WO2020177159A1 - 一种可回收利用副产物的生产氯化钾的方法和系统 - Google Patents

一种可回收利用副产物的生产氯化钾的方法和系统 Download PDF

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Publication number
WO2020177159A1
WO2020177159A1 PCT/CN2019/079266 CN2019079266W WO2020177159A1 WO 2020177159 A1 WO2020177159 A1 WO 2020177159A1 CN 2019079266 W CN2019079266 W CN 2019079266W WO 2020177159 A1 WO2020177159 A1 WO 2020177159A1
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Prior art keywords
slurry
potassium
underflow
sodium
low
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PCT/CN2019/079266
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English (en)
French (fr)
Inventor
李小松
王兴富
谢康民
王石军
黄龙
俞秋平
赵元海
张振杰
田红斌
张生太
任红伟
于建国
宋兴福
海吉忠
于雪峰
史忠录
屈小荣
李建业
任青峰
郝红军
蒋中华
孟浩
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青海盐湖工业股份有限公司
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Priority to EA202191773A priority Critical patent/EA202191773A1/ru
Priority to BR112021009024-0A priority patent/BR112021009024A2/pt
Publication of WO2020177159A1 publication Critical patent/WO2020177159A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C01D3/06—Preparation by working up brines; seawater or spent lyes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B9/00—General methods of preparing halides
    • C01B9/02—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C01D3/08—Preparation by working up natural or industrial salt mixtures or siliceous minerals
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/14—Purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/26—Magnesium halides
    • C01F5/30—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/26—Magnesium halides
    • C01F5/30—Chlorides
    • C01F5/305—Dehydrating ammonium or alkali magnesium chlorides, e.g. carnalite
    • 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
    • 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
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • 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 present invention generally relates to the field of potassium chloride production, and more specifically, to a method and system for producing potassium chloride that can recycle by-products.
  • the existing methods of using salt lake brine to produce potassium chloride mainly include cold crystallization-positive flotation process, hot-melt crystallization process, reverse flotation-cold crystallization process, halogenated salt process, etc. or a combination of the above-mentioned processes .
  • the reverse flotation-cold crystallization process is widely used, but the process requires high quality of raw carnallite. It is suitable to be produced from salt field carnallite ore. The input is large, the energy consumption is large, and the final product is potassium chloride. The grade can only reach about 95%.
  • the potassium chloride contained in the by-products produced is insufficient in the recycling process, resulting in a large amount of potassium chloride being discharged along with the tail salt, which wastes potassium resources.
  • the by-products in potash fertilizer production should be combined with internal utilization and external utilization, and the potassium chloride in the raw materials should be extracted as much as possible to increase potash fertilizer. Yield and efficiency, in addition, improve the connection and combination of equipment to facilitate continuous production, without affecting the overall process due to individual equipment failures.
  • the problem solved by the present invention is to provide a method and system for producing potassium chloride that can recycle by-products.
  • the invention provides a system for producing potassium chloride that can recycle by-products, including a raw ore processing system 1, a slurry conditioning system 2, a flotation system 3, a low-sodium concentration and dehalogenation system 4, cold crystallization and crude potassium Screening system 5, coarse potassium concentration and dehalogenation system 6, refined potassium washing and dehalogenation system 7, and also includes overflow and filtrate treatment system 8, said raw ore treatment system 1 is used to screen carnallite pulp And concentration to obtain a first underflow slurry and a first overflow liquid; the slurry mixing system 2 is connected to the raw ore processing system 1 for mixing the flotation reagent with the first underflow slurry to obtain a slurry Pulp; The flotation system 3 is used to perform flotation operations on the adjusted slurry slurry to obtain tail salt and low-sodium carnallite slurry; the low-sodium concentration and dehalogenation system 4 and the flotation system 3 Connected, used for concentrating the low-sodium carnal
  • the overflow and filtrate treatment system 8 includes a first treatment system 81, a second treatment system 82, and a third treatment system 83, and the first treatment system 81 is separately from the raw ore treatment system.
  • the system 1, the flotation system 3 are connected, and are used to receive the first overflow liquid from the raw ore processing system 1, and receive the flotation tail salt from the flotation system 3, and combine the first overflow liquid with the flotation system.
  • the tail salt is selected for slurrying and then discharged;
  • the second processing system 82 is respectively connected with the cold crystallization and coarse potassium screening system 5 and the refined potassium washing and dehalogenation system 7 for removing the cold crystallization and coarse potassium
  • the screening system 5 receives the third overflow liquid, and receives the fifth overflow liquid from the refined potassium washing and dehalogenation system 7, and after being adjusted by fresh water, it is transported to the cold crystallization and coarse potassium screening system 5 as the decomposition mother liquor;
  • the third processing system 83 is connected to the low-sodium concentration and dehalogenation system 4 for receiving the first filtrate, concentrating and filtering the first filtrate, and recovering carnallite.
  • the first processing system (81) further includes a primary sweeping tank 811, a secondary sweeping tank 812, and a storage tank 813, the primary sweeping tank 811 is connected to the flotation system , Used to receive flotation tailings and perform primary sweeping to obtain primary sweeping froth and primary sweeping underflow; the secondary sweeping tank 812 is connected to the primary sweeping tank 811 for receiving the primary Sweeping the underflow and performing secondary sweeping to obtain secondary sweeping foam and secondary sweeping underflow; the primary sweeping tank 811 is connected to the tailing salt pond, and is used to transport the primary sweeping foam to the tailing salt pond The secondary scavenging tank 812 is connected to the storage tank 813, and is used to transport the secondary scavenging underflow to the storage tank 813; the secondary scavenging tank 812 and the low sodium concentration and The dehalogenation system is connected to transport the secondary sweeping bottom stream to the low sodium concentration and dehalogenation system.
  • the primary sweeping tank 811 is connected to
  • the low-sodium concentration and dehalogenation system 4 is connected to the flotation system 3, and is used to transport the second overflow liquid to the flotation system 3 for adjusting The consistency of the slurry.
  • the crude potassium concentration and dehalogenation system 6 is connected to the raw ore processing system 1 for sending the fourth overflow liquid to the raw ore processing system 1 for concentration and utilization.
  • the raw ore processing system 1 includes a carnallite screening machine 11, a raw ore thickener 12, and the carnallite screening machine 11 is used to screen out impurities and large particles in the carnallite slurry Salt to obtain the under-screen product; the raw ore thickener 12 is connected to the carnallite screening machine 11 for concentrating the under-screen product to obtain the first overflow liquid and the first underflow slurry, so that the second The solid mass content of an underflow slurry: 30-45%, and the number of the raw ore thickener 12 is one or more.
  • the slurry mixing system 2 includes a slurry distribution tank 21 and a slurry tank 22.
  • the slurry distribution tank 21 includes a plurality of raw ore thickeners 12 interfaces for connecting with a plurality of raw ore thickeners. 12 connection, receiving the first underflow slurry, mixing the first underflow slurry with the flotation agent, and distributing the first underflow slurry and the flotation agent to the slurry tank 22;
  • the slurry tank 22 is connected to the slurry distribution tank 21 and is used to uniformly mix the first underflow slurry and the flotation agent to obtain a slurry slurry.
  • the flotation system 3 includes a flotation distribution tank 31 and a flotation machine 32.
  • the flotation distribution tank 31 is connected to the slurry adjustment system 2 and is used to receive the slurry slurry. , And adjust the concentration of the adjusted slurry by adding the adjusted mother liquor to obtain the adjusted slurry; the solid mass content of the adjusted slurry is 20%-25%; the adjusted mother liquor refers to the same components as the slurry mother liquor.
  • the liquid phase; the flotation machine 32 is connected to the flotation distribution tank 31, and is used for roughing, beneficiating and sweeping the conditioning slurry to obtain tailings and low-sodium carnallite slurry;
  • the flotation machine 32 is one or more.
  • the low-sodium concentration and dehalogenation system 4 includes a low-sodium thickener 41, a low-sodium centrifuge distribution tank 42, and a low-sodium centrifuge 43, and the low-sodium thickener 41 is used to receive Sodium carnallite pulp and the low-sodium carnallite pulp are concentrated to obtain a second underflow pulp and a second overflow liquid; the solid mass content of the second underflow pulp is 40%-45%; the low sodium There are one or more thickeners 41; the low-sodium centrifuge distribution tank 42 is connected to the low-sodium thickener 41, and is used to receive the second underflow slurry and distribute the second underflow slurry to the low-sodium centrifuge The machine 43; the low-sodium centrifuge 43 is one or more, connected to the low-sodium centrifuge distribution tank 42, for dehalogenating the second underflow slurry to obtain a first filtrate and moisture
  • the cold crystallization and coarse potassium screening system 5 includes a crystallizer 51 and a coarse potassium screening machine 52.
  • crystallizers 51 for receiving the moisture content ⁇ 10 % Low-sodium carnallite ore and decomposed and crystallized to obtain the third underflow slurry and the third overflow liquid; the solid mass content of the third underflow slurry was 15%-30%; the coarse potassium screening machine 52 and the crystallizer
  • the 51 connection is used to screen the third underflow slurry to obtain the coarse potassium sieve and coarse potassium sieve.
  • the crude potassium concentration and dehalogenation system 6 includes a crude potassium thickener 61, a crude potassium centrifuge distribution tank 62, and a crude potassium centrifuge 63.
  • the crude potassium thickener 61 is one or more One, for receiving and concentrating the crude potassium under sieve to obtain the fourth overflow liquid and the fourth underflow slurry; the solid mass content of the fourth underflow slurry is 40%-45%; the crude potassium centrifuge
  • the distribution tank 62 is connected to the coarse potassium thickener 61, and is used to receive the fourth underflow slurry and distribute the fourth underflow slurry to each coarse potassium centrifuge 63; the coarse potassium centrifuge 63 is One or more are connected to the coarse potassium centrifuge distribution tank 62, and are used for dehalogenating the fourth underflow slurry to obtain a second filtrate and coarse potassium ore with a moisture content of ⁇ 10%.
  • the crude potassium centrifuge 63 is connected to the crude potassium thickener 61 and is used to transport the second filtrate to the crude potassium thickener 61 for recycling.
  • the refined potassium washing and dehalogenation system 7 includes a repulp washing tank 71, a refined potassium thickener 72, and a refined potassium centrifuge 73.
  • the repulp washing tank 71 is one or more, It is used to receive the crude potash ore with moisture content ⁇ 10% and wash it to obtain a repulp washing slurry; there are one or more refined potassium thickeners 72 which are matched with the repulp washing tank and are used to concentrate the repulp washing The slurry is washed to obtain a fifth underflow slurry; there are one or more refined potassium centrifuges 73, which are matched with the refined potassium thickener 72, and are used for dehalogenating the fifth underflow slurry to obtain refined potassium Ore and the third filtrate; the moisture content of the concentrated potash ore ⁇ 10%.
  • the refined potassium thickener 72 is connected to the repulp washing tank, and is used to adjust the concentration of the coarse potassium ore with moisture content ⁇ 10% by using the fifth underflow slurry.
  • the refined potassium thickener 72 is connected to the refined potassium centrifuge 73, and is used to recover the third filtrate to the refined potassium thickener 72 for concentration.
  • a method for producing potassium chloride that can recycle by-products.
  • the method includes, in the first step S1, screening and concentrating carnallite pulp to obtain a first underflow pulp and a first Overflow liquid; the second step S2, mixing the flotation reagent with the first underflow slurry to obtain a mixed slurry; the third step S3, perform flotation operations on the mixed slurry to obtain tail salt and Low-sodium carnallite slurry; the fourth step S4, the low-sodium carnallite slurry is concentrated and the brine is removed to obtain the second overflow liquid, the first filtrate and the low-sodium carnallite ore with a moisture content of ⁇ 10% The fifth step S5, decompose and crystallize the low-sodium carnallite ore with a moisture content of ⁇ 10%, and screen to obtain the third overflow liquid, the coarse potassium sieve and the coarse potassium sieve; Step S6: Concentrate and dehalogenate
  • the eighth step S8 includes mixing the first overflow liquid with the flotation tail salt and then discharging; receiving the third overflow liquid and the fifth overflow liquid, After being adjusted by fresh water, it is used as the decomposition mother liquor of the crystallization process; the first filtrate is received, and the first filtrate is concentrated and filtered to recover carnallite.
  • the method further includes performing primary sweeping of the flotation tailings to obtain primary sweeping foam and primary sweeping underflow; performing secondary sweeping on the primary sweeping underflow to obtain secondary Sweeping foam and secondary sweeping underflow; mixing the primary sweeping foam and the first overflow liquid and then transporting to the tail salt pond; sending the secondary sweeping underflow to the low-sodium concentration and dehalogenation system.
  • the second overflow liquid is used to adjust the concentration of the mixed slurry.
  • the fourth overflow liquid is used for the preparation of carnallite pulp.
  • the first step S1 includes screening out impurities and large-particle salt in the carnallite slurry to obtain an undersize product; and concentrating the undersize product to obtain a first overflow liquid And the first underflow slurry, so that the solid mass content of the first underflow slurry is 30%-45%; the solid mass content of the carnallite slurry is ⁇ 25%.
  • the second step S2 includes mixing the first underflow slurry with a flotation agent, and distributing the first underflow slurry and the flotation agent; The first underflow slurry and the flotation agent are uniformly mixed to obtain a mixed slurry.
  • the third step S3 includes adjusting the concentration of the adjusted slurry by adding a adjusted mother liquor to obtain a adjusted slurry; the solid mass content of the adjusted slurry is 20%-25%
  • the adjustment mother liquor refers to the liquid phase of the same composition as the slurry mother liquor; the adjustment slurry is subjected to rough selection, beneficiation and sweep selection operations to obtain tailings and low-sodium carnallite slurry.
  • the fourth step S4 includes concentrating the low-sodium carnallite slurry to obtain a second underflow slurry and a second overflow liquid; the solid mass content of the second underflow slurry is 40%-45%; distributing the second underflow slurry; dehalogenating the second underflow slurry to obtain a first filtrate and a low sodium carnallite ore with a moisture content of ⁇ 10%.
  • the fifth step S5 includes mixing the low-sodium carnallite ore with a moisture content of ⁇ 10% and the decomposition mother liquor to perform speed-controlled decomposition and crystallization to obtain a third underflow slurry and a third overflow
  • the solid mass content of the third underflow slurry is 15%-30%; the third underflow slurry is subjected to a screening operation to obtain a coarse potassium sieve and a coarse potassium sieve.
  • the sixth step S6 includes concentrating the crude potassium underflow to obtain a fourth overflow liquid and a fourth underflow slurry; the solid content of the fourth underflow slurry is 40% ⁇ 45%; the fourth underflow slurry is distributed; the fourth underflow slurry is dehalogenated to obtain a second filtrate and a crude potash ore with a moisture content of ⁇ 10%.
  • the second filtrate is transported to the process of concentrating the crude potassium undersize for recycling.
  • the seventh step S7 includes washing the crude potassium ore with moisture content ⁇ 10% to obtain a re-slurry washing slurry; concentrating the re-slurry washing slurry to obtain a fifth underflow slurry; The fifth underflow slurry is dehalogenated to obtain the potash concentrate and the third filtrate; the moisture content of the potash concentrate is less than or equal to 10%.
  • the fifth underflow slurry is used to adjust the concentration of the crude potash with moisture content ⁇ 10% in the repulp washing step; the third filtrate is recovered to the repulp washing slurry concentration step to perform concentrate.
  • the invention collects and reuses the first overflow liquid, the third overflow liquid, the fifth overflow liquid and the first filtrate into the system respectively, recovers potassium chloride in the system, and replaces the addition of foreign materials. On the one hand, the yield of potassium chloride is increased, and on the other hand, the cost is saved.
  • multiple devices such as the raw ore thickener 12, flotation machine 32, and low sodium thickener 41 are connected in parallel, and the mixing tank 22 is uniformly mixed with slurry, dispersed and distributed, so that the processing concentration of the material is unified, and each is connected in parallel.
  • the equipment has a standby relationship with each other, even if a certain equipment fails or needs maintenance, it will not affect the operation of the overall process.
  • Figure 1 is a schematic diagram of a system for producing potassium chloride that can recycle by-products
  • Figure 2 is a schematic diagram of the overflow and filtrate treatment system
  • Figure 3 is another schematic diagram of the first processing system
  • Figure 4 is a schematic diagram of the raw ore processing system
  • Figure 5 is a schematic diagram of the mixing system
  • Figure 6 is a schematic diagram of the flotation system
  • Figure 7 is a schematic diagram of a low-sodium concentration and dehalogenation system
  • Figure 8 is a schematic diagram of the cold crystallization and coarse potassium screening system
  • Figure 9 is a schematic diagram of the crude potassium concentration and dehalogenation system
  • Figure 10 is a schematic diagram of the refined potassium washing and dehalogenation system.
  • Figure 11 is a schematic diagram of the steps of a method for producing potassium chloride that can recycle by-products.
  • Figure 1 shows a schematic diagram of a potassium chloride production system that can recycle by-products.
  • a system for producing potassium chloride that can recycle by-products includes raw ore processing system 1, pulping system 2, flotation system 3, low sodium concentration and dehalogenation system 4, cold crystallization and The crude potassium screening system 5, the crude potassium concentration and dehalogenation system 6, the refined potassium washing and dehalogenation system 7, and also the overflow and filtrate treatment system 8.
  • the raw ore treatment system 1 is used to process carnallite pulp Screening and concentrating to obtain the first underflow slurry and the first overflow liquid;
  • the slurry conditioning system 2 is connected to the raw ore processing system 1 and is used to mix the flotation reagent with the first underflow slurry to obtain a conditioning Slurry;
  • the flotation system 3 is used to perform flotation operations on the adjusted slurry to obtain tailings and low-sodium carnallite slurry;
  • the low-sodium concentration and dehalogenation system 4 and the flotation System 3 is connected for concentrating the low-sodium carnallite slurry and removing brine to obtain the second overflow liquid, the first filtrate and the low-sodium carnallite ore with a moisture content of ⁇ 10%;
  • the coarse potassium screening system 5 is connected to the low-sodium concentration and dehalogenation system 4, and is used to decompose and crystallize the low-sodium car
  • the invention uses carnallite produced in salt fields as raw materials to produce potassium chloride.
  • the main components of carnallite harvested from salt fields are potassium chloride, sodium chloride and magnesium chloride.
  • the concentration of carnallite pulp is adjusted to make carnallite pulp The solid mass content of ⁇ 25%.
  • the carnallite ore pulp passes through the carnallite screening machine 11 to screen out impurities and large-particle salt, and the under-screen material is transported to the raw ore thickener 12 for concentration, to obtain the first underflow slurry and the first overflow liquid.
  • the solid mass content of the first underflow slurry is in the range of 30-45%.
  • the first overflow liquid enters the overflow liquid and filtrate treatment system 8 for processing.
  • the first underflow slurry enters the slurry mixing system 2, adds a flotation agent according to the solid mass content in the slurry, and mixes the two uniformly by means such as stirring to obtain a slurry slurry.
  • the first underflow slurry and the flotation agent are fully mixed uniformly, so that the sodium flotation agent can fully contact with sodium chloride in the flotation process, and the flotation efficiency can be increased.
  • the flotation agent is a sodium chloride collector. Before the slurry slurry enters the flotation device, its concentration needs to be adjusted to make its solid mass content : 20% ⁇ 25%, further control the flotation efficiency.
  • the sodium chloride solid and the flotation reagent are combined to form a foam, which is discharged from the flotation system 3 as a tail salt, and a low-sodium carnallite slurry is also obtained.
  • the main components of the low-sodium carnallite slurry are potassium chloride, magnesium chloride, and a small amount of sodium chloride.
  • the low-sodium carnallite slurry is first concentrated in the low-sodium concentration and dehalogenation system 4 so that its solid mass content reaches 40%-45%, and the second overflow liquid is obtained by concentration.
  • the liquid is mainly a solution containing magnesium chloride, which is then subjected to centrifugal dehalogenation, and finally a first filtrate and a low sodium carnallite ore with a moisture content of ⁇ 10% are obtained.
  • the second overflow liquid can be used in the flotation system 3 as the adjustment of the slurry concentration, and the first filtrate is recycled using the overflow liquid and filtrate treatment system 8 with a moisture content of ⁇ 10% low sodium photohalide The quarry enters the next step.
  • the low-sodium carnallite ore with moisture content ⁇ 10% is transported to the cold crystallization and coarse potassium screening system 5, and the mother liquor is decomposed and then crystallized to control the potassium chloride supersaturation in the solution and reduce the number of potassium chloride crystals. It achieves the purpose of making potassium chloride crystals grow up at room temperature, while sodium chloride cannot be precipitated in an unsaturated state, ensuring the quality and particle size of potassium chloride products. Then the sieving operation is carried out, the undecomposed coarse-grained carnallite is returned to the crystallizer 51 to be decomposed again, and the coarse potassium sieve goes to the next step.
  • a third overflow liquid and a third underflow slurry are produced, and the third overflow liquid is used in the overflow liquid and filtrate treatment system 8 for recycling, and is used to synthesize the decomposition mother liquor.
  • the solid mass content of the third underflow slurry is 17-27%, mainly undecomposed coarse-grain carnallite and fine-grain potassium chloride.
  • the third underflow slurry is sieved to obtain the coarse potassium sieve and the coarse potassium sieve.
  • the coarse potassium sieve is returned to the crystallizer 51 to be decomposed again, and the coarse potassium sieve enters the coarse potassium concentration and dehalogenation system 6.
  • the crude potassium concentration and dehalogenation system 6 concentrates the crude potassium under sieve to obtain a fourth underflow slurry and a fourth overflow liquid.
  • the solid mass content of the fourth underflow slurry is 40%-45% .
  • dehalogenate the fourth underflow slurry to obtain a second filtrate and crude potash ore with moisture content ⁇ 10%
  • the second filtrate is returned to the concentration process for recovery
  • the fourth overflow liquid is sent to the raw ore screening system
  • the carnallite in the liquid phase is recovered by adding halogen, and the crude potassium ore with moisture content ⁇ 10% enters the next process.
  • the refined potassium washing and dehalogenation system 7 washes the crude potassium ore with moisture content ⁇ 10%, further dissolves magnesium chloride and potassium chloride, adds fresh water according to the conductivity, and adjusts the slurry concentration to achieve a solid mass content of 40% to 45%, the washed slurry is concentrated to obtain a fifth overflow liquid and a fifth underflow slurry.
  • the fifth overflow liquid is used by the overflow liquid and filtrate treatment system 8 to prepare and decompose mother liquor.
  • a part of the fifth underflow slurry is returned to the washing process for adjusting the concentration of the washing slurry, and most of it enters the dehalogenation process, where the fifth underflow slurry is dehalogenated to obtain concentrated potassium ore with moisture content ⁇ 10%, a third filtrate is also obtained during the dehalogenation process, and the third filtrate is used for recycling in the concentration process inside the refined potassium washing and dehalogenation system 7.
  • Figure 2 shows a schematic diagram of the overflow and filtrate treatment system.
  • the overflow liquid and filtrate treatment system 8 includes a first treatment system 81, a second treatment system 82, and a third treatment system 83.
  • the first treatment system 81 is respectively connected to the raw ore treatment system 1
  • the flotation system 3 is connected to receive the first overflow liquid from the raw ore processing system 1 and the flotation tail salt from the flotation system 3, and connect the first overflow liquid to the flotation tail
  • the salt is slurried and discharged
  • the second processing system 82 is respectively connected with the cold crystallization and coarse potassium screening system 5 and the refined potassium washing and dehalogenation system 7 for screening from the cold crystallization and coarse potassium
  • the system 5 receives the third overflow liquid, receives the fifth overflow liquid from the refined potassium washing and dehalogenation system 7, and after being adjusted by fresh water, it is transported to the cold crystallization and coarse potassium screening system 5 as the decomposition mother liquor
  • the third processing system 83 is connected to the low-sodium concentration and dehalogenation system 4, and is used to receive
  • the flotation tail salt is a foam with sodium chloride solids, which is inconvenient to discharge, and the first overflow liquid can be mixed with it for convenient transportation.
  • the flotation tail salt contains a large amount of sodium chloride, and after being dissolved by the first overflow liquid, it can also be used as a raw material for recovering sodium chloride.
  • the decomposition mother liquor is used in the cold crystallization and coarse potassium screening system 5 to decompose the slurry in the crystallization process.
  • the first filtrate contains fine-particle carnallite, which is concentrated in the present invention and filtered by a horizontal belt machine to recover the fine-particle carnallite.
  • the first treatment system 81 may include a tail salt clarification tank, a tail salt tank, etc.
  • the tail salt tank is used to receive the tail salt and the first overflow liquid, so that the tail salt can be transported smoothly.
  • the remaining first overflow liquid can be discharged to the tail salt clarification tank, and then discharged to the carnallite salt field for recovery after standing still.
  • the second processing system 82 may be a dissolution tank, which receives the third overflow liquid and the fifth overflow liquid, and adds fresh water to configure and decompose the mother liquid.
  • the third processing system 83 includes a thickener and a centrifuge or a belt filter.
  • the low-sodium concentration and dehalogenation system 4 is connected to the flotation system 3, and is used to transport the second overflow liquid to the flotation system 3 for adjusting The consistency of the slurry.
  • the second overflow liquid is preferentially delivered to the flotation system 3 to adjust the concentration of the slurry slurry, and the excess second overflow liquid can be returned to the carnallite salt field for recovery.
  • the crude potassium concentration and dehalogenation system 6 is connected to the raw ore processing system 1 for sending the fourth overflow liquid to the raw ore processing system 1 to prepare carnallite slurry.
  • Fig. 3 shows another schematic diagram of the first processing system.
  • the first processing system (81) also includes a primary sweeping tank 811, a secondary sweeping tank 812, and a storage tank 813.
  • the primary sweeping tank 811 is connected to the flotation system for After receiving flotation tailings and performing primary sweeping to obtain primary sweeping foam and primary sweeping underflow;
  • the secondary sweeping tank 812 is connected to the primary sweeping tank 811 for receiving the primary sweeping Underflow and perform secondary sweeping to obtain secondary sweeping foam and secondary sweeping underflow;
  • the primary sweeping tank 811 is connected to the tailing salt pond, and is used to transport the primary sweeping foam to the tailing salt pond;
  • the secondary scavenging tank 812 is connected to the storage tank 813, and is used to transport the secondary scavenging underflow to the storage tank 813;
  • the secondary scavenging tank 812 is connected to the low sodium concentration and dehalogenation System connection, used to transport the secondary sweep bottom stream to the low sodium concentration and dehalogenation system.
  • the primary scavenging tank 811 performs primary scavenging on the flotation tail salt foam to obtain primary scavenging foam and primary scavenging underflow. Wherein, most of the flotation agent in the primary sweeping foam is combined with sodium chloride, which is difficult to recycle. At the same time, the potassium chloride content in the primary scavenging foam is relatively low, and the potassium chloride in it is difficult to recover economic benefits in the system.
  • the present invention adopts the primary scavenging foam and the first overflow liquid to be discharged into the tail salt pond. In the process.
  • the secondary sweeping tank 812 is also designed to be lower than the primary sweeping tank 811, so that the first underflow flows into the secondary sweeping tank 812 by itself, and performing secondary sweeping to obtain secondary sweeping foam And secondary sweep selection bottom flow.
  • the secondary sweeping underflow can also be transported as a low-sodium slurry to a low-sodium thickener for subsequent processes.
  • the secondary sweeping foam contains a large amount of flotation reagents that are not combined with sodium chloride, and it is combined with potassium chloride in the primary selection process, but potassium chloride is released during the second sweeping and enters the foam Flotation reagent, this part of the flotation reagent is the part that needs to be recycled in the present invention.
  • the secondary scavenging foam is collected in the storage tank 813, and the secondary scavenging foam is transported to the flotation distribution tank by the transfer pump. On the one hand, the flotation agent is recovered; on the other hand, the secondary scavenging foam is recovered.
  • the potassium chloride content in the grade sweeping foam is relatively high, and it also has the value of recovery. This setting greatly improves the flotation effect, saves flotation reagents, and increases the yield of potassium chloride.
  • Figure 4 shows a schematic diagram of the raw ore processing system.
  • the raw ore processing system 1 includes a carnallite screening machine 11 and a raw ore thickening machine 12.
  • the carnallite screening machine 11 is used to screen out impurities and large particles of salt in the carnallite slurry.
  • the raw ore thickener 12 is connected to the carnallite screening machine 11, and is used to concentrate the under-screen product to obtain a first overflow liquid and a first underflow slurry, so that the first underflow
  • the solid mass content of the pulp 30-45%, and the number of the raw ore thickener 12 is one or more.
  • the carnallite pulp passes through the carnallite screening machine 11 to screen out impurities and large particles of salt.
  • the products under the screen enter the ore thickener 12 for concentration, and the first underflow pulp (solid mass content: 30% to 35%) is used
  • the underflow is pumped to the slurry mixing system 2, and a part of the first overflow liquid is used for mixing with the tail salt, and the other part is discharged to the carnallite salt field for recycling.
  • the raw ore thickener 12 may be arranged in parallel, and even if a certain thickener fails, the operation of the entire production line will not be affected. Or adopt a multiple-use and one-standby method to keep the overall processing capacity of the ore thickener 12 stable.
  • Figure 5 shows a schematic diagram of the mixing system.
  • the slurry mixing system 2 includes a slurry distribution tank 21 and a slurry tank 22.
  • the slurry distribution tank 21 includes a plurality of raw ore thickeners 12 interfaces for connecting with a plurality of raw ore thickeners 12 , Receiving the first underflow slurry, mixing the first underflow slurry with a flotation agent, and distributing the first underflow slurry and the flotation agent to the slurry tank 22;
  • the slurry tank 22 is connected with the slurry distribution tank 21, and is used to uniformly mix the first underflow slurry and the flotation agent to obtain a slurry slurry.
  • the slurry distribution tank 21 receives the first underflow slurry from the ore thickener 12, according to the solid mass content of the first underflow slurry, the flotation agent is added to the slurry distribution tank 21, and then the slurry enters the mixing tank 22. At the same time, use an air compressor to input 0.5-0.7Mpa air into the annular pipe at the bottom of the slurry tank 22.
  • the slurry distribution tank 21 is connected with a plurality of raw ore thickeners 12 to mix the underflow slurry of the plurality of thickeners together, and also mix the flotation agent, so that the slurry is adjusted before the flotation process Consistent composition also makes the flotation agent evenly distributed in the mixed slurry, which improves the flotation efficiency.
  • Figure 6 shows a schematic diagram of the flotation system.
  • the flotation system 3 includes a flotation distribution tank 31 and a flotation machine 32.
  • the flotation distribution tank 31 is connected to the slurry adjustment system 2 and is used to receive the slurry adjustment
  • the concentration of the adjusted slurry is adjusted by adding the adjusted mother liquor to obtain the adjusted slurry; the solid content of the adjusted slurry is 20%-25%; the adjusted mother liquor refers to the liquid with the same components as the slurry mother liquor
  • the flotation machine 32 is connected to the flotation distribution tank 31, and is used for roughing, beneficiating and sweeping the conditioning slurry to obtain tailings and low-sodium carnallite pulp; the There are one or more flotation machines 32.
  • the flotation distribution tank 31 receives the adjusted slurry and adjusts its concentration by adjusting the mother liquor, and then transports the adjusted slurry to a plurality of flotation machines 32 to ensure that the material composition of each flotation machine 32 is consistent. It is convenient to control the working parameters of the flotation machine 32 uniformly. Flotation is divided into three steps: rough selection, beneficiation, and sweeping to obtain tail salt and low-sodium carnallite slurry.
  • flotation machines 32 Similar to the raw ore thickener 12, there may be one or more flotation machines 32. When there are multiple flotation machines 32, the flotation machines 32 are arranged side by side. Increase the processing capacity of the present invention.
  • the flotation distribution tank 31 keeps the various properties of the materials in each flotation machine 32 consistent, and facilitates the unified setting of flotation conditions.
  • Figure 7 shows a schematic diagram of a low sodium concentration and dehalogenation system.
  • the low-sodium concentration and dehalogenation system 4 includes a low-sodium thickener 41, a low-sodium centrifuge distribution tank 42, and a low-sodium centrifuge 43.
  • the low-sodium thickener 41 is used to receive low-sodium light halogen.
  • the low-sodium centrifuge distribution tank 42 is connected to the low-sodium thickener 41, and is used to receive the second underflow slurry and distribute the second underflow slurry to the low-sodium centrifuge 43;
  • There are one or more low-sodium centrifuges 43 which are connected to the low-sodium centrifuge distribution tank 42, and are used to dehalogenate the second underflow slurry to obtain a first filtrate with a moisture content of ⁇ 10% low sodium Carnallite mine.
  • the low-sodium thickener 41 receives the low-sodium carnallite ore and concentrates to obtain a second underflow slurry and a second overflow liquid.
  • the low-sodium thickener 41 is connected to the flotation distribution tank 31 for
  • the second overflow liquid is delivered to the flotation distribution tank 31 as a regulating mother liquid.
  • the low-sodium thickener 41 controls the flow and concentration of the underflow to make the solid mass content of the second underflow slurry: 40%-45%, so as to increase the centrifugal dehalogenation yield.
  • the low-sodium thickener 41 may be a plurality of thickeners connected in parallel with the flotation machine 32, which can increase the processing capacity of the low-sodium thickener 41.
  • the low-sodium centrifuge distribution tank 42 is connected to the low-sodium thickener 41.
  • the second underflow pulp discharged from each low-sodium thickener 41 can be placed in the The low-sodium centrifuge distribution tank 42 is evenly mixed, and then distributed to the low-sodium centrifuge 43 for dehalogenation.
  • the overall processing capacity can be increased, and when a certain low-sodium centrifuge 43 fails, the overall The production line is not affected.
  • Figure 8 shows a schematic diagram of the cold crystallization and coarse potassium screening system.
  • the cold crystallization and coarse potassium screening system 5 includes a crystallizer 51 and a coarse potassium screening machine 52.
  • crystallizers 51 for receiving the moisture content ⁇ 10%.
  • Sodium carnallite ore is decomposed and crystallized to obtain a third underflow slurry and a third overflow liquid; the solid mass content of the third underflow slurry is 15%-30%; the coarse potassium screening machine 52 is connected to the crystallizer 51 , Used for sieving the third underflow slurry to obtain coarse potassium oversize and coarse potassium undersize.
  • the crystallizer 51 is connected with a low-sodium centrifuge 43, the centrifuged low-sodium carnallite ore with moisture content ⁇ 10% enters the crystallizer 51, and the decomposition mother liquor is added at the same time to decompose and crystallize the low-sodium carnallite ore at a controlled rate.
  • Control the decomposition conditions of low-sodium carnallite ore to control the potassium chloride supersaturation in the solution reduce the number of potassium chloride crystals, and achieve the purpose of growing potassium chloride crystals at room temperature, while sodium chloride is in the liquid phase. Unsaturated state cannot be precipitated, which ensures the quality and particle size of potassium chloride products.
  • the third underflow slurry and the third overflow liquid are 17%-27%, and it is sent to the coarse potassium separator for screening operations.
  • the undecomposed coarse-grained carnallite returns to the crystallizer 51 to decompose again.
  • the undersieve enters the coarse potassium thickener 61.
  • the third overflow liquid is processed by the overflow liquid and filtrate processing system 8 and is used to configure the decomposition mother liquor.
  • Figure 9 shows a schematic diagram of the crude potassium concentration and dehalogenation system.
  • the crude potassium concentration and dehalogenation system 6 includes a crude potassium thickener 61, a crude potassium centrifuge distribution tank 62, and a crude potassium centrifuge 63.
  • There are one or more crude potassium thickeners 61 Used for receiving and concentrating the coarse potassium sieve to obtain the fourth overflow liquid and the fourth underflow slurry; the solid mass content of the fourth underflow slurry is 40%-45%; the coarse potassium centrifuge distribution tank 62 is connected to the coarse potassium thickener 61, and is used to receive the fourth underflow slurry and distribute the fourth underflow slurry to each coarse potassium centrifuge 63; the coarse potassium centrifuge 63 is one or A plurality of them are connected to the coarse potassium centrifuge distribution tank 62 and used for dehalogenating the fourth underflow slurry to obtain a second filtrate and coarse potassium ore with a moisture content of ⁇ 10%.
  • the coarse potassium thickener 61 receives the coarse potassium sieve, and obtains the fourth underflow slurry and the fourth overflow liquid after concentration.
  • the fourth underflow slurry has a solid mass content of 40%-45%, and is transported to the coarse potassium centrifuge distribution tank 62 to be evenly distributed to the coarse potassium centrifuge 63 for dehalogenation to obtain the second filtrate.
  • the crude potassium thickener 61 is connected to the crude ore thickener 12 of the crude ore processing system 1 and is used to transport the fourth overflow liquid to the crude ore thickener 12 to recover carnallite therein.
  • the crude potassium centrifuge 63 is connected to the crude potassium thickener 61, and the second filtrate is transported from the crude potassium centrifuge 63 to the crude potassium thickener 61 for recycling.
  • the crude potassium centrifuge 63 is connected to the crude potassium thickener 61 and is used to transport the second filtrate to the crude potassium thickener 61 for recycling.
  • Figure 10 shows a schematic diagram of the refined potassium washing and dehalogenation system.
  • the refined potassium washing and dehalogenation system 7 includes a repulp washing tank 71, a refined potassium thickener 72 and a refined potassium centrifuge 73.
  • the repulp washing tank 71 is one or more for Receive the crude potash ore with moisture content ⁇ 10% and wash it to obtain a re-pulp washing slurry;
  • the refined potassium thickener 72 is one or more, matched with the re-pulp washing tank, and is used to concentrate the re-pulp washing material To obtain a fifth underflow slurry; there are one or more refined potassium centrifuges 73, which are matched with the refined potassium thickener 72, and are used to dehalogenate the fifth underflow slurry to obtain refined potassium ore and The third filtrate; the moisture content of the concentrated potassium ore ⁇ 10%.
  • the refined potassium thickener 72 is connected to the repulp washing tank, and is used to adjust the concentration of the coarse potassium ore with moisture content ⁇ 10% by using the fifth underflow slurry.
  • the refined potassium thickener 72 is connected to the refined potassium centrifuge 73, and is used to recover the third filtrate to the refined potassium thickener 72 for concentration.
  • the crude potassium centrifuge 63 After the crude potassium centrifuge 63 is centrifuged, the crude potassium ore with a moisture content of ⁇ 10% is obtained, which enters the repulp washing tank 71, adds fresh water according to the conductivity, and adjusts the repulp washing tank 71 with the fifth underflow slurry of the refined potassium thickener 72
  • the concentration of the slurry reaches the solid mass content: 40%-45%, and the washed slurry enters the refined potassium thickener 72 for concentration to obtain the fifth overflow liquid and the fifth underflow slurry.
  • Most of the fifth underflow pulp enters the refined potassium centrifuge 73 for dehalogenation to obtain potassium chloride wet material (concentrated potassium ore, moisture content ⁇ 10%), and a part is used to adjust the repulp washing tank 71 Slurry concentration.
  • the third filtrate is returned to the refined potassium thickener 72 for recovery.
  • the fifth overflow liquid is recovered by the overflow liquid and filtrate treatment system 8 for the decomposition mother liquid for configuring the crystallizer 51.
  • FIG. 11 shows a schematic diagram of the steps of a method for producing potassium chloride that can recycle by-products.
  • a method for producing potassium chloride that can recycle by-products includes, in the first step S1, screening and concentrating carnallite pulp to obtain a first underflow pulp and a first overflow liquid
  • the second step S2 mixing the flotation reagent with the first underflow slurry to obtain a mixed slurry;
  • the third step S3, perform flotation operations on the mixed slurry to obtain tail salt and low sodium light Halite slurry;
  • the fourth step S4 the low-sodium carnallite slurry is concentrated and the brine is removed to obtain the second overflow liquid, the first filtrate and the low-sodium carnallite ore with a moisture content of ⁇ 10%;
  • Step S5 decompose and crystallize the low-sodium carnallite ore with a moisture content of ⁇ 10%, and screen, to obtain the third overflow liquid, the coarse potassium sieve and the coarse potassium sieve;
  • the sixth step S6 The crude potassium sieve is concentrated and dehalogenated to obtain the
  • the eighth step S8 includes mixing the first overflow liquid with the flotation tail salt and then discharging; receiving the third overflow liquid and the fifth overflow liquid, After being adjusted by fresh water, it is used as the decomposition mother liquor of the crystallization process; the first filtrate is received, and the first filtrate is concentrated and filtered to recover carnallite.
  • the method further includes performing primary sweeping of the flotation tailings to obtain primary sweeping foam and primary sweeping underflow; performing secondary sweeping on the primary sweeping underflow to obtain secondary Sweeping foam and secondary sweeping underflow; mixing the primary sweeping foam and the first overflow liquid and then transporting to the tail salt pond; sending the secondary sweeping underflow to the low-sodium concentration and dehalogenation system.
  • the second overflow liquid is used to adjust the concentration of the mixed slurry.
  • the fourth overflow liquid is used for the preparation of carnallite pulp.
  • the first step S1 includes screening out impurities and large-particle salt in the carnallite slurry to obtain an undersize product; and concentrating the undersize product to obtain a first overflow liquid And the first underflow slurry, so that the solid mass content of the first underflow slurry is 30%-45%; the solid mass content of the carnallite slurry is ⁇ 25%.
  • the second step S2 includes mixing the first underflow slurry with a flotation agent, and distributing the first underflow slurry and the flotation agent; The first underflow slurry and the flotation agent are uniformly mixed to obtain a mixed slurry.
  • the third step S3 includes adjusting the concentration of the adjusted slurry by adding a adjusted mother liquor to obtain a adjusted slurry; the solid mass content of the adjusted slurry is 20%-25%
  • the adjustment mother liquor refers to the liquid phase of the same composition as the slurry mother liquor; the adjustment slurry is subjected to rough selection, beneficiation and sweep selection operations to obtain tailings and low-sodium carnallite slurry.
  • the fourth step S4 includes concentrating the low-sodium carnallite slurry to obtain a second underflow slurry and a second overflow liquid; the solid mass content of the second underflow slurry is 40%-45%; distributing the second underflow slurry; dehalogenating the second underflow slurry to obtain a first filtrate and a low sodium carnallite ore with a moisture content of ⁇ 10%.
  • the fifth step S5 includes mixing the low-sodium carnallite ore with a moisture content of ⁇ 10% and the decomposition mother liquor to perform speed-controlled decomposition and crystallization to obtain a third underflow slurry and a third overflow
  • the solid mass content of the third underflow slurry is 15%-30%; the third underflow slurry is subjected to a screening operation to obtain a coarse potassium sieve and a coarse potassium sieve.
  • the sixth step S6 includes concentrating the crude potassium underflow to obtain a fourth overflow liquid and a fourth underflow slurry; the solid content of the fourth underflow slurry is 40% ⁇ 45%; the fourth underflow slurry is distributed; the fourth underflow slurry is dehalogenated to obtain a second filtrate and a crude potash ore with a moisture content of ⁇ 10%.
  • the second filtrate is transported to the process of concentrating the crude potassium undersize for recycling.
  • the seventh step S7 includes washing the crude potassium ore with moisture content ⁇ 10% to obtain a re-slurry washing slurry; concentrating the re-slurry washing slurry to obtain a fifth underflow slurry; The fifth underflow slurry is dehalogenated to obtain the potash concentrate and the third filtrate; the moisture content of the potash concentrate is less than or equal to 10%.
  • the fifth underflow slurry is used to adjust the concentration of the coarse potash with a moisture content of ⁇ 10% in the repulp washing process.
  • the third filtrate is recovered to the repulp washing slurry concentration step for concentration.
  • the invention collects and reuses the first overflow liquid, the third overflow liquid, the fifth overflow liquid and the first filtrate into the system respectively, recovers potassium chloride in the system, and replaces the addition of foreign materials. On the one hand, the yield of potassium chloride is increased, and on the other hand, the cost is saved.
  • multiple devices such as the raw ore thickener 12, flotation machine 32, and low sodium thickener 41 are connected in parallel, and the mixing tank 22 is uniformly mixed with slurry, dispersed and distributed, so that the processing concentration of the material is unified, and each is connected in parallel.
  • the equipment has a standby relationship with each other, even if a certain equipment fails or needs maintenance, it will not affect the operation of the overall process.

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Abstract

提供可回收利用副产物的生产氯化钾的系统和方法。该系统包括：原矿处理系统（1）、调浆系统（2）、浮选系统（3）、低钠浓缩及脱卤系统（4）、冷结晶及粗钾筛分系统（5）、粗钾浓缩及脱卤系统（6）、精钾洗涤及脱卤系统（7）以及溢流液和滤液处理系统（8）。该方法包括：光卤石矿浆依次经过上述系统处理，得到各阶段的溢流液、滤液、尾盐和氯化钾产品等。该系统和方法增加了氯化钾产率，节约成本。

Description

一种可回收利用副产物的生产氯化钾的方法和系统 技术领域
本发明总体涉及氯化钾生产领域，更具体地，涉及一种可回收利用副产物的生产氯化钾的方法和系统。
背景技术
现有利用盐湖卤水生产氯化钾的方法主要有，冷结晶-正浮选法工艺、热熔结晶法工艺、反浮选-冷结晶工艺、兑卤盐工艺等或者上述多种工艺的联合实施。反浮选—冷结晶法工艺是使用比较广泛的，但该工艺对原料光卤石质量要求高，宜用盐田光卤石矿生产，投入量大，能源消耗较大，且最终产品氯化钾品位只能达到95％左右。
同时，在整条生产工艺过程中，产生的副产品中含有的氯化钾回收处理方面做的不足，造成大量的氯化钾随着尾盐一同排出，浪费了钾资源。
另外，在整条生产线上，由于某个设备出现问题，就会造成物料堆积，严重的甚至需要全线停工检修，不利于提高生产效率。
所以，有必要进一步改善、提高相关生产系统及工艺方法，将钾肥生产中的副产品采用系统内利用和系统外利用相结合的方法，尽可能的将原料中的氯化钾提取出来，增加钾肥的产量和效率，另外，改进各设备的连接方式和组合方式，便于维持连续生产，不因个别设备故障影响整体工艺。
发明内容
本发明解决的问题是，提供一种可回收利用副产物的生产氯化钾的方法和系统。
本发明提供了一种可回收利用副产物的生产氯化钾的系统，包括，原矿处理系统1、调浆系统2、浮选系统3、低钠浓缩及脱卤系统4、冷结晶及粗钾筛分系统5、粗钾浓缩及脱卤系统6，精钾洗涤及脱卤系统7，还包括溢流液和滤液处理系统8，所述原矿处理系统1用于将光卤石矿浆进行筛分和浓 缩，得到第一底流矿浆和第一溢流液；所述调浆系统2与所述原矿处理系统1连接，用于将浮选药剂与所述第一底流料浆混合，得到调浆料浆；所述浮选系统3用于对所述调浆料浆进行浮选作业，得到尾盐和低钠光卤石料浆；所述低钠浓缩及脱卤系统4与所述浮选系统3连接，用于将所述低钠光卤石料浆进行浓缩并脱除卤水，得到第二溢流液、第一滤液和含湿≤10％低钠光卤石矿；所述冷结晶及粗钾筛分系统5与所述低钠浓缩及脱卤系统4连接，用于将含湿≤≤10％低钠光卤石矿进行分解结晶，并进行筛分，得到第三溢流液、粗钾筛上物和粗钾筛下物；所述粗钾浓缩及脱卤系统6与所述冷结晶及粗钾筛分系统5连接，用于将所述粗钾筛下物进行浓缩和脱卤，得到第四溢流液、第二滤液和含湿≤10％粗钾矿；所述精钾洗涤及脱卤系统7与所述粗钾浓缩及脱卤系统6连接，用于将所述含湿≤10％粗钾矿进行洗涤和脱卤，得到第三滤液和精钾矿；所述溢流液和滤液处理系统8用于回收处理所述第一溢流液、第三溢流液、第五溢流液和第一滤液。
根据本发明的一个实施方式，所述溢流液和滤液处理系统8包括第一处理系统81、第二处理系统82、第三处理系统83，所述第一处理系统81分别与所述原矿处理系统1、浮选系统3连接，用于从所述原矿处理系统1接收第一溢流液，从所述浮选系统3接收浮选尾盐，将所述第一溢流液与所述浮选尾盐进行调浆后排出；所述第二处理系统82分别与所述冷结晶及粗钾筛分系统5和精钾洗涤及脱卤系统7连接，用于从所述冷结晶及粗钾筛分系统5接收第三溢流液，从所述精钾洗涤及脱卤系统7接收第五溢流液，经淡水调节后，输送至冷结晶及粗钾筛分系统5用作分解母液；所述第三处理系统83与所述低钠浓缩及脱卤系统4连接，用于接收第一滤液，并对第一滤液进行浓缩和过滤，回收光卤石。
根据本发明的一个实施方式，所述第一处理系统(81)还包括初级扫选槽811、次级扫选槽812、储存罐813，所述初级扫选槽811与所述浮选系统连接，用于接收浮选尾盐，并进行初级扫选，得到初级扫选泡沫和初级扫选底流；所述次级扫选槽812与所述初级扫选槽811连接，用于接收所述初级扫选底流并进行次级扫选，得到次级扫选泡沫和次级扫选底流；所述初级扫选槽811与所述尾盐池连接，用于将所述初级扫选泡沫输送至尾盐池；所述 次级扫选槽812与所述储存罐813连接，用于将所述次级扫选底流输送至所述储存罐813；所述次级扫选槽812与所述低钠浓缩及脱卤系统连接，用于将所述次级扫选底流输送至所述低钠浓缩及脱卤系统。
根据本发明的一个实施方式，所述低钠浓缩及脱卤系统4与所述浮选系统3连接，用于将所述第二溢流液输送至所述浮选系统3，用于调节调浆料浆的浓度。
根据本发明的一个实施方式，所述粗钾浓缩及脱卤系统6与所述原矿处理系统1连接，用于将所述第四溢流液发送至原矿处理系统1浓缩利用。
根据本发明的一个实施方式，所述原矿处理系统1包括光卤石筛选机11、原矿浓密机12，所述光卤石筛选机11用于筛除光卤石矿浆中的杂物及大颗粒盐，得到筛下产品；所述原矿浓密机12与所述光卤石筛选机11连接，用于将所述筛下产品浓缩，得到第一溢流液和第一底流矿浆，使所述第一底流矿浆固体质量含量：30—45％，所述原矿浓密机12为一个或多个。
根据本发明的一个实施方式，所述调浆系统2包括料浆分配槽21和调浆罐22，所述料浆分配槽21包括多个原矿浓密机12接口，用于与多个原矿浓密机12连接，接收所述第一底流料浆，将所述第一底流料浆与浮选药剂混合，并将所述第一底流料浆和所述浮选药剂分配至所述调浆罐22；所述调浆罐22与所述料浆分配槽21连接，用于将所述第一底流料浆和所述浮选药剂混合均匀得到调浆料浆。
根据本发明的一个实施方式，所述浮选系统3包括浮选分配槽31、浮选机32，所述浮选分配槽31，与所述调浆系统2连接，用于接收调浆料浆，并通过加入调节母液对所述调浆料浆进行浓度调节，得到调节料浆；所述调节料浆固体质量含量为20％～25％；所述调节母液是指与料浆母液同组分的液相；所述浮选机32与所述浮选分配槽31连接，用于将所述调节料浆进行粗选、精选和扫选作业，得到尾盐和低钠光卤石矿浆；所述浮选机32为一个或多个。
根据本发明的一个实施方式，所述低钠浓缩及脱卤系统4包括低钠浓密机41、低钠离心机分配罐42和低钠离心机43，所述低钠浓密机41用于接收低钠光卤石矿浆并将所述低钠光卤石矿浆进行浓缩，得到第二底流矿浆和第 二溢流液；所述第二底流矿浆固体质量含量为40％～45％；所述低钠浓密机41为一个或多个；所述低钠离心机分配罐42与所述低钠浓密机41连接，用于接收所述第二底流矿浆并将所述第二底流矿浆分配至低钠离心机43；所述低钠离心机43为一个或多个，与所述低钠离心机分配罐42连接，用于将所述第二底流矿浆进行脱卤，得到第一滤液和含湿≤10％低钠光卤石矿。
根据本发明的一个实施方式，所述冷结晶及粗钾筛分系统5包括结晶器51和粗钾筛选机52，所述结晶器51为一个或多个，用于接收所述含湿≤10％低钠光卤石矿并分解结晶，得到第三底流矿浆和第三溢流液；所述第三底流矿浆固体质量含量15％～30％；所述粗钾筛选机52与所述结晶器51连接，用于将所述第三底流料浆进行筛分，得到粗钾筛上物和粗钾筛下物。
根据本发明的一个实施方式，所述粗钾浓缩及脱卤系统6包括粗钾浓密机61、粗钾离心机分配罐62和粗钾离心机63，所述粗钾浓密机61为一个或多个，用于接收并浓缩所述粗钾筛下物，得到第四溢流液和第四底流矿浆；所述第四底流料浆固体质量含量为40％～45％；所述粗钾离心机分配罐62与所述粗钾浓密机61连接，用于接收所述第四底流料浆，并将所述第四底流料浆分配至各粗钾离心机63；所述粗钾离心机63为一个或多个，与所述粗钾离心机分配罐62连接，用于将所述第四底流料浆进行脱卤，得到第二滤液和含湿≤10％粗钾矿。
根据本发明的一个实施方式，所述粗钾离心机63与所述粗钾浓密机61连接，用于将所述第二滤液输送至所述粗钾浓密机61回收利用。
根据本发明的一个实施方式，所述精钾洗涤及脱卤系统7包括再浆洗涤罐71、精钾浓密机72和精钾离心机73，所述再浆洗涤罐71为一个或多个，用于接收所述含湿≤10％粗钾矿并进行洗涤得到再浆洗料浆；所述精钾浓密机72为一个或多个，与所述再浆洗罐相匹配，用于浓缩所述再浆洗料浆，得到第五底流料浆；所述精钾离心机73为一个或多个，与所述精钾浓密机72相匹配，用于对第五底流料浆进行脱卤，得到精钾矿和第三滤液；所述精钾矿含湿量≤10％。
根据本发明的一个实施方式，所述精钾浓密机72与所述再浆洗罐连接，用于利用所述第五底流料浆调节所述含湿≤10％粗钾矿的浓度。所述精钾浓 密机72与所述精钾离心机73连接，用于将所述第三滤液回收至所述精钾浓密机72进行浓缩。
根据本发明的一个方面，提供了一种可回收利用副产物的生产氯化钾的方法，包括，第一步骤S1，将光卤石矿浆进行筛分和浓缩，得到第一底流矿浆和第一溢流液；第二步骤S2，将浮选药剂与所述第一底流料浆混合，得到调浆料浆；第三步骤S3，对所述调浆料浆进行浮选作业，得到尾盐和低钠光卤石料浆；第四步骤S4，将所述低钠光卤石料浆进行浓缩并脱除卤水，得到第二溢流液、第一滤液和含湿≤10％低钠光卤石矿；第五步骤S5，将所述含湿≤10％低钠光卤石矿进行分解结晶，并进行筛分，得到第三溢流液、粗钾筛上物和粗钾筛下物；第六步骤S6，将所述粗钾筛下物进行浓缩和脱卤，得到第四溢流液、第二滤液和含湿≤10％粗钾矿；第七步骤S7，将所述含湿≤10％粗钾矿进行洗涤和脱卤，得到第三滤液和精钾矿；第八步骤S8，回收处理所述第一溢流液、第三溢流液、第五溢流液和第一滤液。
根据本发明的一个实施方式，所述第八步骤S8包括，将所述第一溢流液与所述浮选尾盐进行调浆后排出；接收第三溢流液和第五溢流液，经淡水调节后，用作结晶工艺的分解母液；接收第一滤液，并对第一滤液进行浓缩和过滤，回收光卤石。
根据本发明的一个实施方式，还包括将所述浮选尾盐进行初级扫选，得到初级扫选泡沫和初级扫选底流；将所述初级扫选底流并进行次级扫选，得到次级扫选泡沫和次级扫选底流；将所述初级扫选泡沫与所述第一溢流液调浆后输送至尾盐池；将所述次级扫选底流输所述低钠浓缩及脱卤系统。
根据本发明的一个实施方式，将所述第二溢流液输用于调节调浆料浆的浓度。
根据本发明的一个实施方式，将所述第四溢流液用于调配光卤石矿浆。
根据本发明的一个实施方式，所述第一步骤S1包括，筛除光卤石矿浆中的杂物及大颗粒盐，得到筛下产品；将所述筛下产品浓缩，得到第一溢流液和第一底流矿浆，使所述第一底流矿浆固体质量含量：30％～45％；所述光卤石矿浆的固体质量含量≥25％。
根据本发明的一个实施方式，所述第二步骤S2包括，将所述第一底流料 浆与浮选药剂混合，并将所述第一底流料浆和所述浮选药剂进行分配；将所述第一底流料浆和所述浮选药剂混合均匀得到调浆料浆。
根据本发明的一个实施方式，所述第三步骤S3包括，通过加入调节母液对所述调浆料浆进行浓度调节，得到调节料浆；所述调节料浆固体质量含量为20％～25％；所述调节母液是指与料浆母液同组分的液相；将所述调节料浆进行粗选、精选和扫选作业，得到尾盐和低钠光卤石矿浆。
根据本发明的一个实施方式，所述第四步骤S4包括，将所述低钠光卤石矿浆进行浓缩，得到第二底流矿浆和第二溢流液；所述第二底流矿浆固体质量含量为40％～45％；将所述第二底流矿浆进行分配；将所述第二底流矿浆进行脱卤，得到第一滤液和含湿≤10％低钠光卤石矿。
根据本发明的一个实施方式，所述第五步骤S5包括，将所述含湿≤10％低钠光卤石矿与分解母液混合，进行控速分解结晶，得到第三底流矿浆和第三溢流液；所述第三底流矿浆固体质量含量15％～30％；将所述第三底流料浆进行筛分作业，得到粗钾筛上物和粗钾筛下物。
根据本发明的一个实施方式，所述第六步骤S6包括，浓缩所述粗钾筛下物，得到第四溢流液和第四底流矿浆；所述第四底流料浆固体质量含量为40％～45％；将所述第四底流料浆进行分配；将所述第四底流料浆进行脱卤，得到第二滤液和含湿≤10％粗钾矿。
根据本发明的一个实施方式，将所述第二滤液输送至浓缩所述粗钾筛下物的工序回收利用。
根据本发明的一个实施方式，所述第七步骤S7包括，将所述含湿≤10％粗钾矿进行洗涤得到再浆洗料浆；浓缩所述再浆洗料浆，得到第五底流料浆；将所述第五底流料浆进行脱卤，得到精钾矿和第三滤液；所述精钾矿含湿量≤10％。
根据本发明的一个实施方式，在再浆洗工序中利用所述第五底流料浆调节所述含湿≤10％粗钾矿的浓度；将所述第三滤液回收至再浆洗料浆浓缩工序进行浓缩。
本发明通过将第一溢流液、第三溢流液、第五溢流液和第一滤液分别进行收集回用至系统中，在系统内回收氯化钾，以及替代外来物料的加入，一 方面增加了氯化钾的产率，另一方面节约了成本。本发明在原矿浓密机12、浮选机32、低钠浓密机41等设备的多个并联，调浆罐22统一调浆、分散分配等方式，使得对物料的处理浓度统一的同时，各并联设备之间互成备用关系，即使某个设备故障或者需要检修，不影响整体工艺的运行。
附图说明
图1是一种可回收利用副产物的生产氯化钾的系统的示意图；
图2是溢流液和滤液处理系统的示意图；
图3是所述第一处理系统的另一种示意图；
图4是原矿处理系统的示意图；
图5是调浆系统的示意图；
图6是浮选系统的示意图；
图7是低钠浓缩及脱卤系统的示意图；
图8是冷结晶及粗钾筛分系统的示意图；
图9是粗钾浓缩及脱卤系统的示意图；
图10是精钾洗涤及脱卤系统的示意图；以及
图11是一种可回收利用副产物的生产氯化钾的方法的步骤示意图。
具体实施方式
下面结合附图对本发明的较佳实施例进行详细阐述，参考标号是指本发明中的组件、技术，以便本发明的优点和特征在适合的环境下实现能更易于被理解。下面的描述是对本发明权利要求的具体化，并且与权利要求相关的其它没有明确说明的具体实现也属于权利要求的范围。
图1示出了一种可回收利用副产物的生产氯化钾的系统的示意图。
如图1所示，一种可回收利用副产物的生产氯化钾的系统，包括，原矿处理系统1、调浆系统2、浮选系统3、低钠浓缩及脱卤系统4、冷结晶及粗钾筛分系统5、粗钾浓缩及脱卤系统6，精钾洗涤及脱卤系统7，还包括溢流液和滤液处理系统8，所述原矿处理系统1用于将光卤石矿浆进行筛分和浓缩，得到第一底流矿浆和第一溢流液；所述调浆系统2与所述原矿处理系统 1连接，用于将浮选药剂与所述第一底流料浆混合，得到调浆料浆；所述浮选系统3用于对所述调浆料浆进行浮选作业，得到尾盐和低钠光卤石料浆；所述低钠浓缩及脱卤系统4与所述浮选系统3连接，用于将所述低钠光卤石料浆进行浓缩并脱除卤水，得到第二溢流液、第一滤液和含湿≤10％低钠光卤石矿；所述冷结晶及粗钾筛分系统5与所述低钠浓缩及脱卤系统4连接，用于将含湿≤≤10％低钠光卤石矿进行分解结晶，并进行筛分，得到第三溢流液、粗钾筛上物和粗钾筛下物；所述粗钾浓缩及脱卤系统6与所述冷结晶及粗钾筛分系统5连接，用于将所述粗钾筛下物进行浓缩和脱卤，得到第四溢流液、第二滤液和含湿≤10％粗钾矿；所述精钾洗涤及脱卤系统7与所述粗钾浓缩及脱卤系统6连接，用于将所述含湿≤10％粗钾矿进行洗涤和脱卤，得到第三滤液和精钾矿；所述溢流液和滤液处理系统8用于回收处理所述第一溢流液、第三溢流液、第五溢流液和第一滤液。
本发明以盐田生产的光卤石为原料生产氯化钾，从盐田采收的光卤石主要成分为氯化钾、氯化钠、氯化镁，调节光卤石矿浆的浓度，使光卤石矿浆的固体质量含量≥25％。所述光卤石矿浆经过光卤石筛选机11，筛除杂物和大颗粒盐等，筛下物输送至原矿浓密机12浓缩，得到第一底流料浆和第一溢流液。通过调节浓缩设备的参数，使第一底流料浆的固体质量含量范围为30-45％。
所述第一溢流液进入所述溢流液和滤液处理系统8进行处理。
所述第一底流料浆进入调浆系统2，根据料浆中固体质量含量添加浮选药剂，通过搅拌等方式使二者混合均匀，得到调浆料浆。
所述第一底流料浆与浮选药剂充分混合均匀，能够在浮选工艺中使钠浮选药剂能够和氯化钠充分的接触，能够增大浮选效率。
本发明中采用的是反浮选冷结晶工艺，浮选药剂为氯化钠捕收剂，所述调浆料浆在进入浮选设备之前，还需要将其浓度进行调节，使其固体质量含量：20％～25％，进一步的控制浮选效率。
在反浮选过程中，氯化钠固体与浮选药剂结合形成泡沫，从浮选系统3中排出作为尾盐，还得到低钠光卤石料浆。所述低钠光卤石料浆主要成分为氯化钾、氯化镁，以及少量的氯化钠。
所述低钠光卤石料浆在所述低钠浓缩及脱卤系统4中先浓缩，使其固体 质量含量达到：40％～45％，浓缩得到第二溢流液，所述第二溢流液主要是含有氯化镁的溶液，然后在进行离心脱卤，最终得到第一滤液和含湿≤10％低钠光卤石矿。
其中，第二溢流液可以用于浮选系统3作为调浆料浆浓度的调节，第一滤液采用所述溢流液和滤液处理系统8进行回收利用，含湿≤10％低钠光卤石矿进入下一步工序。
所述含湿≤10％低钠光卤石矿输送至冷结晶及粗钾筛分系统5经过分解母液进行分解后进行结晶，控制溶液中氯化钾过饱和度，减少氯化钾晶体数量，达到在常温下使氯化钾晶体长大目的，而氯化钠处于不饱状态不能析出，保证了氯化钾产品质量和粒度。然后进行筛分作业，未分解的筛上物粗粒光卤石返回结晶器51再次分解，粗钾筛下物利进入下一步工序。
在分解结晶过程中产生第三溢流液和第三底流矿浆，第三溢流液用于所述溢流液和滤液处理系统8进行回收利用，用于合成分解母液。第三底流矿浆的固体质量含量为17-27％，主要是未分解的粗颗粒光卤石和细颗粒的氯化钾。对第三底流矿浆进行筛分，得到粗钾筛上物和粗钾筛下物，粗钾筛上物返回结晶器51再次分解，粗钾筛下物进入粗钾浓缩及脱卤系统6。
所述粗钾浓缩及脱卤系统6将所述粗钾筛下物进行浓缩，得到第四底流矿浆和第四溢流液，所述第四底流矿浆的固体质量含量为，40％～45％，再将所述第四底流矿浆进行脱卤，得到第二滤液和含湿≤10％粗钾矿，所述第二滤液返回浓缩工序回收，所述第四溢流液送至原矿筛分系统进行兑卤回收液相中的光卤石，所述含湿≤10％粗钾矿进入下一工序。
所述精钾洗涤及脱卤系统7将所述含湿≤10％粗钾矿粗进行洗涤，进一步的使氯化镁和氯化钾溶解，根据电导率加入淡水，调整料浆浓度达到固体质量含量为40％～45％，洗涤后的料浆进行浓缩，得到第五溢流液和第五底流矿浆，所述第五溢流液由所述溢流液和滤液处理系统8用于调配分解母液，所述第五底流料浆一部分返回至洗涤工序用于调节洗涤料浆的浓度，大部分进入脱卤工序，对所述第五底流料浆进行脱卤，得到含精钾矿，含湿量≤10％，脱卤过程中还得到第三滤液，所述第三滤液用于所述精钾洗涤及脱卤系统7内部的浓缩工艺中回收利用。
图2示出了溢流液和滤液处理系统的示意图。
如图2所示，所述溢流液和滤液处理系统8包括第一处理系统81、第二 处理系统82、第三处理系统83，所述第一处理系统81分别与所述原矿处理系统1、浮选系统3连接，用于从所述原矿处理系统1接收第一溢流液，从所述浮选系统3接收浮选尾盐，将所述第一溢流液与所述浮选尾盐进行调浆后排出；所述第二处理系统82分别与所述冷结晶及粗钾筛分系统5和精钾洗涤及脱卤系统7连接，用于从所述冷结晶及粗钾筛分系统5接收第三溢流液，从所述精钾洗涤及脱卤系统7接收第五溢流液，经淡水调节后，输送至冷结晶及粗钾筛分系统5用作分解母液；所述第三处理系统83与所述低钠浓缩及脱卤系统4连接，用于接收第一滤液，并对第一滤液进行浓缩和过滤，回收光卤石；
所述浮选尾盐为带有氯化钠固体的泡沫，不便于排出，将所述第一溢流液与之混合，即可方便的输送。另外，所述浮选尾盐中含有大量的氯化钠，利用所述第一溢流液进行溶解后，还可以用作回收氯化钠的原料。
所述分解母液用于所述冷结晶及粗钾筛分系统5中，用于结晶工序的料浆的分解。
所述第一滤液中含有细颗粒的光卤石，本发明将其浓缩后采用水平带机过滤回收细颗粒光卤石。
所述第一处理系统81可以包括尾盐澄清池、尾盐槽等，尾盐槽用于接收尾盐和第一溢流液，使得尾盐能够顺利输送。剩余的第一溢流液可以排放至尾盐澄清池，静置后排往光卤石盐田回收。
所述第二处理系统82可以是溶解罐，接收第三溢流液和第五溢流液，并加入淡水进行配置分解母液。
所述第三处理系统83包括浓密机和离心机或带式过滤机。
根据本发明的一个实施方式，所述低钠浓缩及脱卤系统4与所述浮选系统3连接，用于将所述第二溢流液输送至所述浮选系统3，用于调节调浆料浆的浓度。
所述第二溢流液优先输送至所述浮选系统3调节调浆料浆的浓度，多余的第二溢流液可以返回至光卤石盐田进行回收。
根据本发明的一个实施方式，所述粗钾浓缩及脱卤系统6与所述原矿处理系统1连接，用于将所述第四溢流液发送至原矿处理系统1调配光卤石矿 浆。
图3示出了所述第一处理系统的另一种示意图。
如图3所示，所述第一处理系统(81)还包括初级扫选槽811、次级扫选槽812、储存罐813，所述初级扫选槽811与所述浮选系统连接，用于接收浮选尾盐，并进行初级扫选，得到初级扫选泡沫和初级扫选底流；所述次级扫选槽812与所述初级扫选槽811连接，用于接收所述初级扫选底流并进行次级扫选，得到次级扫选泡沫和次级扫选底流；所述初级扫选槽811与所述尾盐池连接，用于将所述初级扫选泡沫输送至尾盐池；所述次级扫选槽812与所述储存罐813连接，用于将所述次级扫选底流输送至所述储存罐813；所述次级扫选槽812与所述低钠浓缩及脱卤系统连接，用于将所述次级扫选底流输送至所述低钠浓缩及脱卤系统。
所述初级扫选槽811将浮选尾盐泡沫进行初级扫选，得到初级扫选泡沫和初级扫选底流。其中，所述初级扫选泡沫中浮选药剂绝大部分与氯化钠结合，难以回收利用。同时，所述初级扫选泡沫中的氯化钾含量较低，其中的氯化钾在本系统内回收难以产生经济效益，本发明采取将初级扫选泡沫和第一溢流液排入尾盐池中进行处理。所述次级扫选槽812也设计成低于所述初级扫选槽811，使所述第一底流自流入所述次级扫选槽812，进行二级扫选，得到次级扫选泡沫和次级扫选底流。所述次级扫选底流也可以作为低钠料浆输送至低钠浓密机进行后续工序。所述次级扫选泡沫中含有大量的未与氯化钠结合的浮选药剂，以及在初选工序中与氯化钾结合，但在二次扫选时将氯化钾释放，进入泡沫的浮选药剂，这部分浮选药剂是本发明需要回收利用的部分。
将所述次级扫选泡沫收集到储存罐813中，由输送泵将所述次级扫选泡沫输送至浮选分配槽中，一方面，回收了浮选药剂，另一方面，所述次级扫选泡沫中的氯化钾含量比较高，也具备回收的价值，这种设置大幅度提高浮选效果，节省了浮选药剂，而且提高氯化钾的收率。
图4示出了原矿处理系统的示意图。
如图4所示，所述原矿处理系统1包括光卤石筛选机11、原矿浓密机12，所述光卤石筛选机11用于筛除光卤石矿浆中的杂物及大颗粒盐，得到筛下产 品；所述原矿浓密机12与所述光卤石筛选机11连接，用于将所述筛下产品浓缩，得到第一溢流液和第一底流矿浆，使所述第一底流矿浆固体质量含量：30—45％，所述原矿浓密机12为一个或多个。
光卤石矿浆经所述光卤石筛选机11，筛除杂物及大颗粒盐等，筛下产品进入原矿浓密机12浓缩，第一底流矿浆(固体质量含量：30％～35％)用底流泵送至调浆系统2，第一溢流液一部分用于和尾盐混合侯排出另一部分排往光卤石盐田回收利用。
所述原矿浓密机12可以是多个并列设置，即使某个浓密机出现故障，不影响整条生产线的运行。或者采用多用一备用的方式，保持总的原矿浓密机12处理能力稳定。
图5示出了调浆系统的示意图。
如图5所示，所述调浆系统2包括料浆分配槽21和调浆罐22，所述料浆分配槽21包括多个原矿浓密机12接口，用于与多个原矿浓密机12连接，接收所述第一底流料浆，将所述第一底流料浆与浮选药剂混合，并将所述第一底流料浆和所述浮选药剂分配至所述调浆罐22；所述调浆罐22与所述料浆分配槽21连接，用于将所述第一底流料浆和所述浮选药剂混合均匀得到调浆料浆。
所述料浆分配槽21接收来自原矿浓密机12的第一底流料浆，根据第一底流料浆中固体质量含量在料浆分配槽21中，添加浮选药剂，然后料浆进入调浆罐22，同时用空气压缩机输入0.5～0.7Mpa的空气进入调浆罐22底部的环形管道中，空气经环形管道上均匀分布的气孔中冒出大量大小适中的气泡，在调浆罐22中伴随的机械搅拌，氯化钠则选择性地向气泡附着，最后料浆进入浮选分配槽31，加入调浆母液调整浓度(固体质量含量：20％～25％)后进入浮选系统3。
所述料浆分配槽21与多个原矿浓密机12连接，将多个浓密机的底流料浆混合在一起，并将浮选药剂也进行混合，使得在浮选工序之前，调浆料浆的成分一致，也使得浮选药剂在调浆料浆中分布均匀，提高浮选效率。
图6示出了浮选系统的示意图。
如图6所示，所述浮选系统3包括浮选分配槽31、浮选机32，所述浮选 分配槽31，与所述调浆系统2连接，用于接收调浆料浆，并通过加入调节母液对所述调浆料浆进行浓度调节，得到调节料浆；所述调节料浆固体质量含量为20％～25％；所述调节母液是指与料浆母液同组分的液相；所述浮选机32与所述浮选分配槽31连接，用于将所述调节料浆进行粗选、精选和扫选作业，得到尾盐和低钠光卤石矿浆；所述浮选机32为一个或多个。
所述浮选分配槽31接收调浆料浆，并通过调节母液对其进行浓度的调节，之后将所述调节料浆输送至多个浮选机32，保证各浮选机32的物料成分一致，便于统一控制浮选机32的工作参数。浮选分为粗选、精选、扫选三个步骤，得到尾盐和低钠光卤石矿浆。
与原矿浓密机12类似的，浮选机32可以是一个或多个，浮选机32为多个时，浮选机32并列排列。增大本发明的处理能力。
浮选分配槽31使各浮选机32中的物料各种性质保持一致，方便统一设定浮选条件。
图7示出了低钠浓缩及脱卤系统的示意图。
如图7所示所述低钠浓缩及脱卤系统4包括低钠浓密机41、低钠离心机分配罐42和低钠离心机43，所述低钠浓密机41用于接收低钠光卤石矿浆并将所述低钠光卤石矿浆进行浓缩，得到第二底流矿浆和第二溢流液；所述第二底流矿浆固体质量含量为40％～45％；所述低钠浓密机41为一个或多个；所述低钠离心机分配罐42与所述低钠浓密机41连接，用于接收所述第二底流矿浆并将所述第二底流矿浆分配至低钠离心机43；所述低钠离心机43为一个或多个，与所述低钠离心机分配罐42连接，用于将所述第二底流矿浆进行脱卤，得到第一滤液和含湿≤10％低钠光卤石矿。
所述低钠浓密机41接收所述低钠光卤石矿，浓缩得到第二底流矿浆和第二溢流液，所述低钠浓密机41与浮选分配槽31连接，用于将所述第二溢流液输送至所述浮选分配槽31作为调节母液。所述低钠浓密机41通过控制底流流量与浓度使第二底流矿浆固体质量含量：40％～45％，以提高离心脱卤收率。同时，所述低钠浓密机41可以是多个浓密机并列与所述浮选机32连接，可以增大低钠浓密机41的处理能力。
所述低钠离心机分配罐42与所述低钠浓密机41连接，当本系统中含有 多个低钠浓密机41并联时，可以使各低钠浓密机41排出的第二底流矿浆在所述低钠离心机分配罐42中混合均匀，再分配至所述低钠离心机43中进行脱卤。
所述低钠离心机43可以是一个或者多个，当所述低钠离心机43为多个时，可以增大总体处理能力，并且当某个低钠离心机43出现故障时，可以使得整体生产线不受影响。
图8示出了冷结晶及粗钾筛分系统的示意图。
如图8所示，所述冷结晶及粗钾筛分系统5包括结晶器51和粗钾筛选机52，所述结晶器51为一个或多个，用于接收所述含湿≤10％低钠光卤石矿并分解结晶，得到第三底流矿浆和第三溢流液；所述第三底流矿浆固体质量含量15％～30％；所述粗钾筛选机52与所述结晶器51连接，用于将所述第三底流料浆进行筛分，得到粗钾筛上物和粗钾筛下物。
所述结晶器51与低钠离心机43连接，离心后的含湿≤10％低钠光卤石矿进入结晶器51，同时加入分解母液，将低钠光卤石矿进行控速分解结晶，利用控制低钠光卤石矿分解条件，来控制溶液中氯化钾过饱和度，减少氯化钾晶体数量，达到在常温下使氯化钾晶体长大目的，而氯化钠为液相处于不饱状态不能析出，保证了氯化钾产品质量和粒度。得到第三底流矿浆和第三溢流液。所述第三底流料浆的固体质量含量为17％～27％，送至粗钾选机筛进行筛分作业，未分解的筛上物粗粒光卤石返回结晶器51再次分解，粗钾筛下物进入粗钾浓密机61。所述第三溢流液由所述溢流液和滤液处理系统8处理，用于配置分解母液。
图9示出了粗钾浓缩及脱卤系统的示意图。
如图9所示，所述粗钾浓缩及脱卤系统6包括粗钾浓密机61、粗钾离心机分配罐62和粗钾离心机63，所述粗钾浓密机61为一个或多个，用于接收并浓缩所述粗钾筛下物，得到第四溢流液和第四底流矿浆；所述第四底流料浆固体质量含量为40％～45％；所述粗钾离心机分配罐62与所述粗钾浓密机61连接，用于接收所述第四底流料浆，并将所述第四底流料浆分配至各粗钾离心机63；所述粗钾离心机63为一个或多个，与所述粗钾离心机分配罐62连接，用于将所述第四底流料浆进行脱卤，得到第二滤液和含湿≤10％粗钾 矿。
所述粗钾浓密机61接收粗钾筛下物，进行浓缩后得到第四底流矿浆和第四溢流液。所述第四底流矿浆的固体质量含量为40％～45％，输送至粗钾离心机分配罐62均匀分配至粗钾离心机63进行脱卤，得到第二滤液。
其中，所述粗钾浓密机61与原矿处理系统1的原矿浓密机12连接，用于将所述第四溢流液输送至所述原矿浓密机12回收其中的光卤石。
所述粗钾离心机63和所述粗钾浓密机61连接，所述第二滤液从所述粗钾离心机63输送至粗钾浓密机61回收利用。
根据本发明的一个实施方式，所述粗钾离心机63与所述粗钾浓密机61连接，用于将所述第二滤液输送至所述粗钾浓密机61回收利用。
图10示出了精钾洗涤及脱卤系统的示意图。
如图10所示，所述精钾洗涤及脱卤系统7包括再浆洗涤罐71、精钾浓密机72和精钾离心机73，所述再浆洗涤罐71为一个或多个，用于接收所述含湿≤10％粗钾矿并进行洗涤得到再浆洗料浆；所述精钾浓密机72为一个或多个，与所述再浆洗罐相匹配，用于浓缩所述再浆洗料浆，得到第五底流料浆；所述精钾离心机73为一个或多个，与所述精钾浓密机72相匹配，用于对第五底流料浆进行脱卤，得到精钾矿和第三滤液；所述精钾矿含湿量≤10％。
根据本发明的一个实施方式，所述精钾浓密机72与所述再浆洗罐连接，用于利用所述第五底流料浆调节所述含湿≤10％粗钾矿的浓度。所述精钾浓密机72与所述精钾离心机73连接，用于将所述第三滤液回收至所述精钾浓密机72进行浓缩。
粗钾离心机63离心后得到含湿量≤10％粗钾矿，进入再浆洗涤罐71内，根据电导率加入淡水，利用精钾浓密机72的第五底流矿浆调整再浆洗涤罐71内的料浆浓度达到固体质量含量：40％～45％，洗涤后的料浆进入精钾浓密机72进行浓缩，得到第五溢流液和第五底流矿浆。所述第五底流矿浆大部分进入所述精钾离心机73进行脱卤，得到氯化钾湿料(精钾矿，含湿量≤10％)，一部分用于调整再浆洗涤罐71内的料浆浓度。
所述第三滤液返至精钾浓密机72回收。
所述第五溢流液由所述溢流液和滤液处理系统8回收用于配置结晶器51 用的分解母液。
图11示出了一种可回收利用副产物的生产氯化钾的方法的步骤示意图。
如图11所示，一种可回收利用副产物的生产氯化钾的方法，包括，第一步骤S1，将光卤石矿浆进行筛分和浓缩，得到第一底流矿浆和第一溢流液；第二步骤S2，将浮选药剂与所述第一底流料浆混合，得到调浆料浆；第三步骤S3，对所述调浆料浆进行浮选作业，得到尾盐和低钠光卤石料浆；第四步骤S4，将所述低钠光卤石料浆进行浓缩并脱除卤水，得到第二溢流液、第一滤液和含湿≤10％低钠光卤石矿；第五步骤S5，将所述含湿≤10％低钠光卤石矿进行分解结晶，并进行筛分，得到第三溢流液、粗钾筛上物和粗钾筛下物；第六步骤S6，将所述粗钾筛下物进行浓缩和脱卤，得到第四溢流液、第二滤液和含湿≤10％粗钾矿；第七步骤S7，将所述含湿≤10％粗钾矿进行洗涤和脱卤，得到第三滤液和精钾矿；第八步骤S8，回收处理所述第一溢流液、第三溢流液、第五溢流液和第一滤液。
根据本发明的一个实施方式，所述第八步骤S8包括，将所述第一溢流液与所述浮选尾盐进行调浆后排出；接收第三溢流液和第五溢流液，经淡水调节后，用作结晶工艺的分解母液；接收第一滤液，并对第一滤液进行浓缩和过滤，回收光卤石。
根据本发明的一个实施方式，还包括将所述浮选尾盐进行初级扫选，得到初级扫选泡沫和初级扫选底流；将所述初级扫选底流并进行次级扫选，得到次级扫选泡沫和次级扫选底流；将所述初级扫选泡沫与所述第一溢流液调浆后输送至尾盐池；将所述次级扫选底流输所述低钠浓缩及脱卤系统。
根据本发明的一个实施方式，将所述第二溢流液输用于调节调浆料浆的浓度。
根据本发明的一个实施方式，将所述第四溢流液用于调配光卤石矿浆。
根据本发明的一个实施方式，所述第一步骤S1包括，筛除光卤石矿浆中的杂物及大颗粒盐，得到筛下产品；将所述筛下产品浓缩，得到第一溢流液和第一底流矿浆，使所述第一底流矿浆固体质量含量：30％～45％；所述光卤石矿浆的固体质量含量≥25％。
根据本发明的一个实施方式，所述第二步骤S2包括，将所述第一底流料 浆与浮选药剂混合，并将所述第一底流料浆和所述浮选药剂进行分配；将所述第一底流料浆和所述浮选药剂混合均匀得到调浆料浆。
根据本发明的一个实施方式，所述第三步骤S3包括，通过加入调节母液对所述调浆料浆进行浓度调节，得到调节料浆；所述调节料浆固体质量含量为20％～25％；所述调节母液是指与料浆母液同组分的液相；将所述调节料浆进行粗选、精选和扫选作业，得到尾盐和低钠光卤石矿浆。
根据本发明的一个实施方式，所述第四步骤S4包括，将所述低钠光卤石矿浆进行浓缩，得到第二底流矿浆和第二溢流液；所述第二底流矿浆固体质量含量为40％～45％；将所述第二底流矿浆进行分配；将所述第二底流矿浆进行脱卤，得到第一滤液和含湿≤10％低钠光卤石矿。
根据本发明的一个实施方式，所述第五步骤S5包括，将所述含湿≤10％低钠光卤石矿与分解母液混合，进行控速分解结晶，得到第三底流矿浆和第三溢流液；所述第三底流矿浆固体质量含量15％～30％；将所述第三底流料浆进行筛分作业，得到粗钾筛上物和粗钾筛下物。
根据本发明的一个实施方式，所述第六步骤S6包括，浓缩所述粗钾筛下物，得到第四溢流液和第四底流矿浆；所述第四底流料浆固体质量含量为40％～45％；将所述第四底流料浆进行分配；将所述第四底流料浆进行脱卤，得到第二滤液和含湿≤10％粗钾矿。
根据本发明的一个实施方式，将所述第二滤液输送至浓缩所述粗钾筛下物的工序回收利用。
根据本发明的一个实施方式，所述第七步骤S7包括，将所述含湿≤10％粗钾矿进行洗涤得到再浆洗料浆；浓缩所述再浆洗料浆，得到第五底流料浆；将所述第五底流料浆进行脱卤，得到精钾矿和第三滤液；所述精钾矿含湿量≤10％。
根据本发明的一个实施方式，在再浆洗工序中利用所述第五底流料浆调节所述含湿≤10％粗钾矿的浓度。将所述第三滤液回收至再浆洗料浆浓缩工序进行浓缩。
本发明通过将第一溢流液、第三溢流液、第五溢流液和第一滤液分别进行收集回用至系统中，在系统内回收氯化钾，以及替代外来物料的加入，一 方面增加了氯化钾的产率，另一方面节约了成本。本发明在原矿浓密机12、浮选机32、低钠浓密机41等设备的多个并联，调浆罐22统一调浆、分散分配等方式，使得对物料的处理浓度统一的同时，各并联设备之间互成备用关系，即使某个设备故障或者需要检修，不影响整体工艺的运行。
应该注意的是，上述实施例对本发明进行说明而不是对本发明进行限制，并且本领域技术人员在不脱离所附权利要求的范围的情况下可设计出替换实施例。在权利要求中，不应将位于括号之间的任何参考符号构造成对权利要求的限制。

Claims (28)

  1. 一种可回收利用副产物的生产氯化钾的系统，包括，原矿处理系统(1)、调浆系统(2)、浮选系统(3)、低钠浓缩及脱卤系统(4)、冷结晶及粗钾筛分系统(5)、粗钾浓缩及脱卤系统(6)，精钾洗涤及脱卤系统(7)，还包括溢流液和滤液处理系统(8)，
    所述原矿处理系统(1)用于将光卤石矿浆进行筛分和浓缩，得到第一底流矿浆和第一溢流液；
    所述调浆系统(2)与所述原矿处理系统(1)连接，用于将浮选药剂与所述第一底流料浆混合，得到调浆料浆；
    所述浮选系统(3)用于对所述调浆料浆进行浮选作业，得到尾盐和低钠光卤石料浆；
    所述低钠浓缩及脱卤系统(4)与所述浮选系统(3)连接，用于将所述低钠光卤石料浆进行浓缩并脱除卤水，得到第二溢流液、第一滤液和含湿≤10％低钠光卤石矿；
    所述冷结晶及粗钾筛分系统(5)与所述低钠浓缩及脱卤系统(4)连接，用于将含湿≤10％低钠光卤石矿进行分解结晶，并进行筛分，得到第三溢流液、粗钾筛上物和粗钾筛下物；
    所述粗钾浓缩及脱卤系统(6)与所述冷结晶及粗钾筛分系统(5)连接，用于将所述粗钾筛下物进行浓缩和脱卤，得到第四溢流液、第二滤液和含湿≤10％粗钾矿；
    所述精钾洗涤及脱卤系统(7)与所述粗钾浓缩及脱卤系统(6)连接，用于将所述含湿≤10％粗钾矿进行洗涤和脱卤，得到第三滤液和精钾矿；
    所述溢流液和滤液处理系统(8)用于回收处理所述第一溢流液、第三溢流液、第五溢流液和第一滤液。
  2. 根据权利要求1所述的系统，其中，所述溢流液和滤液处理系统(8)包括第一处理系统(81)、第二处理系统(82)、第三处理系统(83)，
    所述第一处理系统(81)分别与所述原矿处理系统(1)、浮选系统(3) 连接，用于从所述原矿处理系统(1)接收第一溢流液，从所述浮选系统(3)接收浮选尾盐，将所述第一溢流液与所述浮选尾盐进行调浆后排出；
    所述第二处理系统(82)分别与所述冷结晶及粗钾筛分系统(5)和精钾洗涤及脱卤系统(7)连接，用于从所述冷结晶及粗钾筛分系统(5)接收第三溢流液，从所述精钾洗涤及脱卤系统(7)接收第五溢流液，经淡水调节后，输送至冷结晶及粗钾筛分系统(5)用作分解母液；
    所述第三处理系统(83)与所述低钠浓缩及脱卤系统(4)连接，用于接收第一滤液，并对第一滤液进行浓缩和过滤，回收光卤石。
  3. 根据权利要求1所述的系统，其中所述第一处理系统(81)还包括初级扫选槽(811)、次级扫选槽(812)、储存罐(813)，
    所述初级扫选槽(811)与所述浮选系统连接，用于接收浮选尾盐，并进行初级扫选，得到初级扫选泡沫和初级扫选底流；
    所述次级扫选槽(812)与所述初级扫选槽(811)连接，用于接收所述初级扫选底流并进行次级扫选，得到次级扫选泡沫和次级扫选底流；
    所述初级扫选槽(811)与所述尾盐池连接，用于将所述初级扫选泡沫输送至尾盐池；
    所述次级扫选槽(812)与所述储存罐(813)连接，用于将所述次级扫选底流输送至所述储存罐(813)；
    所述次级扫选槽(812)与所述低钠浓缩及脱卤系统连接，用于将所述次级扫选底流输送至所述低钠浓缩及脱卤系统。
  4. 根据权利要求1所述的系统，其中，所述低钠浓缩及脱卤系统(4)与所述浮选系统(3)连接，用于将所述第二溢流液输送至所述浮选系统(3)，用于调节调浆料浆的浓度。
  5. 根据权利要求1所述的系统，其中，所述粗钾浓缩及脱卤系统(6)与所述原矿处理系统(1)连接，用于将所述第四溢流液发送至原矿处理系统(1)浓缩利用。
  6. 根据权利要求1所述的系统，其中，所述原矿处理系统(1)包括光卤石筛选机(11)、原矿浓密机(12)，
    所述光卤石筛选机(11)用于筛除光卤石矿浆中的杂物及大颗粒盐，得 到筛下产品；
    所述原矿浓密机(12)与所述光卤石筛选机(11)连接，用于将所述筛下产品浓缩，得到第一溢流液和第一底流矿浆，使所述第一底流矿浆固体质量含量：30—45％，
    所述原矿浓密机(12)为一个或多个。
  7. 根据权利要求1所述的系统，其中，所述调浆系统(2)包括料浆分配槽(21)和调浆罐(22)，
    所述料浆分配槽(21)包括多个原矿浓密机(12)接口，用于与多个原矿浓密机(12)连接，接收所述第一底流料浆，将所述第一底流料浆与浮选药剂混合，并将所述第一底流料浆和所述浮选药剂分配至所述调浆罐(22)；
    所述调浆罐(22)与所述料浆分配槽(21)连接，用于将所述第一底流料浆和所述浮选药剂混合均匀得到调浆料浆。
  8. 根据权利要求1所述的系统，其中所述浮选系统(3)包括浮选分配槽(31)、浮选机(32)，
    所述浮选分配槽(31)，与所述调浆系统(2)连接，用于接收调浆料浆，并通过加入调节母液对所述调浆料浆进行浓度调节，得到调节料浆；
    所述调节料浆固体质量含量为20％～25％；
    所述调节母液是指与料浆母液同组分的液相；
    所述浮选机(32)与所述浮选分配槽(31)连接，用于将所述调节料浆进行粗选、精选和扫选作业，得到尾盐和低钠光卤石矿浆；
    所述浮选机(32)为一个或多个。
  9. 根据权利要求1所述的系统，其中，所述低钠浓缩及脱卤系统(4)包括低钠浓密机(41)、低钠离心机分配罐(42)和低钠离心机(43)，
    所述低钠浓密机(41)用于接收低钠光卤石矿浆并将所述低钠光卤石矿浆进行浓缩，得到第二底流矿浆和第二溢流液；
    所述第二底流矿浆固体质量含量为40％～45％；
    所述低钠浓密机(41)为一个或多个；
    所述低钠离心机分配罐(42)与所述低钠浓密机(41)连接，用于接收所述第二底流矿浆并将所述第二底流矿浆分配至低钠离心机(43)；
    所述低钠离心机(43)为一个或多个，与所述低钠离心机分配罐(42)连接，用于将所述第二底流矿浆进行脱卤，得到第一滤液和含湿≤10％低钠光卤石矿。
  10. 根据权利要求1所述的系统，其中，所述冷结晶及粗钾筛分系统(5)包括结晶器(51)和粗钾筛选机(52)，
    所述结晶器(51)为一个或多个，用于接收所述含湿≤10％低钠光卤石矿并分解结晶，得到第三底流矿浆和第三溢流液；
    所述第三底流矿浆固体质量含量15％～30％；
    所述粗钾筛选机(52)与所述结晶器(51)连接，用于将所述第三底流料浆进行筛分，得到粗钾筛上物和粗钾筛下物。
  11. 根据权利要求1所述的系统，其中，所述粗钾浓缩及脱卤系统(6)包括粗钾浓密机(61)、粗钾离心机分配罐(62)和粗钾离心机(63)，
    所述粗钾浓密机(61)为一个或多个，用于接收并浓缩所述粗钾筛下物，得到第四溢流液和第四底流矿浆；
    所述第四底流料浆固体质量含量为40％～45％；
    所述粗钾离心机分配罐(62)与所述粗钾浓密机(61)连接，用于接收所述第四底流料浆，并将所述第四底流料浆分配至各粗钾离心机(63)；
    所述粗钾离心机(63)为一个或多个，与所述粗钾离心机分配罐(62)连接，用于将所述第四底流料浆进行脱卤，得到第二滤液和含湿≤10％粗钾矿。
  12. 根据权利要求11所述的系统，其中，所述粗钾离心机(63)与所述粗钾浓密机(61)连接，用于将所述第二滤液输送至所述粗钾浓密机(61)回收利用。
  13. 根据权利要求1所述的系统，其中，所述精钾洗涤及脱卤系统(7)包括再浆洗涤罐(71)、精钾浓密机(72)和精钾离心机(73)，
    所述再浆洗涤罐(71)为一个或多个，用于接收所述含湿≤10％粗钾矿并进行洗涤得到再浆洗料浆；
    所述精钾浓密机(72)为一个或多个，与所述再浆洗罐相匹配，用于浓缩所述再浆洗料浆，得到第五底流料浆；
    所述精钾离心机(73)为一个或多个，与所述精钾浓密机(72)相匹配，用于对第五底流料浆进行脱卤，得到精钾矿和第三滤液；
    所述精钾矿含湿量≤10％。
  14. 根据权利要求13所述的系统，其中，所述精钾浓密机(72)与所述再浆洗罐连接，用于利用所述第五底流料浆调节所述含湿≤10％粗钾矿的浓度。
    所述精钾浓密机(72)与所述精钾离心机(73)连接，用于将所述第三滤液回收至所述精钾浓密机(72)进行浓缩。
  15. 一种可回收利用副产物的生产氯化钾的方法，包括，
    第一步骤(S1)，将光卤石矿浆进行筛分和浓缩，得到第一底流矿浆和第一溢流液；
    第二步骤(S2)，将浮选药剂与所述第一底流料浆混合，得到调浆料浆；
    第三步骤(S3)，对所述调浆料浆进行浮选作业，得到尾盐和低钠光卤石料浆；
    第四步骤(S4)，将所述低钠光卤石料浆进行浓缩并脱除卤水，得到第二溢流液、第一滤液和含湿≤10％低钠光卤石矿；
    第五步骤(S5)，将所述含湿≤10％低钠光卤石矿进行分解结晶，并进行筛分，得到第三溢流液、粗钾筛上物和粗钾筛下物；
    第六步骤(S6)，将所述粗钾筛下物进行浓缩和脱卤，得到第四溢流液、第二滤液和含湿≤10％粗钾矿；
    第七步骤(S7)，将所述含湿≤10％粗钾矿进行洗涤和脱卤，得到第三滤液和精钾矿；
    第八步骤(S8)，回收处理所述第一溢流液、第三溢流液、第五溢流液和第一滤液。
  16. 根据权利要求15所述的方法，其中，所述第八步骤(S8)包括，
    将所述第一溢流液与所述浮选尾盐进行调浆后排出；
    接收第三溢流液和第五溢流液，经淡水调节后，用作结晶工艺的分解母液；
    接收第一滤液，并对第一滤液进行浓缩和过滤，回收光卤石。
  17. 根据权利要求16所述的方法，其中还包括将所述浮选尾盐进行初级扫选，得到初级扫选泡沫和初级扫选底流；
    将所述初级扫选底流并进行次级扫选，得到次级扫选泡沫和次级扫选底流；
    将所述初级扫选泡沫与所述第一溢流液调浆后输送至尾盐池；
    将所述次级扫选底流输所述低钠浓缩及脱卤系统。
  18. 根据权利要求15所述的方法，将所述第二溢流液用于调节调浆料浆的浓度。
  19. 根据权利要求15所述的方法，将所述第四溢流液用于调配光卤石矿浆。
  20. 根据权利要求15所述的方法，其中，所述第一步骤(S1)包括，
    筛除光卤石矿浆中的杂物及大颗粒盐，得到筛下产品；
    将所述筛下产品浓缩，得到第一溢流液和第一底流矿浆，使所述第一底流矿浆固体质量含量：30％～45％；
    所述光卤石矿浆的固体质量含量≥25％。
  21. 根据权利要求15所述的方法，其中，所述第二步骤(S2)包括，
    将所述第一底流料浆与浮选药剂混合，并将所述第一底流料浆和所述浮选药剂进行分配；
    将所述第一底流料浆和所述浮选药剂混合均匀得到调浆料浆。
  22. 根据权利要求15所述的方法，其中，所述第三步骤(S3)包括，
    通过加入调节母液对所述调浆料浆进行浓度调节，得到调节料浆；
    所述调节料浆固体质量含量为20％～25％；
    所述调节母液是指与料浆母液同组分的液相；
    将所述调节料浆进行粗选、精选和扫选作业，得到尾盐和低钠光卤石矿浆。
  23. 根据权利要求15所述的方法，其中，所述第四步骤(S4)包括，
    将所述低钠光卤石矿浆进行浓缩，得到第二底流矿浆和第二溢流液；
    所述第二底流矿浆固体质量含量为40％～45％；
    将所述第二底流矿浆进行分配；
    将所述第二底流矿浆进行脱卤，得到第一滤液和含湿≤10％低钠光卤石矿。
  24. 根据权利要求15所述的方法，其中，所述第五步骤(S5)包括，
    将所述含湿≤10％低钠光卤石矿与分解母液混合，进行控速分解结晶，得到第三底流矿浆和第三溢流液；
    所述第三底流矿浆固体质量含量15％～30％；
    将所述第三底流料浆进行筛分作业，得到粗钾筛上物和粗钾筛下物。
  25. 根据权利要求15所述的方法，其中，所述第六步骤(S6)包括，
    浓缩所述粗钾筛下物，得到第四溢流液和第四底流矿浆；
    所述第四底流料浆固体质量含量为40％～45％；
    将所述第四底流料浆进行分配；
    将所述第四底流料浆进行脱卤，得到第二滤液和含湿≤10％粗钾矿。
  26. 根据权利要求25所述的方法，其中，将所述第二滤液输送至浓缩所述粗钾筛下物的工序回收利用。
  27. 根据权利要求15所述的方法，其中，所述第七步骤(S7)包括，
    将所述含湿≤10％粗钾矿进行洗涤得到再浆洗料浆；
    浓缩所述再浆洗料浆，得到第五底流料浆；
    将所述第五底流料浆进行脱卤，得到精钾矿和第三滤液；
    所述精钾矿含湿量≤10％。
  28. 根据权利要求27所述的方法，在再浆洗工序中利用所述第五底流料浆调节所述含湿≤10％粗钾矿的浓度；将所述第三滤液回收至再浆洗料浆浓缩工序进行浓缩。
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