• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A hydrometallurgical process for the treatment of a raw material which contains iron and other metals, with a sulfuric acid solution, in order to dissolve the metals and to precipitate and separate the iron, the separated metal sulfate solution being exposed to evaporation in order to crystallize and separate the metal sulfates from the mother liquor, which is recycled to the treatment stage performed with sulfuric acid solution, and the separated metal sulfate being recovered.
    公开号:SU1165238A3
    申请号:SU782690956
    申请日:1978-11-28
    公开日:1985-06-30
    发明作者:Калеви Растас Юсси；Педер Фуглеберг Сигмунд；Олави Хеймала Септо；Хальтхольм Стиг-Эрик；Тейе Илмари Пойярви Яакко
    申请人:Оутокумпу Ой (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to hydrometallurgy of non-ferrous metals, in particular to methods of processing cf containing non-ferrous metals and iron. in the pre-neutralization stage, the free acid is neutralized up to the point of rosite precipitation with the calcine, which complicates the process. In addition, the insoluble components of the calcined product remaining in the rosite sediment contaminate the precipitate and such raw materials are not suitable for the production of iron. Sludge must be supplied to the washing site, while heavy metals (zinc, cadmium, copper) dissolved in water are a 1bt hazard to the environment. The method of hydrometallurgical processing of raw materials containing non-ferrous metals and iron, including leaching of the raw material with a solution of sulfuric acid at elevated temperatures, separation of the solution and its purification from iron and other impurities, followed by processing of the products obtained by known methods and returning the circulating acid to leaching stage 2. However, when using this method, it is not possible to avoid the loss of valuable metals and a significant amount of contaminant waste is generated in the process. The purpose of the invention is to protect the environment from harmful production waste. The goal is achieved by the method of hydrometallurgical processing of raw materials containing non-ferrous metals and iron, including leaching the raw material with a solution of sulfuric acid at elevated temperatures, separating the solution and cleaning it from iron and other impurities by processing the obtained limestone products and returning the circulating acid to the alkalization stage, the solution after purification from iron is subjected to extra-crystallization and the resulting metal sulphates are separated from the mother liquor. solution. Iron removal is carried out in an autoclave at 140-250 ° C and a concentration of sulfuric acid in a solution of 5-150 g / l, and leaching of zinc-containing sf with a solution of sulfuric acid is carried out in the presence of ammonium ions or alkali. The advantage of this method is to trace. After leaching with a strong: acid (50-100 g / l of sulfuric acid), the solution is fed without neutralization into an autoclave, where most of the iron present in the solution is present in the form of basic sulphate (). Then the solution is scorched and cooled, while the metal sulfates are removed from the solution. After the salt has been separated, the mother liquor is returned to the leaching stage with a strong acid. The acid of the mother liquor is used to leach the starting material and, after leaching, the iron remaining in the solution circulates with the iron dissolved from the raw material into the autoclave, where most of the iron is released. During the course of crystallization — the crystallization of most of the non-ferrous metals contained in the solution is in the form of a salt. Salt, almost free of acid and iron, is obtained by washing. After that, the salt should be dissolved in water and neutralized with a small amount of neutralizing agent. The neutralized solution is then fed to the purification step and then to electrolysis. The concentration of iron in the solution fed to the autoclave is 100 g / l more. Since iron circulates in a cycle, it is not necessary to completely separate it from the solution. The amount of iron excreted in one process cycle is 70-80 g / l. Selected iron is subjected to thermal decomposition, which. carried out at 650-750 ° C and using coal or pyrite. The iron salt decomposes to form hematics and gaseous sulfur oxides. The gas is supplied to the waste heat boiler.
    and then through the gas cleaning stage, to a sulfuric acid treatment unit.
    The ferrous iron can be subjected to thermal decomposition or ground to work.
    At the stage of aiming, it is possible to use both working acid after electrolysis and pure acid diluted with water.
    P r and I r. Ferrite raw materials with Content,%: zinc 14.2; copper 7, lead 16.1j iron 32.5j silver 300 and gold 30 ppm, were fed at a rate of 308 kg / h to the leaching stage. The leaching time was 6 hours and the temperature was 95 ° C. The concentration of sulfuric acid in the solution at the end of the leach is 90 g / l. After clarification, the solution was separated from the solid residue. The composition of the washed and dried residue: lead 49.8, silver 970 and gold 102 parts per million; The concentration of iron in the solution, going to the aktoklav to distribute iron, was 62.6 g / l copper 16 g / l and zinc - 61 g / l. The iron separation was carried out at 205 ° C for 2 hours. The isolated iron was separated (from the solution. The iron release rate was 307 kg / h and its concentration was 32.5%. The sulfuric acid concentration in the solution fed by evaporation-crystallization, Soil was 127 g / l and iron was 21 g / l. The temperature at the Evaporation crystallization stage is 74 ° C. The concentration of zinc, copper and iron in the separated and slightly washed solid phase was respectively%: 25.0, 6.1 and 0.7. The feed rate of the solution from the Evaporation-crystalline stage 1 after separation of the crystals The leaching stage with a strong acid was 0.89, and the concentration in a solution of sulfuric acid, iron, zinc and copper, respectively, g / l: 437, 54, 65 and 18.5. The crystalline residue was leached in water, the pH of the solution was regulated by the addition of the product of roasting zinc in the range of 2-3.
    The concentration of zinc in a solution free from solid particles was 131 g / l, copper - 29.3 g / l. Copper Separated from the solution by cementation
    on zinc powder. The solution, free from copper, after additional purification was subjected to electrolysis. The yield of zinc and copper from the process was 99.7 and 99.8%, respectively.
    Example 2. 1000 kg of zinc calcine was fed to a leaching stage with a neutral solvent. The composition of the product of roasting zinc,%: zinc 58,0; iron 10.0 lead 3.0; cadmium 0.22, copper 0.54; silver 0.0085.
    Leaching time 2 hours at a pH of 2.5. Particles and solution separated. The composition of the solid,%: zinc 17.0; iron 19.5, lead 5.3, Solid was applied to the final stage of leaching with a strong acid. Leaching time 10 h, temperature 95 ° C. The concentration of sulfuric acid at the end of the leach is 80 g / l. The solid and solution separated. The lead concentration in the washed and dried leach residue is 4.5, and that of silver is 0.13%. The composition of the solution supplied to the autoclave for the release of iron: hshna 99 and iron 100 g / l. The iron was precipitated at 200 ° C for 2 hours. The deposition of iron was separated from the solution. The amount of washed and dried iron was 3.5 kg, and the iron concentration in it was 32.7%. The concentration of sulfuric acid in the solution supplied from the autoclave for evaporation-crystallization was 151 g / d, the concentration of iron was 20.5, zinc 100 g / l. At the evaporation-crystallization stage, 2 m of circulating acid with a concentration of sulfuric acid 180 and zinc of 60 g / l was supplied. The final temperature in the evaporation crystallization step. The composition of the precipitate separated by crystallization,% t zinc 23.4; iron 1.1, sulfuric acid 18.5. Unwashed crystals were applied to a neutral solution. Uterine
    the solution from the stage of% crystallization with a content of 690 g / l of sulfuric acid, 40.6 g / l of zinc and. 22.3 g / l of iron in the amount of 0.76 m was converted to the extrusion stage with a strong acid. The iron implanted in the autoclave was thermally decomposed at 710 s. The resulting SO2 gas was fed to the smelter, and the resulting hematite was washed with water .. and the filters were separated 51165238
    by niem. Wash water was supplied at a stagnant value and dangerous for
    The day of neutralization with a neutral solution of the surrounding medium does not form. The boarder. Sucking neutral leach from strong leaching of oxygen, after cleaning it was applied natoy can be used as raw material.
    Zinc electrolysis. Zinc output from pro 5c. another process (for example, in a process of 99.6%,. all the production of lead), and washed
    Compared to the known precursors, the iron oxide (obtained in the resultant method has the following advantage of thermal decomposition, hydrothermal decomposition or processing
    The need to neutralize Justification) can be used
    small and precipitation, not having a pro-for iron.
    权利要求:
    Claims (3)
    [1]
    1 1. METHOD FOR HYDROMETALLURGICAL PROCESSING OF RAW MATERIALS CONTAINING TH FOUR NON-FERROUS METALS AND IRON, including
    I leaching of raw materials with a solution; sulfuric acid at an elevated temperature, separation of the solution and its purification from iron and other impurities, followed by processing of the obtained products by known methods and · returning the circulating acid to the leaching stage, characterized in that, in order to protect the environment from harmful production wastes, the solution after purification from iron is subjected to evaporation-crystallization and the resulting metal sulfates are separated from the mother liquor.
    [2]
    2. The method of pop. 1, characterized in that the leaching of zinc-containing raw material solution 1 sulfuric acid is carried out in the presence of alkali ions or atony.
    [3]
    3. The method according to p. 1, about t l and h a yu. and the fact that the purification of iron is carried out in an autoclave at 140-250 C and the concentration of sulfuric acid in solution 5-150 g / l.
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    同族专利:
    公开号 | 公开日
    AU4190478A|1979-06-07|
    CA1112880A|1981-11-24|
    JPS612735B2|1986-01-27|
    BR7807787A|1979-07-24|
    YU278878A|1982-06-30|
    PL115840B1|1981-05-30|
    JPS54106003A|1979-08-20|
    DE2850644C2|1984-05-03|
    FI773588A|1979-05-29|
    AU525034B2|1982-10-14|
    DE2850644A1|1979-05-31|
    US4219354A|1980-08-26|
    CS223805B2|1983-11-25|
    PL211282A1|1979-08-27|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE556321C|1926-10-08|1932-08-06|Metallgesellschaft Ag|Process for the production of pure zinc sulphate from alkalis containing zinc sulphate and sodium sulphate|
    US1834960A|1930-04-25|1931-12-08|Anaconda Copper Mining Co|Treating zinc concentrate and plant residue|
    US2599816A|1948-09-22|1952-06-10|Ellsworth Mildred|Purification of zinc electrolytes|
    US3493365A|1965-03-31|1970-02-03|Electrolyt Zinc Australasia|Treatment of zinc plant residue|
    BE673023A|1965-04-30|1900-01-01|
    US3753692A|1969-08-20|1973-08-21|Ici Australia Ltd|A process for the coproduction of zinc and sulphuric acid from zinc sulphide ores|
    NO123248B|1969-10-02|1971-10-18|Norske Zinkkompani As|
    US3676107A|1971-01-04|1972-07-11|Us Interior|Refining iron-bearing wastes|
    ES407811A2|1972-10-20|1976-02-01|Asturiana De Zinc Sa|Process for recovering zinc from ferrites|
    FI50141C|1973-02-01|1975-12-10|Outokumpu Oy|Process for producing a raw material suitable for iron production from a precipitate derived from electrolytic zinc production.|
    FI50097C|1973-02-12|1980-10-24|Outokumpu Oy|HYDROMETALLURGICAL FOERFARANDE FOER AOTERVINNING AV ZINK KOPPAR OCH CADMIUM FRAON DERAS FERRITER|
    US3933478A|1973-08-27|1976-01-20|Nicosep Associates|Recovery of zinc and copper from brass scrap|
    GB1509537A|1974-09-13|1978-05-04|Cominco Ltd|Treatment of zinc plant residues|ZW3481A1|1980-02-18|1981-05-20|Nat Inst Metallurg|The leaching of sulphidic mattes containing non-ferrous metals and iron|
    FI64646C|1980-06-19|1983-12-12|Outokumpu Oy|HYDROMETALLURGICAL FOERFARANDE FOER UTVINNING AV VAERDEMETALLER UR METALLISKA LEGERINGAR|
    MX157259A|1980-09-30|1988-11-09|Outokumpu Oy|IMPROVED HYDROMETALLURGICAL METHOD FOR TREATING A RAW MATERIAL CONTAINING OXIDE AND FERRITE OF ZINC, COPPER AND CADMIUM|
    FI65810C|1980-09-30|1984-07-10|Outokumpu Oy|FOERFARANDE FOER BEHANDLING AV RAOMATERIAL INNEHAOLLANDE OXID OCH FERRIT AV ZINK KOPPAR OCH KADMIUM|
    ES8204696A1|1981-07-24|1982-05-16|Martin San Lorenzo Daniel|Process for the production of electrolytic zinc or high purity zinc salts from secondary zinc raw-materials|
    US4979987A|1988-07-19|1990-12-25|First Miss Gold, Inc.|Precious metals recovery from refractory carbonate ores|
    FR2634751B1|1988-07-29|1991-02-08|Metaleurop Sa|
    US5188713A|1991-03-05|1993-02-23|Envirochip Technologies Ltd.|Process for recovery of metal|
    US5401485A|1994-03-15|1995-03-28|Shell Oil Company|Reduction of residual chloride in iron oxides|
    US5788740A|1995-03-06|1998-08-04|Bay Zinc Company, Inc.|Method for the hydrometallurgical separation and recovery of biological nutrients, lead, gypsum and cadmium from raw materials|
    US20060002835A1|2004-06-28|2006-01-05|David Neudorf|Method for nickel and cobalt recovery from laterite ores by reaction with concentrated acid and water leaching|
    US7604783B2|2004-12-22|2009-10-20|Placer Dome Technical Services Limited|Reduction of lime consumption when treating refractor gold ores or concentrates|
    US8061888B2|2006-03-17|2011-11-22|Barrick Gold Corporation|Autoclave with underflow dividers|
    US8252254B2|2006-06-15|2012-08-28|Barrick Gold Corporation|Process for reduced alkali consumption in the recovery of silver|
    LU91509B1|2008-12-22|2010-06-24|Wurth Paul Sa|Valorization of secondary zinc oxides rich in fluorides and chlorides|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FI773588A|FI773588A|1977-11-28|1977-11-28|HYDROMETALLURGICAL PROCESS FOR BEHANDLING AV OXIDER OCH FERRITER INNEHAOLLANDE JAERN OCH ANDRA METALLER|
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