• 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:
    In a method for manufacturing potassium chloride with a K2O content of 55 wt. % from the fine salt resulting from the decomposition of carnallite, n-alkyl amine salts are used as conditioning agents, and flotation media containing magnesium and potassium chloride are used to separate this fine decomposition salt in an initial flotation stage into a grain size fraction of <0.1 mm as the first pre-concentrate and a residue having a grain size of >0.315. After the conditioning, this residue is again floated and the potassium chloride comes to the surface as a second pre-concentrate. Then the potassium chloride is separated from the mixture of the two pre-concentrates, without any further conditioning, in another flotation stage, and collected.
    公开号:SU1669401A3
    申请号:SU853947358
    申请日:1985-08-30
    公开日:1991-08-07
    发明作者:Хагедорн Фритц；Пойшель Герд；Зингевальд Арно
    申请人:Кали Унд Зальц Аг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the production of potassium chloride with a high content of teO from carnallite or raw ellite potassium salts by flotation.
    The aim of the invention is to simplify the process.
    Potassium chloride with a CaO content of more than 55% by weight, after conditioning with water-soluble salts of long-chain amines, is obtained from the fines fraction obtained during the radiotepy of carnallite or carnellite potassium salts. C. by flotation in the liquor medium containing magnesium chloride and potassium chloride.
    Accordingly, the fine salt from decomposition, after conditioning with 50–200 g of n-alkylamine silicon per 1 ton, is floated, and a fine fraction of 0.1 mm emerges as the first forconcentrate. The residue thus obtained is again concentrated with 50-150 g of n-alkylamine salt per 1 ton and then floated as the potassium chloride is flooded as a second concentrate. After that, both the preconcentrate (primary concentrate) are additionally floated together, and potassium chloride floats up and accumulates.
    Saline solution with MgCte content can be used as a flotation alkali (liquor) carrier. up to 320 g / l, which, for example, is obtained by cold decomposition of carnallite. Particularly suitable were silginogshe
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    liquors with a magnesium chloride content of 70-90 g / l as a lye (alkali) carrier for flotation. These carrier liquors, after separation of the corresponding residues after flotation, can be introduced into the cycle.
    During the cold decomposition of carnallite, the salt, together with the liquor, is passed through sieves and divided into a large fraction with a grain size of more than 1 mm and a small fraction with a grain size of 1 mm and below. The coarse fraction after separation from the liquor is fed to the dissolution, and the fine salt with a particle size (grain) up to 1 mm is also separated from the liquor and used as a starting material in the proposed method. Its content is “20 over 20 wt.%, Preferably about 23-40 wt.%.
    The method is based on the fact that in carrying out the proposed operations at the first flotation stage with a satisfactory result in the flotation process, the fine fraction itself with a grain size less than 0.1 mm emerges and thus can be separated from the larger residue.
    The residue remaining during this flotation contains about 10% by weight foO. It is obtained in an amount that corresponds to about half the amount of decomposition salt used. This residue, together with the carrier liquor, is transferred to the second flotation stage, after 50-150 g of the n-alkylamine salt is added to the mixture from the residue and liquor carrier per ton of residue.
    Both stages of flotation are carried out in conventional devices at ambient temperature.
    In the second stage of flotation, the proportion of grains of potassium chloride contained in the salt after decomposition floats, and the grain size is above 0.1 mm. The resulting residue contains up to 1.5 wt.% KAO. It can be discarded or sent to dissolve.
    The concentrates of the valuable substance obtained at both stages of flotation without further conditioning together undergo additional flotation, from the foam of which the concentrate of KCI is released with foO content above 55% by weight, namely with removal over 90%. Also with additional flotation, a residue is obtained which can contain another 5 to 10% of the amount of CrO used and therefore is preferably fed to the dissolving process.
    Using a combination of the individual stages of the proposed method, it became possible for the first time from the fine decomposition salt produced by the decomposition of carnallite to produce potassium chloride only by flotation with a CaO content of more than 55 wt.
    The mechanical separation and grinding of the larger constituents of the fine decomposition salt is not necessary according to the invention, which simplifies the process.
    Example 1. 1000 kg of finely divided salt with a particle size of 1.0 mm with a content of "2027.8% is subjected to first flotation. 100 g / t of C 18-alkylamine hydrochloride is used as a flotation agent. The first preconcentrate is obtained in the amount of 496.2 kg with a cao content of 45.9%, which corresponds to a teO yield of 82%. The residue in the amount of 503.8 kg with a KAO content of 10%, which corresponds to a yield of K20 of 18%, is subjected to a second flotation. 90 g / t of Cie-alkylamine hydrochloride are used as a flotation agent, to which another 60 g / t of a blowing agent is added. A second concentrate is obtained in the amount of 150.1 kg with a K2O content of 31.2%, which corresponds to a yield of K20 of 16.8%.
    The residue in the amount of 353.7 kg with a content of 20 1%, which corresponds to a yield of 1.2%, is removed from the process. The first and second forconcentrates are combined, yielding 646.3 kg with a content of "20 to 42.5%. This number “20 corresponds to a yield of 98.8%.
    This concentrate is subjected to additional flotation and a concentrate is obtained in the amount of 485.4 kg with a foO content of 55.6% and an intermediate product in the amount of 160.9 kg. The intermediate product has a content of 8.7%, which corresponds to a yield of 4.9%. This amount is fed to the dissolution plant.
    The amount of CrO in the resulting concentrate is 93.9% of its content in the starting material. Saline solutions, which are obtained from the cold decomposition of carnallite, are used as the starting material. The latter contain from 70 to 90 g / l of magnesium chloride.
    EXAMPLE 2. 1000 kg of finely divided salt with a particle size of 1.0 mm and a content of "20 27.8% is subjected to first flotation. 200 g / t Cie-alkylamine hydrochloride are used as a flotation agent. Get the first forconcentrate in the amount of 512.8 kg with toO content of 45.0%, which corresponds to a yield of K20 83%. The residue in the amount of 487.2 kg with the content of “20 9.7%, which corresponds to a yield of CsO of 17%, is subjected to a second flotation. 50 g / t is used as a flotation agent.
    Cie-alkylamine hydrochloride, to which 60 g / t of a blowing agent is further added. A second forcoitseitrate is obtained in the amount of 133.5 kg with a K20 content of 33.0%, which corresponds to a KAO yield of 16.8%. The balance in the amount of 353.7 kg with the content of "ГС 1%, which corresponds to a yield of 1.2%, is removed from the process.
    The first and second forconcentrate are combined, yielding 646.3 kg with a content of "20 to 42.5%. This amount of KAO corresponds to a yield of 98.8%. This concentrate is subjected to additional flotation and a concentrate is obtained in the amount of 485.4 kg with a K20 content of 55.6% and an intermediate product in the amount of 160.9 kg. The intermediate product has a KO content of 8.7%, which corresponds to a yield of 4.9 % This quantity of eoTi o is fed to the installation of the dissolution of r-p-20 in the resulting concentrate.
    equals 93.9% of the content of the -th material.
    EXAMPLE 3. 1000 kg of finely divided salt with a particle size of 0.1 mm and a KAO content of 27.8% is subjected to first flotation. 50 g / t of Cie-alkylamine hydrochloride is used as a flotation agent. Get the first forkononi ntrat in the amount of 437.7 kg with soda. 47.0%. which corresponds to a yield of, j71.0% Balance and quantity, 7 kg with the content of "20 12.8%. which corresponds to a yield of CRO of 26.0%, is subjected to a second flotation. 150 g / t of C18-alkylamine hydrochloride. E are used as a flotation agent. to which another 60 g / t of foam is added, tel. Get the second forconcentrate in the amount of 209.0 kg with a content of KAO 33.0%. which corresponds to the output of KAO 16.8%.
    The residue in the amount of 353.7 kg with a cao 1 content of 1%, which corresponds to a yield of 1.2%, is removed from the process.
    The first and second forconcentrates are combined, yielding 646.3 kg with a cao content of 42.5%. This amount of KAO corresponds to a yield of 98.8%. This concentrate is subjected to an additional product of sci-dium to obtain a concentrate in the amount of 485.4 kg with a K20 content of 55.6% and an intermediate product in the amount of 160.9 KJ. The intermediate product, .ct, has a content of 8.7%, which corresponds to The yield is 4.9%. This amount is fed to the plant installation.
    The content of PP in the resulting concentrate is 93.9% of the content in the. "- walkable material.
    The method allows to simplify the process by eliminating mechanically (ore separation and grinding, as well as combining the flotation of the large and small fraction.
    权利要求:
    Claims (2)
    [1]
    1. A method for separating potassium chloride from carnallite ore, including decomposing it in magnesium chloride liquor, flotation in the presence of water-soluble salts of primary M-alkylamines and separating the fine fraction containing potassium chloride, characterized in that, in order to simplify the process, a fine fraction potassium chloride is subjected to flg. gpiguggii alklaminydro gr "dy t. of this quantity 50 - 200 hl.; Ome pen1, l-or-kgs1, entraz from the particles of hlsrid kalig, -aj less than 9.1 mm from the fraction, the last fleet is injected. 50 - 150 g / t of alkylamine hydrochlorides with forchant concentrate. kru.1 "-: oh Fractions, after casting forconcentrates with two stewlenb f / utation, mix and float together to obtain the desired product in the froth fraction,
    [2]
    2. A method according to P. 1, characterized in that the magnesium-chloride liquor is used with a content of plastic chloride of 70-90 g / l.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1669401A3|1991-08-07|Method for separation potassium chloride out of carnallite ore
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    US3891544A|1975-06-24|Process for the separate recovery of potassium chloride and sodium chloride from a solid mixture thereof
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    US2188932A|1940-02-06|Flotation process for sylvinite ores
    US3640382A|1972-02-08|Flotation concentration of magnesite with emulsified collector reagents
    US2336854A|1943-12-14|Method of treating potassium chloride concentrates
    US4040519A|1977-08-09|Froth flotation process for recovering sheelite
    US2330158A|1943-09-21|Concentration of potash ores
    US2283295A|1942-05-19|Process of purifying glass sands
    US3768738A|1973-10-30|Flotation of arsenic minerals from borate ores
    RU1784617C|1992-12-30|Process for producing potassium fertilizers
    KR930009722B1|1993-10-09|Iron stone refining method
    SU1351911A1|1987-11-15|Method of obtaining potash fertilizer
    SU1710137A1|1992-02-07|Method of floatation of potassium ores
    US2393008A|1946-01-15|Ore concentration
    US1619790A|1927-03-01|Concentration of slimes by flotation
    US2965231A|1960-12-20|Flotation separation of cryolite and fluorite
    US3794159A|1974-02-26|Process for flotation of large size mineral particles
    CA2076216C|1997-10-28|Process for purifying silica sand and other materials
    SU763267A1|1980-09-15|Method of extracting potassium chloride
    US2292503A|1942-08-11|Purification of calcium carbonate
    同族专利:
    公开号 | 公开日
    US5057208A|1991-10-15|
    DD236913A5|1986-06-25|
    DE3435124C2|1987-03-05|
    OA08106A|1987-03-31|
    DE3435124A1|1986-03-27|
    CA1271272A|1990-07-03|
    ES8604470A1|1986-02-01|
    BR8504270A|1986-06-17|
    ES544959A0|1986-02-01|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2733809A|1956-02-07|Separation |
    US2364520A|1943-06-23|1944-12-05|Minerals Separation North Us|Concentration of sylvinite ores|
    US2604988A|1946-07-16|1952-07-29|Mines Domaniales De Potasse|Froth flotation of potassium chloride from sodium chloride|
    US2702121A|1950-01-11|1955-02-15|Public Ets|Methods of froth-flotation|
    DE931702C|1953-03-22|1955-08-16|Verkaufsgemeinschaft Deutscher|Process for the swimming treatment of carnallitic raw or mixed salts|
    US2931502A|1956-07-02|1960-04-05|Saskatchewan Potash|Method for flotation concentration in coarse size range|
    US2999595A|1956-07-02|1961-09-12|Saskatchewan Potash|Apparatus for flotation concentration in coarse size range|
    US2984348A|1958-08-14|1961-05-16|Int Minerals & Chem Corp|Beneficiation of potash ores|
    US3137650A|1961-09-05|1964-06-16|Saskatchewan Potash|Reflotation concentration of sylvite|
    US3259237A|1963-04-22|1966-07-05|Saskatchewan Potash|Phase desliming and concentration of potash ores|
    US3451788A|1965-01-18|1969-06-24|Ideal Basic Ind Inc|Method of slimes elimination in potash ore treatment|
    US3380666A|1965-08-09|1968-04-30|United States Borax Chem|Process for obtaining potash values from potash ore|
    FR1457664A|1965-09-23|1966-01-24|Mines Domaniales De Potasse|Processing of potassium ores|
    US3446443A|1965-12-08|1969-05-27|United States Borax Chem|Process for recovering potash values|
    FR1516906A|1967-01-06|1968-02-05|Mines Domaniales De Potasse|Potassium ores flotation process and new reagents used|
    US3640385A|1969-11-17|1972-02-08|Ideal Basic Ind Inc|Reagents for beneficiating ores|
    US3782546A|1971-12-03|1974-01-01|Calgon Corp|Cationic conditioning agents for potash flotation|
    US4045335A|1976-03-10|1977-08-30|Duval Corporation|Beneficiation of kieserite and langbeinite from a langbeinite ore|
    US4198288A|1979-03-22|1980-04-15|Celanese Polymer Specialties Company|Desliming of potash ores|
    FR2501181B1|1981-03-05|1984-02-17|Mdpa|
    CA1211235A|1983-11-22|1986-09-09|Richard R. Tamosiunis|Process for the flotation of insol from potash ore|DE4200810C2|1992-01-15|1994-05-05|Kali & Salz Ag|Process for increasing the yield of potassium salt flotation|
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    DE4416261C1|1994-05-07|1995-06-01|Kali & Salz Ag|Unstirred pneumatic flotation of poorly hydrophobic salts|
    CN1083801C|1997-01-14|2002-05-01|中国科学院海洋研究所|Process for preparing salt by working up seawater|
    CN1052705C|1997-03-13|2000-05-24|青海盐湖工业集团有限公司|Process for producing potassium chloride from carnallite|
    CN1094466C|1999-01-04|2002-11-20|化学工业部连云港设计研究院|Method of extracting potassium chloride from mixed ore of sylvine and carnallite|
    CN101905895A|2010-08-10|2010-12-08|山西大学|Method for producing potassium chloride by using sylvite as raw material|
    CN102008999B|2010-10-26|2012-08-01|化工部长沙设计研究院|Process for extracting potassium chloride from native sylvite ore|
    CN102198429B|2011-02-22|2013-01-09|化工部长沙设计研究院|Flotation desliming process for solid sylvite mineral containing slime|
    WO2013074328A1|2011-11-14|2013-05-23|Intercontinential Potash Corp. |Methods of processing polyhalite ore, methods of producing potassium sulfate, and related systems|
    WO2014043118A1|2012-09-12|2014-03-20|Intercontinental Potash Corporation|Methods of processing potassium sulfate and magnesium sulfate, and related systems|
    CN102963912B|2012-12-25|2014-08-27|中蓝连海设计研究院|Process for producing potassium chloride by using potassic salt ores|
    CN103145152B|2013-04-11|2013-11-13|中蓝连海设计研究院|Process for extracting potassium chloride by coarse flotation of primary sylvine ores|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3435124A|DE3435124C2|1984-09-25|1984-09-25|
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