invention aims to provide a comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag.
The invention aims to realize the comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag, which comprises the steps of medium-temperature neutral leaching, high-temperature peracid leaching, primary water washing, alkali leaching, secondary water washing and medium-temperature roasting, and specifically comprises the following steps:
A. neutral leaching at medium temperature: pulping the organic purified cobalt slag, and then performing neutral leaching at medium temperature to obtain leaching slag a and leaching solution b; the leaching solution b is merged into a sponge cadmium precipitation process in a zinc cadmium wet smelting process;
B. high-temperature high-acid leaching: pulping the leaching residue a, and then carrying out high-temperature high-acid leaching to obtain leaching residue c and leaching solution d; returning the leaching solution d to the medium-temperature neutral leaching step;
C. first-stage water washing: washing the leached residues c with water to obtain washing residues e and washing water f; the washing water f returns to the step of slurrying in the medium-temperature neutral leaching and/or the high-temperature high-acid leaching;
D. alkaline leaching: pulping the washing residues, and performing alkaline leaching to obtain alkaline leaching residues g and alkaline leaching solution h; the alkali leaching solution h is merged into a sodium vanadium method iron removal process;
E. secondary water washing: washing the alkaline leaching residue g with water to obtain washing residue i and washing water j; washing water j returns to the step of slurrying in alkaline leaching;
F. intermediate-temperature roasting: roasting the washing slag i at medium temperature to obtain flue gas k and calcine l, wherein the calcine l is cobalt concentrate; the flue gas k is merged into the boiler flue gas treatment.
The research and the report of the recycling of the purified cobalt slag of zinc hydrometallurgy are common, but the main body aims at the comprehensive recycling of the cobalt slag replaced by zinc powder, a few researches aim at the comprehensive recycling of xanthate and beta-naphthol precipitated cobalt slag, the research and the study of the comprehensive recycling of the cobalt slag produced by removing cobalt by a modified active xanthate organic purification reagent and an inorganic activator are only rarely reported, the process of treating the organic reagent cobalt slag by medium-immersion, high-immersion, alkaline-immersion and roasting is provided on the basis of looking up a large amount of literature and early-stage exploration experiments, the medium-immersion liquid returns to precipitate sponge cadmium, the alkaline solution returns to the production process, sodium alum is used for removing iron, the goal of the solution recovery production process in the cobalt slag recovery process is realized, and the treatment process is reduced; the reason why the flue gas generated in the process of medium-temperature roasting of the cobalt slag is merged into the flue gas of the boiler is that the main body of the flue gas generated in the process of medium-temperature roasting is carbon dioxide and a small amount of dust, in addition, the amount of the cobalt slag is relatively small, the amount of the generated flue gas is limited, the cobalt content is 10mg/L after iron removal in a zinc smelting plant, 10 ten thousand tons of zinc ingots are produced every year, and the amount of the produced washing cobalt slag is about 400 tons every year; and roasting the cobalt slag to produce roasted product, namely the cobalt concentrate.
According to the standard of purchasing cobalt raw materials provided by a certain cobalt smelting enterprise: the Co + Cu is more than or equal to 25 percent, the Ca is less than or equal to 5 percent, the Mg is less than or equal to 5 percent, the Mn is less than or equal to 4 percent, the Fe is less than or equal to 5 percent, the Zn is less than or equal to 1 percent, the Al is less than or equal to 2 percent, the Pb is less than or equal to 1 percent, and the P is less than or equal to 1 percent.
The comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag comprises the following specific operation steps:
(1) pulping organic purified cobalt slag, and neutral leaching at medium temperature;
(2) merging the leachate obtained in the step (1) into a sponge cadmium precipitation process in a zinc cadmium hydrometallurgy working section;
(3) pulping the leaching residue in the step (1), and leaching at high temperature and high acid;
(4) returning the leachate obtained in the step (3) to the step (1) for pulping and leaching;
(5) washing the leached residues in the step (3) with water, returning the washing water to the cobalt residues for leaching and high-leaching pulp mixing;
(6) slurrying the water washing slag in the step (5) and carrying out alkaline leaching;
(7) the alkaline leaching solution in the step (6) is merged into an iron removal process by a sodium alum method;
(8) washing the leaching residue in the step (6) with water, and returning the washing water to alkaline leaching for size mixing;
(9) roasting the washing slag in the step (8) at medium temperature;
(10) merging the flue gas generated in the step (9) into boiler flue gas for treatment;
(11) and (4) obtaining the roasted product generated in the step (9) as the cobalt concentrate.
The comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag preferably comprises the following steps: in the step (1), the organic purification cobalt slag is cobalt slag produced by removing cobalt by using a modified active xanthate organic purification reagent and an inorganic activator;
the comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag preferably comprises the following steps: in the step (1), pulping the organic purified cobalt slag, performing medium-temperature neutral leaching by using a high-temperature high-acid leaching solution as a leaching stock solution, wherein the temperature and the acid are the residual temperature of the high-temperature high-acid leaching solution at 40-70 ℃ and the residual acid at 20-40 g/L;
the comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag preferably comprises the following steps: in the step (1), the concentration of ore pulp subjected to medium-temperature neutral leaching is 0.1-0.3g/mL, the leaching time is 60-120min, and the neutral leaching means that the pH value at the leaching end point is 5.0-5.4;
the comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag preferably comprises the following steps: in the step (2), the working procedure of sponge cadmium deposition in the cadmium working section is a process for replacing cadmium in a zinc sulfate solution with zinc powder to produce sponge cadmium, the pH value of a system needs to be controlled to be 5.0-5.4, the risk of generating arsenic hydride is caused if the pH value is too low, and the pH value of a neutral leaching solution of copper cadmium slag does not exceed 5.4;
the comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag preferably comprises the following steps: in the step (3), the temperature of the high-temperature peracid leaching is 70-90 ℃, and particularly preferred is: the high-temperature peracid leaching temperature is 75-85 ℃, the temperature range is selected mainly to ensure that elements such as zinc, cadmium, iron and the like in the cobalt slag are fully leached, the water evaporation loss is large when the temperature exceeds 85 ℃, and the temperature range is selected by comprehensively considering the leaching rate of metal elements and the field operation environment; the acidity of the initial acid is 40-120g/L, the final acid is controlled to be 0-80g/L, and the following is particularly preferred: the initial acid acidity is 60-80g/L, the final acid is controlled to be 20-40g/L, the range of the acidity is selected to ensure the high-efficiency leaching of the metal elements, and simultaneously, the pH value at the medium-temperature neutral leaching end point is 5.0-5.4; the concentration of the ore pulp is 0.1-0.2g/mL, the added acid can be concentrated sulfuric acid, waste electrolyte or a mixture of the concentrated sulfuric acid and the waste electrolyte, the leaching time is 60-300min, and particularly preferred is that: leaching for 90-180 min;
the comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag preferably comprises the following steps: in the step (6), the temperature in the alkaline leaching process is 45-85 ℃, the NaOH concentration is 20-100g/L, and particularly preferred is that: the concentration of NaOH is 30-60 g/L; the concentration of the ore pulp is 0.1-0.2g/mL, and the alkaline leaching time is 60-180 min;
the comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag preferably comprises the following steps: in the step (9), the medium-temperature roasting is carried out, the roasting temperature is 300-: the roasting temperature is 500-700 ℃; the roasting time is 30-300min, and particularly preferred is that: the baking time is 120-240 min.
The technical scheme of the invention is mainly based on the following principle: the zinc hydrometallurgy organic purification cobalt slag mainly comprises 12-18% of Zn, 3-10% of Fe, 1-5% of Cd, 78-10% of SiO 25, 1-2% of Co, and low contents of Cu, Ca, Mg, Al, Pb, Mn, P and other elements; zn in the cobalt slag exists basically in the form of zinc sulfate and can be effectively leached under the condition of proper acidity, Cd and Fe exist in two forms, namely sulfate and sulfide, an iron part also exists in the form of goethite, the part existing in the form of sulfate and the goethite is easy to leach, and the part existing in the form of sulfide is relatively difficult to leach; according to the principle analysis of cobalt precipitation by using a modified active xanthate organic reagent, the cobalt complex formed in the cobalt precipitation process is similar to the cobalt precipitation by using xanthate and beta-naphthol, the cobalt leaching rate in the cobalt residues of the two organic reagents in the conventional acid leaching process is very low, the cobalt precipitation slag of the modified active xanthate organic reagent is obtained by combining an exploration experiment, the leaching rate of Co in the middle leaching process and the high leaching process is very low, and the total leaching rate of two sections is less than 2%, so that a support is provided for the cobalt residue treatment by the middle leaching-high leaching-alkaline leaching-roasting process; in the acid leaching process, the leachable part of Si is less, most of Si is left in acid leaching residue, desiliconization is required to be realized, the grade of cobalt concentrate is further improved, desiliconization can be performed in the common modes of ore dressing or smelting and the like, in consideration of the effect of ore dressing desiliconization and the loss of cobalt, alkali leaching desiliconization is selected, SiO2 in the cobalt residue and NaOH form Na2SiO3 during alkali leaching and are dissolved in a solution to realize cobalt residue desiliconization, and the loss of cobalt in the alkali leaching process of the cobalt residue is less than 1%; the medium-temperature roasting of the cobalt slag is to burn out inorganic matters such as cobalt in the cobalt slag which only account for 10-20% of the total amount of the slag, and the rest 80-90% of the inorganic matters by roasting, and the rest inorganic salt main body is cobalt concentrate. In conclusion, the xanthate cobalt slag can realize comprehensive recovery of valuable metals such as zinc, cadmium, cobalt and the like in the cobalt slag through medium leaching, high leaching, alkaline leaching and roasting.
The comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag has the advantages that:
(1) the invention adopts the middle leaching-high leaching-alkaline leaching-roasting process to treat the zinc hydrometallurgy modified active xanthic acid organic purified cobalt slag, realizes the recycling of valuable elements such as zinc, cobalt and the like in the cobalt slag, reduces the stock of hazardous waste residues in a zinc smelting plant, and creates economic value and social benefit for enterprises;
(2) silicon in the organic cobalt slag still remains in a solid phase in the acid leaching process, the grade of cobalt concentrate produced by direct roasting is 20 percent lower than that of cobalt concentrate produced by roasting after desiliconization, and in addition, in combination with the production practice of a zinc smelting plant, alkaline leaching solution is returned to a sodium alum method iron removal process to be used as a part of sodium source and a neutralizing agent;
(3) the organic cobalt slag is leached by adopting the combination of medium leaching and high leaching, so that the high-efficiency leaching of elements such as zinc, cadmium, iron and the like in the cobalt slag is met, and the production requirement of the working procedure of returning the leachate to the sponge cadmium precipitation is met.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention.
Detailed Description
The present invention is further illustrated by the following examples and the accompanying drawings, but the present invention is not limited thereto in any way, and any modifications or alterations based on the teaching of the present invention are within the scope of the present invention.
The comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag comprises the steps of medium-temperature neutral leaching, high-temperature peracid leaching, primary water washing, alkaline leaching, secondary water washing and medium-temperature roasting, and specifically comprises the following steps:
A. neutral leaching at medium temperature: pulping the organic purified cobalt slag, and then performing neutral leaching at medium temperature to obtain leaching slag a and leaching solution b; the leaching solution b is merged into a sponge cadmium precipitation process in a zinc cadmium wet smelting process;
B. high-temperature high-acid leaching: pulping the leaching residue a, and then carrying out high-temperature high-acid leaching to obtain leaching residue c and leaching solution d; returning the leaching solution d to the medium-temperature neutral leaching step;
C. first-stage water washing: washing the leached residues c with water to obtain washing residues e and washing water f; the washing water f returns to the step of slurrying in the medium-temperature neutral leaching and/or the high-temperature high-acid leaching;
D. alkaline leaching: pulping the washing residues, and performing alkaline leaching to obtain alkaline leaching residues g and alkaline leaching solution h; the alkali leaching solution h is merged into a sodium vanadium method iron removal process;
E. secondary water washing: washing the alkaline leaching residue g with water to obtain washing residue i and washing water j; washing water j returns to the step of slurrying in alkaline leaching;
F. intermediate-temperature roasting: roasting the washing slag i at medium temperature to obtain flue gas k and calcine l, wherein the calcine l is cobalt concentrate; the flue gas k is merged into the boiler flue gas treatment.
The organic purification cobalt slag is produced by removing cobalt by using a modified active xanthic acid organic purification reagent and an inorganic activator.
In the step A, the concentration of the ore pulp subjected to medium-temperature neutral leaching is 0.1-0.3g/ml, the leaching time is 60-120min, and the pH value of the leaching end point is 5.0-5.4.
The working procedure of sponge cadmium precipitation in the cadmium working section in the step A is a process for replacing cadmium in zinc sulfate solution with zinc powder to produce sponge cadmium, and the pH value of the system is controlled to be 5.0-5.4.
And B, the temperature of the high-temperature peracid leaching in the step B is 70-90 ℃, the concentration of the ore pulp is 0.1-0.2g/ml, the leaching time is 60-300min, and the pH value of the leaching end point is 5.0-5.4.
The temperature of the high-temperature peracid leaching is 75-85 ℃.
And D, in the step D, the temperature of alkaline leaching is 45-85 ℃, and the concentration of NaOH is 20-100 g/L.
The concentration of the alkaline leaching ore pulp is 0.1-0.2g/ml, the concentration of NaOH is 30-60g/L, and the alkaline leaching time is 60-180 min.
In the step F, the medium-temperature roasting temperature is 300-900 ℃, and the roasting time is 30-300 min.
The medium-temperature roasting temperature is 500-700 ℃, and the roasting time is 120-240 min.
The invention is further illustrated by the following specific examples:
example 1
Intermediate leaching: 500g of cobalt slag, 0.2g/mL of ore pulp concentration, 30g/L of acidity, 50 ℃ of temperature and 60min of time, pH of leachate is 5.0, and the cobalt loss of the leachate is 0.09%; high-temperature high-acid leaching: the concentration of ore pulp of all the middle leaching residues is 0.2g/mL, the acidity is 70g/L, the temperature is 80 ℃, the time is 120min, the acidity of a leaching solution is 28g/L, the cobalt loss is 0.15 percent in terms of solution, and the leaching rate of main components in terms of residues is as follows: zn 97.70%, Cd 92.82%, Fe 96.17%, Co 0.45%, SiO212.14 percent; taking 50g of dried two-stage acid-leaching cobalt slag, roasting at 600 ℃ for 150min, wherein the yield of roasted product is 19.42%, and the cobalt concentrate comprises the following components: 32.18% of Co, 0.51% of Cu, 0.81% of CaO, 0.17% of MgO, 0.60% of Mn, 2.04% of Fe, 2.35% of Zn, 0.98% of Al, 0.15% of Pb, 0.32% of P, and SiO2 38.54%。
Example 2
Intermediate leaching: 500g of cobalt slag, 0.2g/mL of ore pulp concentration, 30g/L of acidity, 50 ℃ of temperature and 80min of time, pH of leachate is 5.0, and cobalt loss is 0.10% by liquid meter; high-temperature high-acid leaching: the concentration of ore pulp of all the middle leaching residues is 0.2g/mL, the acidity is 80g/L, the temperature is 80 ℃, the time is 120min, the acidity of the leaching solution is 35g/L, the cobalt loss is 0.14% by liquid meter, and the leaching rate of main components is calculated by residues: zn 98.93%, Cd 93.27%, Fe 95.83%, Co 0.82%, SiO2 10.69 percent; taking 50g of dried two-stage acid-leaching cobalt slag, roasting at 600 ℃ for 60min, wherein the yield of roasted product is 29.85%, and the cobalt concentrate comprises the following components: co 25.67%, Cu 0.32%, CaO 0.41%, MgO 0.36%, Mn 0.45%, Fe 1.89%, Zn 1.65%, Al 0.79%, Pb 0.11%, P0.41%, SiO2 33.67%。
Example 3
Intermediate leaching: 500g of cobalt slag, 0.2g/mL of ore pulp concentration, 30g/L of acidity, 40 ℃ of temperature and 60min of time, pH of leachate is 5.0, and cobalt loss is 0.11% by liquid meter; high-temperature high-acid leaching: the concentration of ore pulp of all the middle leaching residues is 0.2g/mL, the acidity is 70g/L, the temperature is 80 ℃, the time is 120min, the acidity of the leaching solution is 26g/L, the cobalt loss is 0.09% in terms of liquid, and the leaching rate of main components in terms of residues is as follows: zn 98.02%, Cd 92.39%, Fe 94.71%, Co 0.53%, SiO29.98 percent; taking 50g of dried two-stage acid-leaching cobalt slag, roasting at 700 ℃ for 150min, wherein the yield of roasted product is 18.69%, and the cobalt concentrate comprises the following components: 33.37% of Co, 0.48% of Cu, 0.75% of CaO, 0.09% of MgO, 0.42% of Mn, 2.41% of Fe, 1.87% of Zn, 0.77% of Al, 0.12% of Pb, 0.36% of P, SiO2 40.13%。
Example 4
Intermediate leaching: 500g of cobalt slag, 0.2g/mL of ore pulp concentration, 30g/L of acidity, 50 ℃ of temperature and 60min of time, pH of leachate is 5.0, and the cobalt loss of the leachate is 0.09%; high-temperature high-acid leaching: the concentration of ore pulp of all the middle leaching residues is 0.2g/mL, the acidity is 80g/L, the temperature is 80 ℃, the time is 120min, the acidity of the leaching solution is 36g/L, the cobalt loss is 0.17% by liquid meter, and the leaching rate of main components is calculated by residues: zn 98.85%, Cd 93.25%, Fe 96.45%, Co 0.62%, SiO210.58 percent; alkaline leaching desiliconization: all the high leaching residues have the pulp concentration of 0.1g/mL, the alkalinity of 50g/L, the temperature of 80 ℃, the time of 120min, the cobalt loss of 0.20 percent in liquid meter and SiO percent in residue meter2The leaching rate is 98.34 percent; taking 50g of dried alkaline leaching residue, roasting at 600 ℃ for 150min, wherein the yield of roasted product is 12.05%, and the cobalt concentrate comprises the following components: co 55.31%, Cu 0.85%, CaO 0.98%, MgO 0.31%, Mn 0.58%, Fe 3.67%, Zn 3.82%, Al 1.37%, Pb 0.32%, P0.38%, SiO25.21 %。
Example 5
Intermediate leaching: 500g of cobalt slag, 0.2g/mL of ore pulp concentration, 30g/L of acidity, 50 ℃ of temperature, 60min of time, pH5.0 of leachate, and 0.10% of cobalt loss in a liquid meter; high-temperature high-acid leaching: the concentration of ore pulp of all the middle leaching residues is 0.2g/mL, the acidity is 80g/L, the temperature is 80 ℃, the time is 120min, the acidity of the leaching solution is 36g/L, the cobalt loss is 0.16% by liquid meter, and the leaching rate of main components is calculated by residues: zn 98.55%, Cd 93.52%, Fe 95.78%, Co 0.63%, SiO211.34 percent; alkaline leaching desiliconization: all the high leaching residues have the pulp concentration of 0.2g/mL, the alkalinity of 40g/L, the temperature of 70 ℃, the time of 150min, the cobalt loss of 0.17 percent in liquid meter and SiO percent in residue meter2The leaching rate is 92.84 percent; taking 50g of dried alkaline leaching residue, roasting at 600 ℃ for 150min, wherein the yield of roasted product is 15.02%, and the cobalt concentrate comprises the following components: co 44.21%, Cu 0.74%, CaO 0.83%, MgO 0.21%, Mn 0.48%, Fe 3.11%, Zn 3.29%, Al 1.09%, Pb 0.26%, P0.39%, SiO210.12 %。
Claims (10)
1. The comprehensive recovery process of the zinc hydrometallurgy organic purification cobalt slag is characterized by comprising the steps of medium-temperature neutral leaching, high-temperature peracid leaching, primary washing, alkaline leaching, secondary washing and medium-temperature roasting, and specifically comprises the following steps:
A. neutral leaching at medium temperature: pulping the organic purified cobalt slag, and then performing neutral leaching at medium temperature to obtain leaching slag a and leaching solution b; the leaching solution b is merged into a sponge cadmium precipitation process in a zinc cadmium wet smelting process;
B. high-temperature high-acid leaching: pulping the leaching residue a, and then carrying out high-temperature high-acid leaching to obtain leaching residue c and leaching solution d; returning the leaching solution d to the medium-temperature neutral leaching step;
C. first-stage water washing: washing the leached residues c with water to obtain washing residues e and washing water f; the washing water f returns to the step of slurrying in the medium-temperature neutral leaching and/or the high-temperature high-acid leaching;
D. alkaline leaching: pulping the washing residues, and performing alkaline leaching to obtain alkaline leaching residues g and alkaline leaching solution h; the alkali leaching solution h is merged into a sodium vanadium method iron removal process;
E. secondary water washing: washing the alkaline leaching residue g with water to obtain washing residue i and washing water j; washing water j returns to the step of slurrying in alkaline leaching;
F. intermediate-temperature roasting: roasting the washing slag i at medium temperature to obtain flue gas k and calcine l, wherein the calcine l is cobalt concentrate; the flue gas k is merged into the boiler flue gas treatment.
2. The process of claim 1, wherein the organic purified cobalt residue is produced by removing cobalt with a modified active xanthate organic purifying agent and an inorganic activating agent.
3. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag according to claim 1, characterized in that in the step A, the concentration of ore pulp subjected to medium-temperature neutral leaching is 0.1-0.3g/ml, the leaching time is 60-120min, and the pH value at the end of leaching is 5.0-5.4.
4. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag as claimed in claim 1, wherein the step of cadmium sponge precipitation in the cadmium working section in the step a is a process of replacing cadmium in zinc sulfate solution with zinc powder to produce sponge cadmium, and the pH value of the system is controlled to be 5.0-5.4.
5. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag according to claim 1, characterized in that the temperature of high temperature peracid leaching in step B is 70-90 ℃, the pulp concentration is 0.1-0.2g/ml, the leaching time is 60-300min, and the pH value at the end of leaching is 5.0-5.4.
6. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag according to claim 1 or 5, characterized in that the temperature of the high temperature peracid leaching is 75-85 ℃.
7. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag according to claim 1, wherein the temperature of alkaline leaching in the step D is 45-85 ℃, and the concentration of NaOH is 20-100 g/L.
8. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag according to claim 1 or 7, characterized in that the concentration of the alkaline leaching ore pulp is 0.1-0.2g/ml, the concentration of NaOH is 30-60g/L, and the time of alkaline leaching is 60-180 min.
9. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag according to claim 1, characterized in that the temperature of medium-temperature roasting in the step F is 300-900 ℃, and the roasting time is 30-300 min.
10. The comprehensive recovery process of zinc hydrometallurgy organic purification cobalt slag according to claim 1 or 9, characterized in that the medium-temperature roasting temperature is 500-700 ℃, and the roasting time is 120-240 min.
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