Classifications

• • 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
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
  • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
  • C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
• • 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
  • 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
• • 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
  • 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
  • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
• • 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
  • C22B47/00—Obtaining manganese
• • 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
  • C22B47/00—Obtaining manganese
  • C22B47/0018—Treating ocean floor nodules
  • C22B47/0045—Treating ocean floor nodules by wet processes
  • C22B47/0081—Treatment or purification of solutions, e.g. obtained by leaching
• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
  • C25B1/00—Electrolytic production of inorganic compounds or non-metals
  • C25B1/01—Products
  • C25B1/21—Manganese oxides
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P10/00—Technologies related to metal processing
  • Y02P10/20—Recycling

Definitions

• the invention relates to a method for producing mercury-free alkali-manganese electrolytic manganese dioxide, in particular to a method for producing mercury-free alkali-manganese electrolytic manganese dioxide by using the "two-mine method" to extract ultra-low-grade manganese oxide ore. Background technique
• the alkaline manganese battery As the best high-power battery in the battery industry, the alkaline manganese battery has stable working voltage, high current continuous discharge, excellent performance, long storage time (up to 3 ⁇ 5 years), low temperature performance and good leakproof performance. And so on, it is well received by consumers at home and abroad.
• the main raw material for the production of alkaline manganese batteries mercury-free alkali-manganese electrolytic manganese dioxide, has a worldwide annual consumption of more than 300,000 tons and is increasing at a rate of more than 10% per year, which has broad market prospects.
• manganese carbonate or manganese oxide ore is used as raw material.
• domestic manganese carbonate ore is used as raw material, and manganese ore consumption is low due to low manganese carbonate content in the ore (30% or less).
• the main methods currently used are reduction roasting of manganese oxide ore after leaching to produce liquid or using "two-mine method” to produce electrolytic manganese dioxide, and using reduced roasting manganese oxide ore after leaching
• the liquid preparation process has the disadvantages of long process flow, high production cost, and easy pollution to the surrounding environment of the plant; high-grade manganese oxide ore is used as raw material, and electrolytic manganese dioxide is produced by the "two-mine method", that is, two The manganese oxide ore is leached together with the reducing agent pyrite, because the manganese ore in the domestic manganese metallurgy industry adopts the intermittent leaching process, that is, the manganese ore is directly dissolved into the solution in only one leaching tank, and the process has a grade of 25% for the low grade manganese ore.
• the following ore has a low leaching rate, a long turnaround time between materials, and the number of equipment
• the disadvantages of increased and low utilization rate; and the use of such high-grade manganese ore resources (with grades above 25%) are decreasing, making it difficult to maintain long-term production.
• Guangxi manganese ore resources are abundant, but most of them are low-grade manganese ore, which is characterized by low manganese content and high impurity content, which has not been fully exploited for a long time. Summary of the invention
• the technical problem to be solved by the present invention is to provide an ultra-low-grade manganese oxide ore as a main material,
• the "two-mine method" produces a mercury-free alkaline manganese type electrolytic manganese dioxide.
• the technical solution adopted by the present invention to solve the above technical problems is to provide a mercury-free alkaline manganese type electrolytic manganese dioxide production method, which comprises the following steps in sequence: (1) mixing manganese oxide ore with pyrite and continuously simultaneously with sulfuric acid Continuously put into a continuous leaching tank consisting of 1 ⁇ 7 stirred leaching tanks in series to form one or more stages of continuous leaching, the process reaction temperature is controlled at 90 ⁇ 95 ° C, the reaction time is about 3 ⁇ 4 hours, leaching After the reaction is completed, the potassium ion is removed first, and then the iron is removed by neutralization and iron removal. The lime powder is added to the lime solution to adjust the solution ra to 6 to 6.
• the reaction time is about 3 to 4 hours, and the temperature is 90 to 95 ° C.
• the chute is dynamically removed from calcium and magnesium, and then sent to a static tank for 32 hours to precipitate the solution to remove calcium and magnesium impurities.
• the prepared suspending agent and foaming agent are added to the respective electrolytic cells through the pipeline.
• the electrolysis conditions are as follows: The electrolyte temperature is 100 ⁇ 103 °C, the anode current density is 80 ⁇ 85A/m 2 , the cell voltage is 2. 2 ⁇ 3. 5V, the electrolysis cycle is 12 ⁇ 20 days, and the mercury-free alkaline manganese type electrolytic manganese dioxide is obtained after electrolysis.
• the manganese oxide ore and pyrite are directly fed into the continuous leaching tank at a ratio of 1:0.4, and at the same time, 1:4.7.
• the mineral acid ratio is blended with sulfuric acid and waste electrolyte.
• the waste electrolyte is derived from the tail liquid after the electrolysis in the step 3.
• the anodic electrolytic manganese dioxide crude product obtained by electrolysis is crushed into particles of 6 to 8 mm, and is washed into a rinsing tank and washed with water and alkali.
• the three-stage rinsing process the temperature of the second rinsing lye is 60 ⁇ 7 (TC, the temperature of the last rinsing water is 80 ⁇ 90 °C, the rinsing period is about 40 hours, and the rinsing liquid is directly heated by steam, after Electrolyzed manganese dioxide that has been milled to the desired particle size.
• the milled electrolytic manganese dioxide is fed into a gravity-type mixing silo by means of dense phase transportation for homogenization, and the mixing time is about 16 hours.
• the method for producing mercury-free alkali-manganese electrolytic manganese dioxide uses ultra-low-grade manganese oxide ore as a main raw material, and uses the "two-mine method" to directly extract ultra-low Manganese in manganese oxide ore, after obtaining manganese sulfate solution, deep purification and impurity removal, re-electrolysis to produce mercury-free alkali manganese
• the type of electrolytic manganese dioxide can be reduced to 16% using manganese oxide ore, and the production process is not only applicable to manganese oxide ore with low grade and complex source, but also to high-grade manganese oxide ore.
• the ferromanganese ore powder containing 14.32% of manganese and the pyrite powder having a sulfur content of 44.4% is mixed according to the dry specific gravity of 1:24, and the sulfuric acid having a concentration of 98% is added with water to prepare 100 g/L.
• the dilute sulfuric acid solution, the mixed manganese oxide powder and the pyrite powder and the prepared sulfuric acid are continuously added to the continuous leaching tank at a ratio of 1:0.7, and continuously stirred, and the continuous leaching tank is composed of one
• the leaching tank is formed to form a first-stage continuous leaching, the effective volume of the leaching tank is lm 3 , the bath temperature is 95 ° C, and the leaching reaction time is 3 hours from the feeding to the liquid leaching tank, and the PH value is 3 ⁇ 3.
• the leaching reaction is completed, and the reaction is continuously stirred.
• the liquid flowing out of the leaching tank enters the neutralization tank in series with the neutralization tank.
• the effective volume of the neutralization tank is 1. 5 m 3 , and the lime powder is continuously added.
• the neutralization reaction was carried out to control the ra value to be 6.0.
• the reaction time was 3 hours.
• the filtrate after neutralization was filtered, and the filter residue was sent to a slag field to obtain a crude manganese sulfate solution.
• the crude manganese sulfate solution contains heavy metals such as copper, cobalt, nickel and lead, and impurities such as calcium and magnesium.
• the two-stage continuous purification process is used.
• the crude manganese sulfate solution enters a continuous purification process to add calcium polysulfide, and the temperature is controlled at 60 ° C.
• the filter residue is sent to the slag field, and the solution enters the second stage purification.
• the calcium and magnesium are dynamically removed through the chute, and then sent to the static storage tank, and allowed to stand for 32 hours to precipitate the solution, and the calcium and magnesium impurities are precipitated and removed, thereby obtaining refined manganese sulfate.
• the solution, the filter residue is sent to the slag field, and the filtrate is sent to the electrolysis.
• the refined qualified manganese sulfate solution is subjected to ultrafine filtration, and is heated to 9 CTC through a plate heat exchanger to enter a high-level tank for suspension electrolysis.
• the prepared suspending agent and foaming agent were added, the electrolyte temperature was 100 ° C, the anode current density was 81 A/m 2 , the cell voltage was 2. 4 V, the electrolysis cycle was 12 days, and the manganese dioxide was stripped from the anode.
• the product is crushed to 6 ⁇ 8mm particles by the crusher and then into the rinsing tank.
• the effective volume of each rinsing tank is Lm 3 , a three-stage rinsing process using water-washing-alkaline washing and one-washing.
• the temperature of the second rinsing lye is 60 ° C
• the temperature of the last rinsing water is 80 ° C
• the rinsing period is 40 hours
• the rinsing liquid is used.
• the steam is heated directly.
• the electrolytic manganese dioxide is sent to the pendulum mill to collect the product powder (particle size -325 mesh).
• the dense phase conveying method is used to send the gravity mixing bin. Homogenization blending was carried out for about 16 hours to produce a qualified mercury-free alkali manganese-type manganese dioxide product.
• the ferromanganese ore powder containing 15.56% of manganese, the pyrite powder having a sulfur content of 40.4% is mixed according to the dry specific gravity of 1:24, and the sulfuric acid having a concentration of 98% is added with water to prepare 100g/L.
• the dilute sulfuric acid solution, the mixed manganese oxide powder and the pyrite powder and the prepared sulfuric acid are continuously added to the continuous leaching tank at a ratio of 1:0.7, and continuously stirred, and the continuous leaching tank is composed of three
• the leaching tanks are arranged in series to form a three-stage continuous leaching.
• the effective volume of each leaching tank is lm 3 , and the liquid enters the second-stage leaching tank and then enters the third-stage leaching tank.
• the temperature of each tank is 93 ° C.
• the leaching reaction time of the feed liquid from the third-stage leaching tank is 3.5 hours, and the stirring is continued during the reaction, and the liquid flowing out of the tertiary leaching tank enters the neutralization tank connected in series, and the neutralization tank is The effective volume is 1.5 m 3 , and then the lime powder is continuously added for the neutralization reaction, the control 13 ⁇ 4 value is 6.3, the reaction time is 3.5 hours, the filtrate after the neutralization is filtered, and the filter residue is sent to the slag field to obtain a coarse Making manganese sulfate solution.
• the crude manganese sulfate solution contains heavy metals such as copper, cobalt, nickel and lead, and impurities such as calcium and magnesium.
• the two-stage continuous purification process is used.
• the crude manganese sulfate solution enters a continuous purification process to add calcium polysulfide, and the temperature is controlled at 60 ° C.
• the filter residue is sent to the slag field, and the solution enters the second stage purification.
• the calcium and magnesium are dynamically removed through the chute, and then sent to the static storage tank, and allowed to stand for 32 hours to precipitate the solution, and the calcium and magnesium impurities are precipitated and removed, thereby obtaining refined manganese sulfate.
• the solution, the filter residue is sent to the slag field, and the filtrate is sent to the electrolysis.
• the refined qualified manganese sulfate solution is subjected to ultrafine filtration, and is heated to 95 ° C in a plate heat exchanger to enter a high-position tank for suspension electrolysis.
• the prepared suspending agent and foaming agent were added, the electrolyte temperature was 102 ° C, the anode current density was 83 A/m 2 , the cell voltage was 2. 9 V, the electrolysis cycle was 15 days, and the manganese dioxide was stripped from the anode.
• the product is crushed to 6 ⁇ 8mm particles by the crusher, and then enters the rinsing tank.
• each rinsing tank The effective volume of each rinsing tank is lm 3 , and the three-stage rinsing process is washed with water and alkali, and the lye is washed twice.
• the temperature is 65 ° C
• the last rinse water temperature is 85 ° C
• the rinse cycle is 40 hours
• the rinse liquid is directly heated by steam.
• the electrolytic manganese dioxide is sent to the pendulum mill to collect the product powder (particle size -325 mesh).
• the dense phase conveying method is used to send the gravity mixing bin. Homogenization blending was carried out for about 16 hours to produce a qualified mercury-free alkali manganese-type manganese dioxide product.
• Example 3 The ferromanganese ore powder containing 13.58% of manganese and the pyrite powder having a sulfur content of 47.48% are mixed according to the dry specific gravity of 1:24, and the sulfuric acid having a concentration of 98% is added with water to prepare 100 g/L.
• the dilute sulfuric acid solution, the mixed manganese oxide powder and the pyrite powder and the prepared sulfuric acid are continuously added to the continuous leaching tank at a ratio of 1:0.7 while continuously stirring, and the continuous leaching tank is composed of seven
• the leaching tanks are arranged in series to form a seven-stage continuous leaching.
• the effective volume of each leaching tank is lm 3 .
• the feed liquid enters the second-stage leaching tank and then enters the third to seventh-stage leaching tanks.
• the temperature of each tank is 95°. C
• the leaching reaction time from the feeding to the feed liquid from the seventh-stage leaching tank is 4 hours
• the stirring is continued during the reaction
• the liquid flowing out from the seventh-stage leaching tank enters the neutralization tank connected in series, and the neutralization tank
• the effective volume is 1.5 m 3
• the lime powder is continuously subjected to the neutralization reaction
• the control 13 ⁇ 4 value is 6.5.
• the neutralized filtrate is filtered, and the filter residue is sent to the slag field to obtain a crude manganese sulfate solution.
• the crude manganese sulfate solution contains heavy metals such as copper, cobalt, nickel and lead, and impurities such as calcium and magnesium.
• the two-stage continuous purification process is used.
• the crude manganese sulfate solution enters a continuous purification process to add calcium polysulfide, and the temperature is controlled at 60 ° C.
• the filter residue is sent to the slag field, and the solution enters the second stage purification.
• the calcium and magnesium are dynamically removed through the chute, and then sent to the static storage tank, and allowed to stand for 32 hours to precipitate the solution, and the calcium and magnesium impurities are precipitated and removed, thereby obtaining refined manganese sulfate.
• the solution, the filter residue is sent to the slag field, and the filtrate is sent to the electrolysis.
• the refined qualified manganese sulfate solution is subjected to ultrafine filtration, and is heated to locrc through a plate heat exchanger to enter a high-position tank for suspension electrolysis.
• the prepared suspending agent and foaming agent were added, the electrolyte temperature was 103 ° C, the anode current density was 85 A/m 2 , the cell voltage was 3.5 V, the electrolysis cycle was 20 days, and the manganese dioxide was stripped from the anode.
• the product is crushed to 6 ⁇ 8mm particles by the crusher, and then enters the rinsing tank.
• each rinsing tank The effective volume of each rinsing tank is lm 3 , and the three-stage rinsing process is washed with water and alkali, and the lye is washed twice.
• the temperature is 70 ° C
• the last rinse water temperature is 85 ° C
• the rinse cycle is 40 hours
• the rinse liquid is directly heated by steam.
• the electrolytic manganese dioxide is sent to the pendulum mill to collect the product powder (particle size -325 mesh).
• the dense phase conveying method is used to send the gravity mixing bin. Homogenization blending was carried out for about 16 hours to produce a qualified mercury-free alkali manganese-type manganese dioxide product.
• the main indicators of the obtained manganese dioxide products are Mn0 2 91. 0%, Fe 60 ppm, Cu 5 ppm, Pb 5 ppm, Ni 5 ppm, Co 5 ppm, Mo 0.5 ppm, As 0. 5 ppm, Sb 0. 5 ppm, K. 200ppm.

Landscapes

• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Organic Chemistry (AREA)
• Metallurgy (AREA)
• Materials Engineering (AREA)
• Manufacturing & Machinery (AREA)
• Mechanical Engineering (AREA)
• Life Sciences & Earth Sciences (AREA)
• General Life Sciences & Earth Sciences (AREA)
• Geochemistry & Mineralogy (AREA)
• Geology (AREA)
• Environmental & Geological Engineering (AREA)
• Inorganic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Ocean & Marine Engineering (AREA)
• Oceanography (AREA)
• Electrochemistry (AREA)
• General Chemical & Material Sciences (AREA)
• Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
• Battery Electrode And Active Subsutance (AREA)
• Inorganic Compounds Of Heavy Metals (AREA)
• Manufacture And Refinement Of Metals (AREA)

Priority Applications (2)

Applications Claiming Priority (2)

Publications (1)

Family

ID=43101728

Family Applications (1)

Country Status (4)

Cited By (3)

Families Citing this family (22)

Citations (7)

Family Cites Families (20)

• 2010
  • 2010-07-15 CN CN2010102279887A patent/CN101892384B/zh active Active
• 2011
  • 2011-07-09 US US13/521,952 patent/US20130037416A1/en not_active Abandoned
  • 2011-07-09 WO PCT/CN2011/077011 patent/WO2012006935A1/zh not_active Ceased
  • 2011-07-09 JP JP2013518940A patent/JP5764207B2/ja active Active

Patent Citations (7)

Also Published As

Similar Documents

Legal Events