WO2013091403A1 - 利用光卤石矿井采卤水生产氯化钾、氯化钠及镁片的方法 - Google Patents

利用光卤石矿井采卤水生产氯化钾、氯化钠及镁片的方法 Download PDF

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WO2013091403A1
WO2013091403A1 PCT/CN2012/081014 CN2012081014W WO2013091403A1 WO 2013091403 A1 WO2013091403 A1 WO 2013091403A1 CN 2012081014 W CN2012081014 W CN 2012081014W WO 2013091403 A1 WO2013091403 A1 WO 2013091403A1
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tank
carnallite
hot
sent
potassium chloride
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PCT/CN2012/081014
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English (en)
French (fr)
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冯跃华
陈伟来
刘小力
杨晓烽
周作其
孙成高
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化工部长沙设计研究院
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Publication of WO2013091403A1 publication Critical patent/WO2013091403A1/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
    • C01D3/08—Preparation by working up natural or industrial salt mixtures or siliceous minerals
    • 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
    • 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
    • C22B26/20—Obtaining alkaline earth metals or magnesium
    • C22B26/22—Obtaining magnesium

Definitions

  • the present invention relates to a method for producing potassium chloride, sodium chloride and magnesium flakes by using brine in a carnallite mine, and in particular to a method for producing potassium chloride by using a 3 ⁇ 4 stone hydrothermal decomposition method.
  • China is a country with a serious shortage of potassium resources.
  • the cultivated land is generally deficient in potassium, and the contradiction between supply and demand of potash fertilizer is very prominent.
  • the domestic potassium fertilizer satisfaction rate only accounts for about 30%, and the annual imported potassium fertilizer reaches 4000kt (K 2 0) or more.
  • China's potash consumption will also have a high annual growth rate. It is estimated that by 2020, China's potash consumption will reach lOOOOkt (K 2 0), and the market space is broad.
  • the main production methods for preparing potassium chloride from domestic carnallite mines are: cold decomposition-flotation method, cold decomposition-hot melt crystallization method, reverse flotation-cold crystallization method, and sodium-desulfurization controlled decomposition method.
  • the carnallite mines in the salt lakes are generally open-pit mining on the ground or mined from the beaches. It is more appropriate to use the above method to prepare potassium chloride. For the deep underground carnallite mines, the depth of open pit mining is limited and the vegetation is seriously damaged. The accumulated impurities and waste salts accumulate to cause environmental pollution.
  • Underground mining includes conventional solid mining and drilling water-soluble mining.
  • the present invention mainly relates to a method for processing brine produced by a well water-soluble method. If normal temperature plus fresh water is used, the difference in solubility between potassium chloride and sodium chloride at low temperature is small. In the subsequent stage of preparation of potassium chloride, a large amount of waste salt will also accumulate, and in order not to cause geological hazard, waste salt is needed. Backfilling adds a lot of cost.
  • the invention aims to provide a method for producing potassium chloride and chlorine by thermal decomposition of brine in a carnallite mine.
  • the filtrate is decomposed into the mother liquor and sent to the step (2) evaporation concentration process; the obtained potassium salt cake is fresh water or from the step (5)
  • the mother liquor of potassium chloride crystals is washed according to the mass ratio of the mother liquor or the fresh water and potassium salt cakes to a ratio of 1:1.5 to 3, and then sent to the step (5) to thermally dissolve the crystals, and the washing liquid is discharged back to the decomposition of the carnallite.
  • the decomposed mother liquor from the step (1) is preheated to 135 ⁇ 145 ° C for evaporation concentration.
  • the boiling point of the evaporation chamber reaches the temperature of 24 ⁇ 27 ° C
  • the discharge is discharged, and the evaporated mother liquor is discharged to the five-stage series of hawite.
  • the crystallizer is cooled and crystallized, the crystallization temperature is gradually reduced, the temperature of each stage is 18 ⁇ 22 ° C, the cooling crystallization end temperature is 35 ⁇ 45 ° C, and the final crystallizer slurry enters the step (3) carnallite separation process;
  • the slurry from the final stage (2) crystallizer is sent to the thickener, and the thickener overflows the old brine from the pump to the magnesium sheet production workshop, the old brine pool and the cold injection tank;
  • the overflow old brine in the production workshop accounts for 5 ⁇ 8% of the total mass of the overflow old brine, 15 ⁇ 18% for the backfill of the old brine pool, and 75 ⁇ 80% for the cold injection tank;
  • the quality of the lower underflow solid material accounts for 35% ⁇ 55% of the total mass of the material, and is separated by filtration.
  • the obtained filter cake is returned to the step (1), and the filtrate is recirculated into the overflow old brine;
  • Hot solution The potassium salt cake from the step (1) and the second hot solution of the step are firstly hot-dissolved, and the first hot solution time is controlled for 15 to 30 minutes, and the hot solution temperature is 90 to 95°.
  • the first hot melt slurry enters the thickener thickening, and the quality of the underlying solid material is controlled to be 35% ⁇ 55 % of the total mass of the material.
  • the overflow of the top of the thickener is sent to the high temperature mother liquor tank, and the underflow slurry is heated by the secondary preheating.
  • the underflow solid material is sent to the step (6) salt washing process; crystallization: the hot melt slurry in the high temperature mother liquor tank is pumped to the three-stage series potassium chloride crystallizer, and controlled The temperature of the first, second and third stage crystallization mother liquids are 70 ⁇ 75°C, 57 ⁇ 63 °C, 30 respectively. At 40 °C, the slurry is discharged from the third-stage crystallizer to the thickener to thicken, and the quality of the solid material in the bottom of the thickener is controlled to be 35% ⁇ 55 % of the total mass of the material. The thickened bottom material is sent to the centrifuge for centrifugation.
  • the filtrate flows to the low temperature mother liquor storage tank, the filter cake is sent to the potassium chloride washing salt tank, the washing time is controlled for 15 to 30 minutes, the solid-liquid mass ratio is controlled to 1: 2 ⁇ 3, and the slurry is sent to the cyclone;
  • the mass of the solid material in the underflow of the cyclone accounts for 45 ⁇ 55 % of the total mass of the material, the underflow material enters the precision potassium centrifuge to filter, the filtrate returns to the potassium chloride washing salt tank, and the filter cake is sent to the step (6) potassium chloride drying process;
  • the thickener overflow mother liquor and the centrifugally separated filtrate are transferred to the low temperature mother liquor storage tank, they are mixed with the secondary steam from the secondary crystallizer to be heated to 40 to 50 ° C, and mixed with the secondary steam from the primary crystallizer.
  • the bottom salt slurry from the cyclone (5) hot-dissolving process enters the centrifuge for centrifugation, and the filtrate returns to the first-stage hot-dissolving tank.
  • the filter cake enters the two-stage series of sodium chloride washing tank and washes the salt with fresh water to wash the salt. Time 30 ⁇ 50 minutes, the mass ratio of washing salt solid-liquid is controlled at 1: 2 ⁇ 3, the slurry is sent to the current cyclone; the top stream of the cyclone enters the settler, and the bottom of the settler returns to the first-stage salt washing tank.
  • the overflow of the settler is discharged into the waste water tank; the quality of the solid material in the underflow of the cyclone is controlled to be 45 ⁇ 55 % of the total mass of the material, and the centrifuge is centrifuged, the filtrate is returned to the first-stage salt washing tank, and the sodium chloride filter cake is fluidized. 5 ⁇ ⁇ After drying, the water content is 0. 5wt%, NaCl content 98. 5wt Q / ⁇ sodium chloride product;
  • the potassium chloride product from the step (5) crystallization step enters the potassium chloride drying cooler, and the potassium chloride product obtained after drying, the water content is 1 wt%, KC1 ⁇ 95 wt%;
  • the old halogen from the step (3) carnallite separation process is fed into the two-effect evaporation system, and the pressure of the I effect evaporation chamber is controlled to be 0. 11 ⁇ 0. 13Mpa, the temperature is 102 ⁇ 108 °C, and the pressure of the II effect evaporation chamber is 0. 11 ⁇ 0. 13Mpa, temperature is 57 ⁇ 63°C, using II effect countercurrent feed, I effect discharge, discharge control point is MgCl 2 mass fraction 45% ⁇ 48%, discharge into cooling/slicing Machine, made of magnesium.
  • step (4) the preferred temperature for the steam preheating to the hot injection tank is 90 ⁇ 93.
  • the method for thermally decomposing carnallite to produce industrial potassium chloride, magnesium flakes and sodium chloride according to the phase diagram theory of K + , Na ⁇ Mg 2+ ⁇ C1—H 2 0 quaternary water salt system, using heat Decomposition, carnallite evaporation crystallization, hot melt, separation, multi-stage series vacuum cold precipitation crystallization, separation and drying to obtain the finished potassium chloride.
  • Magnesium and sodium in the old brine can be adjusted to produce corresponding products such as magnesium flakes and sodium chloride according to market conditions, and the waste can be used for waste well filling.
  • the present invention has the following significant advantages:
  • the original halogen decomposition of carnallite can greatly reduce the amount of water added to the system and reduce the evaporation of the system; (2) using one-effect evaporation, multi-stage flash vacuum cooling of crystalline carnallite, evaporation of secondary steam for preheating decomposition of mother liquor , flashing secondary steam for preheating the mineral injection and raw halogen, rational use of energy; (3) Potassium salt hot solution process using two sections of hot solution, potassium salt is fully dissolved, the potassium content of the waste salt is low, Potassium yield is high; (4) Potassium chloride vacuum cooling crystallization process makes full use of the residual heat of the secondary steam to heat the mother liquor, reducing the consumption of hot-dissolved steam, and also reducing the amount of cooling circulating water; (5) Old halogen is used for preparation The replacement of the agent and the waste well can adjust the production of magnesium flakes and industrial salt products according to market conditions, and completely solve the problem of waste discharge caused by the production of potassium chloride by the carburizing type potassium salt deposit by the
  • the present invention utilizes a hot injection agent to dissolve ore, and the solubility of potassium chloride at a high temperature is much greater than that of sodium chloride and magnesium chloride, thereby greatly reducing the recovery rate of sodium chloride and magnesium chloride when producing potassium chloride in a unit yield.
  • the amount of waste salt discharged from the subsequent process is reduced, the amount of backfilling work is also significantly reduced, a large amount of cost is saved, and the potassium and magnesium resources in the carnallite are comprehensively utilized, and the economic benefit is considerable.
  • the decomposition of the mother liquor, that is, the filtrate, is sent to the evaporation concentration step;
  • the obtained potassium salt cake is prepared by using the potassium chloride crystal mother liquor from the step (4) according to the mother liquor: potassium stone.
  • the salt cake has a mass ratio of 1:2 for washing,
  • the initial production is washed with fresh water; after washing, it is sent to the step (4) for hot solution crystallization, and the washing liquid is discharged back to the carnallite decomposition stirring tank;
  • the decomposed mother liquor from the step (1) is preheated to 14 CTC for evaporation concentration.
  • the discharge is discharged, and the evaporated mother liquid is discharged to the five-stage series of carnallite crystallizer for cooling and crystallization.
  • the crystallization temperature is gradually reduced, the temperature of each stage is 20 ° C, the cooling crystallization end temperature is 40 ° C, and the final crystallizer slurry enters the step (3) carnallite separation process;
  • the slurry from the final stage (2) crystallizer is sent to the thickener, and the thickener overflows the old brine from the pump to the magnesium sheet production workshop, the old brine pool and the cold injection tank;
  • the overflow old brine in the production workshop accounts for 7% of the total mass of the overflow old brine, 17% for the backfill of the old brine pool, and 76% for the cold injection tank.
  • the quality of the underlying solid material in the lower part of the thickener is controlled. 45% of the total mass of the material, separated by filtration, and the obtained filter cake, that is, the carnallite, is returned to the step (1), and the filtrate is sent to the overflow old brine;
  • the flashing secondary steam of the step (2) crystallizer is introduced into the cold injection tank, mixed with 76% of the overflow old halogen mass fraction from the step (3), heated to 58 ° C, and sent to the hot injection.
  • the tank is preheated to 88 ° C with steam to form a well heat injection agent;
  • Hot solution The potassium salt from the step (1) and the second hot solution of the solution are firstly hot-dissolved, and the first hot solution time is controlled for 20 minutes, the hot solution temperature is 92 ° C, and the first stage is hot.
  • the slurry enters the thickener to thicken, and the quality of the underlying solid material is controlled to be 40% of the total mass of the material.
  • the overflow of the thickener is sent to the high temperature mother liquor tank, and the underflow slurry is heated to 107 ° C for two-stage stirring by secondary preheating.
  • the tank, the subsequent potassium chloride crystal is centrifuged to separate the filtrate, and is also returned to the second hot-melt stirred tank for secondary heat-dissolving, controlling the secondary hot-dissolving time 20 Minute, the hot solution temperature is 94 °C, the second hot melt slurry is sent to the cyclone, and the top stream of the cyclone is the second hot solution mother liquor returned to the first stage hot melt tank, and the quality of the solid material in the underflow of the cyclone is controlled. 48% of the mass, the underflow solid material is sent to the step (6) salt washing process;
  • Crystallization The hot-melt slurry in the high-temperature mother liquor tank is pumped to a three-stage series potassium chloride crystallizer to control the temperature of the first, second and third-grade crystallization mother liquors to be 75 °C, 63 °C, 40 °C, respectively.
  • the slurry is discharged from the third stage crystallizer to the thickener to thicken, and the quality of the solid material in the bottom of the thickener is controlled to be 45% of the total mass of the material.
  • the thickened bottom material is sent to the centrifuge for centrifugation, and the filtrate flows to the low temperature mother liquor.
  • the storage tank, the filter cake is sent to the potassium chloride washing salt tank, the washing time is controlled for 20 minutes, the solid-liquid mass ratio is controlled to 1: 2. 5, the slurry is sent to the cyclone; the quality of the solid material of the underflow of the cyclone is controlled. 49% of the total mass, the underflow material is filtered into a precision potassium centrifuge, the filtrate is returned to the potassium chloride washing salt tank, and the filter cake is sent to the step (6) potassium chloride drying process; the thickener overflow mother liquor and the centrifuge are centrifuged.
  • the filtrate is transferred to the low temperature mother liquor storage tank, it is mixed with secondary steam from the secondary crystallizer to be heated to 45 ° C, and mixed with secondary steam from the primary crystallizer to be heated to 65 ° C, and then from the step (2).
  • the condensate from the evaporation tank is heated to After 90 ° C, enter the secondary hot-melt stirred tank of the hot melt process;
  • the bottom salt slurry from the cyclone (5) hot-dissolving process enters the centrifuge for centrifugation, and the filtrate returns to the first-stage hot-dissolving tank.
  • the filter cake enters the two-stage series of sodium chloride washing tank and washes the salt with fresh water to wash the salt.
  • the mass ratio of washing salt solid-liquid is controlled at 1: 2, the slurry is sent to the current cyclone; the top stream of the cyclone enters the settler, the bottom of the settler returns to the first-stage salt washing tank, and the settler overflows Discharge into the waste water tank; control the quality of the underflow solid material of the cyclone to 50% of the total mass of the material, centrifuge into the centrifuge, return the filtrate to the first-stage salt washing tank, and the sodium chloride filter cake enters the fluidized drying cooler, after drying 5 ⁇ %;
  • the content of the sodium chloride is 0. 4wt%, the content of NaCl is 98. 8wt%;
  • the wet potassium chloride from the crystallization step (5) is dried in a potassium chloride drying chiller to obtain chlorination.
  • the decomposed mother liquor from the step (1) is preheated to 143 ° C for evaporation concentration.
  • the discharge is discharged, and the evaporation mother liquid is discharged to the five-stage series of halogen.
  • the crystallizer is cooled and crystallized, the crystallization temperature is gradually reduced, the temperature of each stage is 20 ° C, the cooling crystallization end temperature is 43 ° C, and the final crystallizer slurry enters the step (3) carnallite separation process;
  • the flashing secondary steam of the step (2) crystallizer is introduced into the cold injection tank, mixed with 77% of the mass fraction of the overflow old brine from the step (3), heated to 62 ° C, and sent to the hot injection.
  • the tank is preheated to 89 ° C with steam to form a well heat injection agent;
  • Hot solution The potassium salt cake from the step (1) and the second hot solution of the second stage are hot-dissolved, and the first-stage hot-dissolving time is controlled for 27 minutes, and the hot-melting temperature is 94 ° C.
  • the dissolved slurry enters the thickener to thicken, and the quality of the underlying solid material is controlled to be 48% of the total mass of the material.
  • the overflow of the thickener is sent to the high temperature mother liquor tank, and the underflow slurry is heated to 109 ° C for two stages of preheating.
  • Crystallization The hot-melt slurry in the high-temperature mother liquor tank is pumped to a three-stage series potassium chloride crystallizer to control the temperature of the first, second and third-grade crystallization mother liquors to 72 ° C, 61 ° C and 35 ° C, respectively.
  • the slurry is discharged from the third stage crystallizer to the thickener to thicken, and the quality of the solid material in the bottom of the thickener is controlled to 52% of the total mass of the material.
  • the thickened material is sent to a centrifuge for centrifugation, and the filtrate flows to the low temperature mother liquor.
  • the filter cake is sent to the potassium chloride washing salt tank, the washing time is controlled for 22 minutes, the solid-liquid mass ratio is controlled to 1: 2, the slurry is sent to the cyclone; the quality of the solid material of the underflow of the cyclone is controlled to the total mass of the material.
  • the slurry is sent to the current cyclone; the top stream of the cyclone enters the settler, and the settler underflow returns
  • the first-stage salt washing tank, the overflow of the settler is discharged into the waste water tank; the quality of the solid material in the underflow of the cyclone is controlled to 52% of the total mass of the material, and the centrifuge is centrifuged, the filtrate is returned to the first-stage washing tank, and the sodium chloride is filtered.
  • the cake enters the fluidized drying cooler and is dried to obtain a sodium chloride product; the sodium chloride product has a water content of 0.4 wt%, a NaCl content of 99. 2 wt%; a wet potassium chloride from the crystallization step (5)
  • the potassium chloride product has a water content of 0.06 wt%, a KC1 content of 97 wt%;
  • the upper part overflows to the decomposition mother liquor storage tank; the quality of the solid material in the dense underflow is controlled to be 35% of the total mass of the material, and the separation is carried out by filtration, and the mother liquor is separated into the evaporation concentration process; the obtained potassium salt cake is obtained from the step (4)
  • the potassium chloride crystallization mother liquid is washed according to the ratio of the mother liquid: potassium salt cake cake mass ratio of 1:2.2, wherein the initial production is washed with fresh water; after washing, it is sent to the step (4) hot solution crystallization, and the washing liquid is discharged back.
  • the decomposed mother liquid from the step (1) is preheated to 145 ° C for evaporation concentration, when the evaporation chamber boiling point rises to 30 ° C, the discharge is discharged, and the evaporated mother liquid is discharged to the five-stage series of carnallite crystallizer for cooling. Crystallization, crystallization temperature is gradually reduced, the temperature difference between the various stages is 20 ° C, the cooling crystallization end temperature is 40 ° C, and the final crystallizer slurry enters the step (3) carnallite separation process;
  • the slurry from the final stage (2) crystallizer is sent to the thickener, and the thickener overflows the old brine from the pump to the magnesium sheet production workshop, the old brine pool and the cold injection tank;
  • the overflow old brine in the production process accounts for 11% of the total mass of the overflow old brine, 17% is sent back to the old brine pool, and 72% is sent to the cold injection tank.
  • the quality of the underlying solid material in the lower part of the thickener is controlled. 48% of the total mass of the material, separated by filtration, and the obtained filter cake, that is, the carnallite, is returned to the step (1), and the filtrate is recirculated into the overflow old brine;
  • the flashing secondary steam of the step (2) crystallizer is introduced into the cold injection tank, mixed with 74% of the overflow old halogen mass fraction from the step (3), heated to 63 ° C, and sent to the hot injection.
  • the tank is preheated to 90 ° C with steam to form a well heat injection agent;
  • the subsequent filtrate of the potassium chloride crystals is also added to the secondary hot-melt stirred tank for secondary heat-dissolving, controlling the secondary hot-dissolving time for 24 minutes, the hot-melting temperature of 92 ° C, and the second hot-melt slurry.
  • the top stream of the cyclone is returned to the first-stage hot-dissolving tank, and the quality of the solid material in the underflow of the cyclone is controlled to be 50% of the total mass of the material.
  • the underlying solid material is sent to the step (6) salt washing process;
  • the hot-melt slurry in the high-temperature mother liquor tank is pumped to the three-stage series potassium chloride crystallizer to control the temperature of the first, second and third-grade crystallization mother liquors to 72 ° C, 61 ° C, and 35 ° C, respectively.
  • the third stage crystallizer is pumped to the thickener to thicken, and the quality of the solid material in the bottom of the thickener is controlled.
  • the thickened material is sent to the centrifuge for centrifugation, the filtrate flows to the low temperature mother liquor storage tank, the filter cake is sent to the potassium chloride washing salt tank, the washing time is controlled for 22 minutes, and the solid-liquid mass ratio control is 1: 2, the slurry is sent to the cyclone; the quality of the solid material in the underflow of the cyclone is controlled to 50% of the total mass of the material, the underflow material is filtered into a precision potassium centrifuge, the filtrate is returned to the potassium chloride washing tank, and the filter cake is sent to Step (6) potassium chloride drying process;
  • the thickener overflow mother liquor and the centrifugally separated filtrate are transferred to the low temperature mother liquor storage tank, mixed with secondary steam from the secondary crystallizer to be heated to 46 ° C, and mixed with secondary steam from the primary crystallizer to be heated to 68 °C, and then heated to 89 ° C with condensed water from the evaporation tank of step (2), and then enter the secondary hot-melt stirred tank of the hot-dissolving process;
  • the bottom stream slurry of the cyclone from the step (5) hot-dissolving process is centrifuged, and the filtrate is returned to the first-stage hot-dissolving tank.
  • the filter cake enters the two-stage series of sodium chloride washing salt tank and washes the salt with fresh water.
  • the salt time is 45 minutes, the mass ratio of washing salt to solid is controlled at 1:1.8, the slurry is sent to the current cyclone; the top stream of the cyclone enters the settler, and the bottom of the settler returns to the first-stage salt washing tank, and the sedimentation
  • the overflow is discharged into the waste water tank; the swirl is controlled
  • the mass of the underlying solid material accounts for 55 % of the total mass of the material, enters the centrifuge for centrifugation, the filtrate returns to the first-stage washing tank, the sodium chloride filter cake enters the fluidized drying cooler, and is dried to obtain a sodium chloride product; 5 ⁇ %;
  • the content of the sodium content is 0. 3wt%, the content of NaCl is 99. 5wt%;
  • the wet potassium chloride from the crystallization step (5) is dried in a potassium chloride drying chiller to obtain a potassium chloride product;
  • the potassium chloride product has a water content of 0.02 wt%, a KC1 content of 99 wt%;
  • the temperature of the I-evaporation chamber is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature is 0. 12Mpa, the temperature At 60 ° C, using II effect countercurrent feed, I effect discharge, discharge control point is MgCl 2 mass fraction 48wt%; discharge into the cooling / slicer, made of magnesium.

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Abstract

利用光卤石矿井采卤水生产氯化钾、氯化钠及镁片的方法，其包括如下步骤：（1）光卤石分解；（2）蒸发浓缩；（3）光卤石分离；（4）井采注剂配制；（5）热溶、结晶，得氯化钾；（6）洗盐及干燥，得氯化钠；（7）镁片加工。本发明由于采用热注剂溶矿，高温下氯化钾溶解度远大于氯化钠和氯化镁，从而可以大大降低生产单位产出氯化钾时氯化钠和氯化镁的采出率，后续工艺排出废盐量减少，回填量也显著降低，节约了成本，综合利用了光卤石中的钾和镁资源，经济效益可观。

Description

说 明 书
利用光卤石矿井采卤水生产氯化钾、 氯化钠及镁片的方法 技术领域
本发明涉及一种利用光卤石矿井采卤水生产氯化钾、 氯化钠及镁片的方法， 具体地说， 是涉及一种利用光 ¾石矿井采 ¾水热分解法生产氯化钾、 氯化钠及 镁片的方法。
背景技术
我国是一个钾资源严重缺乏的国家， 耕地普遍缺钾， 钾肥供需矛盾十分突 出。 国产钾肥满足率仅占 30%左右， 每年进口钾肥达 4000kt (K20) 以上。 随着 农业的发展和结构调整， 中国钾肥消费量还将有较高的年增长率， 预计到 2020 年， 中国钾肥消费量将达 lOOOOkt (K20)， 市场空间广阔。
我国绝大多数的钾肥都产自盐湖， 目前我国生产氯化钾肥料主要采用可溶 性钾盐矿光卤石为原料。 国内光卤石矿制取氯化钾的主要生产方法有： 冷分解- 浮选法， 冷分解-热熔结晶法， 反浮选 -冷结晶法， 兌卤脱钠控速分解法等。 盐 湖的光卤石矿一般是地面露天开采或者从滩晒盐田开采出来， 采用以上方法制 取氯化钾比较合适， 而对于地下深层的光卤石矿， 露天开采的深度有限， 且严 重破坏植被， 采出的杂质和废盐堆积造成环境污染， 因此， 一般用地下开采的 方式进行开发。 地下开采包括常规固采和钻井水溶法开采， 本发明主要涉及钻 井水溶法采出的卤水的加工方法。 如果采用常温加淡水溶采， 由于氯化钾和氯 化钠低温下溶解度差别不大， 在后续制取氯化钾的阶段同样会出现大量废盐堆 积， 并且为了不造成地质危害废盐还需要回填， 增加大量成本。
发明内容
本发明目的在于提供一种利用光卤石矿井采卤水热分解法生产氯化钾、 氯 化钠及镁片的方法。
本发明目的是通过以下技术方案实现的： 其包括如下歩骤：
(1) 光卤石分解
将光卤石矿井采卤水预热到 65〜75°C后， 与来自歩骤 （3) 的光卤石按卤 水：光卤石的质量比为 1： 0.17〜0.27 的比例加入到光卤石搅拌槽， 其中初次 生产使用的光 ¾石为由井采 ¾水直接蒸发浓缩获得的光 ¾石， 搅拌 20〜40分钟 后送至浓密机， 浓密机物料上部溢流至分解母液储罐； 控制浓密机下部底流固 体物料质量占物料总质量的 35%〜55%，过滤分离，滤液即分解母液送往歩骤（2) 蒸发浓缩工序； 得到的钾石盐滤饼用淡水或来自歩骤 （5) 的氯化钾结晶母液按 照母液或淡水与钾石盐滤饼质量比为 1： 1.5〜3的比例进行洗涤后送往歩骤（5) 热溶结晶， 洗液回排至光卤石分解搅拌槽；
(2) 蒸发浓缩
将来自歩骤 （1) 的分解母液预热至 135〜145°C进行蒸发浓缩， 当蒸发室 料液沸点升值达到 24〜27°C时排料， 蒸发母液排至五级串联的光卤石结晶器进 行冷却结晶， 结晶温度逐级降低， 各级温度相差 18〜22°C， 冷却结晶终点温度 35〜45°C， 末级结晶器料浆进入歩骤 （3) 光卤石分离工序；
(3) 光卤石分离
将来自歩骤 （2) 末级结晶器的料浆送至浓密机， 浓密机溢流老卤由泵分 别送至镁片生产车间、 老卤池和冷注剂储罐； 其中送至镁片生产车间的溢流老 卤占溢流老卤总质量的 5〜8%， 送至老卤池回填的占 15〜18%， 送至冷注剂储罐 的占 75〜80%； 控制浓密机下部底流固体物料质量占物料总质量的 35%〜55%， 过滤分离， 所得滤饼即光 ¾石返回歩骤 （1)， 滤液汇入溢流老卤；
(4) 井采注剂配制 将歩骤 （2 ) 结晶器的闪发二次蒸汽导入冷注剂储罐， 与来自歩骤 （3 ) 的 溢流老卤质量分数的 75〜80%混合， 加热到 55〜60°C， 再送至热注剂储罐， 用 蒸汽预热至 85〜95°C， 形成井采热注剂；
( 5 ) 热溶、 结晶
热溶： 将来自歩骤 （1 ) 的钾石盐滤饼和本歩骤的二级热溶母液进行一级 热溶， 控制一级热溶时间 15〜30分钟， 热溶温度 90〜95°C， 一级热溶料浆进入 浓密机增稠， 控制底流固体物料质量占物料总质量的 35%〜55 %， 浓密机顶部溢 流送入高温母液槽， 底流料浆经二级预热加热到 105〜110°C送入二级搅拌槽， 后续氯化钾结晶离心分离歩骤的滤液， 亦返回加入到二级热溶搅拌槽进行二级 热溶， 控制二级热溶时间 15〜30分钟， 热溶温度 90〜95°C， 二级热溶料浆送至 旋流器， 旋流器顶流即二级热溶母液返回一级热溶槽， 控制旋流器底流固体物 料质量占物料总质量的 47〜53 %， 底流固体物料送往歩骤 （6) 洗盐工序； 结晶： 将高温母液槽里的热溶料浆用泵送至三级串联的氯化钾结晶器， 控 制一、 二、 三级结晶母液温度分别为 70〜75°C、 57〜63 °C、 30〜40°C， 料浆从 第三级结晶器用泵排出至浓密机增稠， 控制浓密机底流固体物料质量占物料总 质量的 35%〜55 %， 增稠后的底流物料送至离心机进行离心分离， 滤液自流至低 温母液储罐， 滤饼送入氯化钾洗盐槽， 控制洗涤时间 15〜30分钟， 固液质量比 控制为 1： 2〜3， 料浆送至旋流器； 控制旋流器底流固体物料质量占物料总质量 的 45〜55 %， 底流物料进入精钾离心机过滤， 滤液返回氯化钾洗盐槽，滤饼送往 歩骤 （6) 氯化钾干燥工序；
浓密机溢流母液及离心机离心分离的滤液至低温母液储罐后， 与来自二级 结晶器的二次蒸汽混合加热至 40〜50°C， 与来自一级结晶器的二次蒸汽混合加 热至 60〜70°C， 再用来自歩骤 （2 ) 蒸发罐的冷凝水加热至 85〜95°C后， 进入 热溶工序的二级热溶搅拌槽；
(6) 洗盐及干燥
来自歩骤 （5 ) 热溶工序的旋流器底流盐浆进入离心机进行离心分离， 滤液 返回一级热溶槽，滤饼进入两级串联氯化钠洗盐槽用淡水洗盐，洗盐时间 30〜50 分钟， 洗盐固液质量比控制在 1： 2〜3， 料浆送至本歩骤旋流器； 旋流器顶流进 入沉降器， 沉降器底流返回一级洗盐槽， 沉降器溢流排入废水地槽； 控制旋流 器底流固体物料质量占物料总质量的 45〜55 %， 进入离心机离心分离， 滤液返 回一级洗盐槽， 氯化钠滤饼进入流化干燥冷却机， 干燥后得到含水量 0. 5wt %、 NaCl含量 98. 5wtQ/^ 氯化钠产品；
来自歩骤 （5 ) 结晶工序的湿氯化钾进入氯化钾干燥冷却机， 干燥后得到的 氯化钾产品， 含水量 1 wt % , KC1 ^95 wt %;
( 7) 镁片加工
将来自歩骤 （3) 光卤石分离工序的老卤送入两效蒸发系统， 控制 I效蒸发 室压力为 0. 11〜0. 13Mpa， 温度为 102〜108 °C， II效蒸发室压力为 0. 11〜 0. 13Mpa， 温度为 57〜63°C， 采用 II效逆流进料， I效排料，排料控制点为 MgCl2 质量分数 45%〜48%， 排料进入冷却 /切片机， 制成镁片。
进一歩， 歩骤（1)中， 卤水：光卤石的优选质量比为 1： 0. 20〜0. 25。
进一歩， 歩骤（4)中， 所述送至热注剂储罐蒸汽预热的优选温度为 90〜93
°C。
本发明之光卤石热分解生产工业氯化钾、 镁片和氯化钠的方法， 依据 K+、 Na\ Mg2+〃C1—一 H20四元水盐体系相图理论， 采用热分解、 光卤石蒸发结晶、 热 熔、 分离、 多级串联真空冷析结晶， 分离干燥得到成品氯化钾。 老卤中镁和钠 可根据市场情况调节生产镁片和氯化钠等相应产品， 废弃物可用于废井填充。 本发明有如下显著优点：
( 1 ) 原卤分解光卤石可大大减少系统加水量， 减少系统蒸发量； （2 ) 采用 一效蒸发、 多级闪发真空冷却结晶光卤石， 蒸发二次汽用于预热分解母液、 闪 发二次蒸汽用于预热采矿注剂和原卤， 合理利用能源； （3 ) 钾石盐热溶工艺采 用两段热溶， 钾石盐溶解充分， 废盐中钾含量较低， 钾收率高； （4) 氯化钾真 空冷却结晶工艺充分利用二次蒸汽的余热加热母液， 减少热溶蒸汽消耗， 同时 还可减少冷却循环水的用量； （5 ) 老卤用于配制注剂和废井置换， 可根据市场 情况调节生产镁片和工业盐产品， 彻底解决了溶采法开采光卤石型钾盐矿床生 产氯化钾带来的排废问题。 概而言之， 本发明由于采用热注剂溶矿， 高温下氯化钾溶解度远大于氯化 钠和氯化镁， 从而可以大大降低生产单位产量氯化钾时氯化钠和氯化镁的采出 率， 后续工艺排出废盐量减少， 回填工程量也显著降低， 节约了大量的成本， 综合利用了光卤石中的钾和镁资源， 经济效益可观。
具体实施方式
以下结合实施例， 对本发明作进一歩详细说明。
实施例 1
( 1 ) 光卤石分解 将光卤石矿井采卤水预热到 70°C后， 与来自歩骤 （3) 的光卤石按卤水： 光卤石的质量比 1： 0. 2的比例加入到光卤石搅拌槽， 其中初次生产的光卤石为 由井采卤水直接蒸发浓缩获得的光卤石， 搅拌 25分钟后送至浓密机， 浓密机物 料上部溢流至分解母液储罐；控制浓密底流固体物料质量占物料总质量的 40%， 过滤分离， 分解母液即滤液送去蒸发浓缩工序； 得到的钾石盐滤饼用来自歩骤 (4) 的氯化钾结晶母液按照母液：钾石盐滤饼质量比为 1： 2的比例进行洗涤， 初次生产采用淡水洗涤； 洗涤后， 送往歩骤 （4) 热溶结晶， 洗液回排至光卤石 分解搅拌槽；
( 2 ) 蒸发浓缩
将来自歩骤（1 ) 的分解母液预热至 14CTC进行蒸发浓缩， 当蒸发室料液沸 点升值达到 25°C时排料，蒸发母液排至五级串联的光卤石结晶器进行冷却结晶， 结晶温度逐级降低， 各级温度相差 20°C， 冷却结晶终点温度 40°C， 末级结晶器 料浆进入歩骤 （3 ) 光卤石分离工序；
( 3 ) 光卤石分离
将来自歩骤 （2 ) 末级结晶器的料浆送至浓密机， 浓密机溢流老卤由泵分 别送至镁片生产车间、 老卤池和冷注剂储罐； 其中送至镁片生产车间的溢流老 卤占溢流老卤总质量的 7%，送至老卤池回填的占 17%，送至冷注剂储罐的占 76%; 控制浓密机下部底流固体物料质量占物料总质量的 45%， 过滤分离， 所得滤饼即 光卤石返回歩骤 （1 )， 滤液汇入溢流老卤；
(4) 井采注剂配制
将歩骤 （2 ) 结晶器的闪发二次蒸汽导入冷注剂储罐， 与来自歩骤 （3 ) 的 溢流老卤质量分数的 76%混合， 加热到 58°C， 再送至热注剂储罐， 用蒸汽预热 至 88°C， 形成井采热注剂；
( 5 ) 热溶、 结晶
热溶： 将来自歩骤 （1 ) 的钾石盐和本歩骤的二级热溶母液进行一级热溶， 控制一级热溶时间 20分钟， 热溶温度 92°C， 一级热溶料浆进入浓密机增稠， 控 制底流固体物料质量占物料总质量的 40 %， 浓密机顶部溢流送入高温母液槽， 底流料浆经二级预热加热到 107°C送入二级搅拌槽，后续氯化钾结晶离心分离歩 骤的滤液， 亦返回加入到二级热溶搅拌槽进行二级热溶， 控制二级热溶时间 20 分钟， 热溶温度 94°C， 二级热溶料浆送至旋流器， 旋流器顶流即二级热溶母液 返回一级热溶槽， 控制旋流器底流固体物料质量占物料总质量的 48 %， 底流固 体物料送往歩骤 （6) 洗盐工序；
结晶： 将高温母液槽里的热溶料浆用泵送至三级串联的氯化钾结晶器， 控 制一、 二、 三级结晶母液温度分别为 75 °C、 63°C、 40°C， 料浆从第三级结晶器 用泵排出至浓密机增稠， 控制浓密机底流固体物料质量占物料总质量的 45%， 增 稠后的底流物料送至离心机进行离心分离， 滤液自流至低温母液储罐， 滤饼送 入氯化钾洗盐槽， 控制洗涤时间 20分钟， 固液质量比控制为 1： 2. 5， 料浆送至 旋流器； 控制旋流器底流固体物料质量占物料总质量的 49 %， 底流物料进入精 钾离心机过滤， 滤液返回氯化钾洗盐槽，滤饼送往歩骤 （6 ) 氯化钾干燥工序； 浓密机溢流母液及离心机离心分离的滤液至低温母液储罐后， 与来自二级 结晶器的二次蒸汽混合加热至 45°C， 与来自一级结晶器的二次蒸汽混合加热至 65°C， 再用来自歩骤（2 )蒸发罐的冷凝水加热至 90°C后， 进入热溶工序的二级 热溶搅拌槽；
( 6) 洗盐及干燥
来自歩骤 （5 ) 热溶工序的旋流器底流盐浆进入离心机进行离心分离， 滤液 返回一级热溶槽，滤饼进入两级串联氯化钠洗盐槽用淡水洗盐， 洗盐时间 40 分 钟， 洗盐固液质量比控制在 1： 2， 料浆送至本歩骤旋流器； 旋流器顶流进入沉 降器， 沉降器底流返回一级洗盐槽， 沉降器溢流排入废水地槽； 控制旋流器底 流固体物料质量占物料总质量的 50 %， 进入离心机离心分离， 滤液返回一级洗 盐槽， 氯化钠滤饼进入流化干燥冷却机， 干燥后得到氯化钠产品； 所述氯化钠 产品含水量 0. 4wt % , NaCl含量 98. 8wt%;
来自歩骤 （5 ) 结晶工序的湿氯化钾进入氯化钾干燥冷却机干燥， 得到氯化 钾产品； 所述氯化钾产品， 含水量 0.4wt%， KC1含量 97wt %;
(7) 镁片加工 将来自歩骤 （3) 光卤石分离工序的老卤送入两效蒸发系统， 控制 I效蒸发 室压力为 0.12Mpa， 温度为 104°C， II效蒸发室压力为 0.13Mpa， 温度为 59°C， 采用 II效逆流进料， I效排料，排料控制点为 MgCl2质量分数 45wt%; 排料进入冷 却 /切片机， 制成镁片。
实施例 2
(1) 光卤石分解 将光卤石矿井采卤水预热到 72Ό后， 与来自歩骤 （3) 的光卤石按卤水： 光卤石的质量比 1 : 0.25 的比例加入到光卤石搅拌槽， 其中初次生产的光卤石 为由井采卤水直接蒸发浓缩获得的光卤石， 搅拌 36分钟后送至浓密机， 浓密机 物料上部溢流至分解母液储罐； 控制浓密底流固体物料质量占物料总质量的 38 %, 过滤分离， 分解母液即滤液送去蒸发浓缩工序； 得到的钾石盐滤饼用来自 歩骤 （4) 的氯化钾结晶母液按照母液：钾石盐滤饼质量比为 1： 2.5 的比例进 行洗涤， 其中初次生产采用淡水洗涤； 洗涤后， 送往歩骤 （4) 热溶结晶， 洗液 回排至光 ¾石分解搅拌槽；
(2) 蒸发浓缩 将来自歩骤（1) 的分解母液预热至 143°C进行蒸发浓缩， 当蒸发室料液沸 点升值达到 26°C时排料，蒸发母液排至五级串联的光卤石结晶器进行冷却结晶， 结晶温度逐级降低， 各级温度相差 20°C， 冷却结晶终点温度 43°C， 末级结晶器 料浆进入歩骤 （3) 光卤石分离工序；
(3) 光卤石分离 将来自歩骤 （2) 末级结晶器的料浆送至浓密机， 浓密机溢流老卤由泵分 别送至镁片生产车间、 老卤池和冷注剂储罐； 其中送至镁片生产车间的溢流老 卤占溢流老卤总质量的 8%，送至老卤池回填的占 15%，送至冷注剂储罐的占 77%; 控制浓密机下部底流固体物料质量占物料总质量的 50 %， 过滤分离， 所得滤饼 即光卤石返回歩骤 （1 )， 滤液汇入溢流老卤；
(4) 井采注剂配制
将歩骤 （2 ) 结晶器的闪发二次蒸汽导入冷注剂储罐， 与来自歩骤 （3 ) 的 溢流老卤质量分数的 77%混合， 加热到 62°C， 再送至热注剂储罐， 用蒸汽预热 至 89°C， 形成井采热注剂；
( 5 ) 热溶、 结晶
热溶： 将来自歩骤 （1 ) 的钾石盐滤饼和本歩骤二级热溶母液进行一级热 溶，控制一级热溶时间 27分钟，热溶温度 94°C，一级热溶料浆进入浓密机增稠， 控制底流固体物料质量占物料总质量的 48 %，浓密机顶部溢流送入高温母液槽， 底流料浆经二级预热加热到 109°C送入二级搅拌槽，后续氯化钾结晶离心分离歩 骤的滤液亦加入到二级热溶搅拌槽进行二级热溶， 控制二级热溶时间 25分钟， 热溶温度 92°C， 二级热溶料浆送至旋流器， 旋流器顶流返回一级热溶槽， 控制 旋流器底流固体物料质量占物料总质量的 51 %， 底流固体物料送往歩骤（6)洗 盐工序；
结晶： 将高温母液槽里的热溶料浆用泵送至三级串联的氯化钾结晶器， 控 制一、 二、 三级结晶母液温度分别为 72 °C、 61 °C、 35°C , 料浆从第三级结晶器 用泵排出至浓密机增稠， 控制浓密机底流固体物料质量占物料总质量的 52%， 增 稠后的物料送至离心机进行离心分离， 滤液自流至低温母液储罐， 滤饼送入氯 化钾洗盐槽，控制洗涤时间 22分钟，固液质量比控制为 1： 2，料浆送至旋流器; 控制旋流器底流固体物料质量占物料总质量的 50 %， 底流物料进入精钾离心机 过滤， 滤液返回氯化钾洗盐槽，滤饼送往歩骤 （6) 氯化钾干燥工序； 浓密机溢流母液及离心机离心分离的滤液至低温母液储罐后， 与来自二级 结晶器的二次蒸汽混合加热至 46°C， 与来自一级结晶器的二次蒸汽混合加热至 58°C， 再用来自歩骤（2)蒸发罐的冷凝水加热至 89°C后， 进入热溶工序的二级 热溶搅拌槽；
(6) 洗盐及干燥 将来自歩骤 （5) 热溶工序的旋流器底流盐浆进入离心机进行离心分离， 滤 液返回一级热溶槽，滤饼进入两级串联氯化钠洗盐槽用淡水洗盐， 洗盐时间 46 分钟， 洗盐固液质量比控制在 1： 1. 8， 料浆送至本歩骤旋流器； 旋流器顶流进 入沉降器， 沉降器底流返回一级洗盐槽， 沉降器溢流排入废水地槽； 控制旋流 器底流固体物料质量占物料总质量的 52 %， 进入离心机离心分离， 滤液返回一 级洗盐槽， 氯化钠滤饼进入流化干燥冷却机， 干燥后得到氯化钠产品； 所述氯 化钠产品含水量 0. 4wt % , NaCl含量 99. 2wt%; 来自歩骤 （5 ) 结晶工序的湿氯化钾进入氯化钾干燥冷却机干燥， 得到氯化 钾产品； 所述氯化钾产品， 含水量 0. 06wt %， KC1含量 97wt %;
( 7) 镁片加工 将来自歩骤 （3) 光卤石分离工序的老卤送入两效蒸发系统， 控制 I效蒸发 室压力为 0. 12Mpa， 温度为 105°C， II效蒸发室压力为 0. 12Mpa， 温度为 60°C， 采用 II效逆流进料， I效排料，排料控制点为 MgCl2质量分数 46wt%; 排料进入冷 却 /切片机， 制成镁片。
实施例 3
( 1 ) 光卤石分解 将光卤石矿井采卤水预热到 70°C后， 与来自歩骤 （3) 的光卤石按卤水： 光卤石的质量比 1 : 0.28 的比例加入到光卤石搅拌槽， 其中初次生产的光卤石 为由井采卤水直接蒸发浓缩获得光卤石， 搅拌 40分钟后送至浓密机， 浓密机物 料上部溢流至分解母液储罐；控制浓密底流固体物料质量占物料总质量的 35%， 过滤分离， 分解母液即滤液送去蒸发浓缩工序； 得到的钾石盐滤饼用来自歩骤 (4) 的氯化钾结晶母液按照母液：钾石盐滤饼质量比为 1： 2.2 的比例进行洗 涤， 其中初次生产采用淡水洗涤； 洗涤后， 送往歩骤 （4) 热溶结晶， 洗液回排 至光 ¾石分解搅拌槽；
(2) 蒸发浓缩
将来自歩骤（1) 的分解母液预热至 145°C进行蒸发浓缩， 当蒸发室料液沸 点升值达到 30°C时排料，蒸发母液排至五级串联的光卤石结晶器进行冷却结晶， 结晶温度逐级降低， 各级温度相差 20°C， 冷却结晶终点温度 40°C， 末级结晶器 料浆进入歩骤 （3) 光卤石分离工序；
(3) 光卤石分离
将来自歩骤 （2) 末级结晶器的料浆送至浓密机， 浓密机溢流老卤由泵分 别送至镁片生产车间、 老卤池和冷注剂储罐； 其中送至镁片生产工序的溢流老 卤占溢流老卤总质量的 11%，送至老卤池回填的占 17%，送至冷注剂储罐的占 72%; 控制浓密机下部底流固体物料质量占物料总质量的 48%， 过滤分离， 所得滤饼 即光卤石返回歩骤 （1)， 滤液汇入溢流老卤；
(4) 井采注剂配制
将歩骤 （2) 结晶器的闪发二次蒸汽导入冷注剂储罐， 与来自歩骤 （3) 的 溢流老卤质量分数的 74%混合， 加热到 63°C， 再送至热注剂储罐， 用蒸汽预热 至 90°C， 形成井采热注剂；
(5) 热溶、 结晶 热溶： 将来自歩骤 （1 ) 的钾石盐滤饼和本歩骤二级热溶母液进行一级热 溶，控制一级热溶时间 27分钟，热溶温度 95°C，一级热溶料浆进入浓密机增稠， 控制底流固体质量占总质量的 48 %， 浓密机顶部溢流送入高温母液槽， 底流料 浆经二级预热加热到 108°C送入二级搅拌槽，后续氯化钾结晶离心分离歩骤的滤 液亦加入到二级热溶搅拌槽进行二级热溶， 控制二级热溶时间 24分钟， 热溶温 度 92°C， 二级热溶料浆送至旋流器， 旋流器顶流返回一级热溶槽， 控制旋流器 底流固体物料质量占物料总质量的 50 %，底流固体物料送往歩骤（6)洗盐工序； 结晶： 将高温母液槽里的热溶料浆用泵送至三级串联的氯化钾结晶器， 控 制一、 二、 三级结晶母液温度分别为 72 °C、 61 °C、 35°C , 料浆从第三级结晶器 用泵排出至浓密机增稠， 控制浓密机底流固体物料质量占物料总质量的 52%， 增 稠后的物料送至离心机进行离心分离， 滤液自流至低温母液储罐， 滤饼送入氯 化钾洗盐槽，控制洗涤时间 22分钟，固液质量比控制为 1： 2，料浆送至旋流器; 控制旋流器底流固体物料质量占物料总质量的 50 %， 底流物料进入精钾离心机 过滤， 滤液返回氯化钾洗盐槽，滤饼送往歩骤 （6) 氯化钾干燥工序；
浓密机溢流母液及离心机离心分离的滤液至低温母液储罐后， 与来自二级 结晶器的二次蒸汽混合加热至 46°C， 与来自一级结晶器的二次蒸汽混合加热至 68°C， 再用来自歩骤（2 )蒸发罐的冷凝水加热至 89°C后， 进入热溶工序的二级 热溶搅拌槽；
( 6) 洗盐及干燥
将来自歩骤 （5 ) 热溶工序的旋流器底流盐浆进入离心机进行离心分离， 滤 液返回一级热溶槽，滤饼进入两级串联氯化钠洗盐槽用淡水洗盐， 洗盐时间 45 分钟， 洗盐固液质量比控制在 1： 1. 8， 料浆送至本歩骤旋流器； 旋流器顶流进 入沉降器， 沉降器底流返回一级洗盐槽， 沉降器溢流排入废水地槽； 控制旋流 器底流固体物料质量占物料总质量的 55 %， 进入离心机离心分离， 滤液返回一 级洗盐槽， 氯化钠滤饼进入流化干燥冷却机， 干燥后得到氯化钠产品； 所述氯 化钠产品含水量 0. 3wt % , NaCl含量 99. 5wt%;
来自歩骤 （5 ) 结晶工序的湿氯化钾进入氯化钾干燥冷却机干燥， 得到氯化 钾产品； 所述氯化钾产品， 含水量 0. 02wt %， KC1含量 99wt %;
( 7) 镁片加工
将来自歩骤 （3) 光卤石分离工序的老卤送入两效蒸发系统， 控制 I效蒸发 室压力为 0. 12Mpa， 温度为 105°C， II效蒸发室压力为 0. 12Mpa， 温度为 60°C， 采用 II效逆流进料， I效排料，排料控制点为 MgCl2质量分数 48wt%; 排料进入冷 却 /切片机， 制成镁片。

Claims

权 利 要 求 书
1、 一种利用光卤石矿井采卤水生产氯化钾、 氯化钠及镁片的方法， 其特 征在于， 包括如下歩骤：
(1) 光卤石分解
将光卤石矿井采卤水预热到 65〜75°C后， 与来自歩骤 （3) 的光卤石按卤 水：光卤石的质量比为 1： 0.17〜0.27 的比例加入到光卤石搅拌槽， 其中初次 生产使用的光 ¾石为由井采 ¾水直接蒸发浓缩获得的光 ¾石， 搅拌 20〜40分钟 后送至浓密机， 浓密机物料上部溢流至分解母液储罐； 控制浓密机下部底流固 体物料质量占物料总质量的 35%〜55%，过滤分离，滤液即分解母液送往歩骤（2) 蒸发浓缩工序； 得到的钾石盐滤饼用淡水或来自歩骤 （5) 的氯化钾结晶母液按 照母液或淡水与滤饼质量比为 1： 1.5〜3的比例进行洗涤后送往歩骤 （5) 热溶 结晶， 洗液回排至光卤石分解搅拌槽；
(2) 蒸发浓缩
将来自歩骤 （1) 的分解母液预热至 135〜145°C进行蒸发浓缩， 当蒸发室 料液沸点升值达到 24〜27°C时排料， 蒸发母液排至五级串联的光卤石结晶器进 行冷却结晶， 结晶温度逐级降低， 各级温度相差 18〜22°C， 冷却结晶终点温度 35〜45°C， 末级结晶器料浆进入歩骤 （3) 光卤石分离工序；
(3) 光卤石分离
将来自歩骤 （2) 末级结晶器的料浆送至浓密机， 浓密机溢流老卤由泵分 别送至镁片生产车间、 老卤池和冷注剂储罐； 其中送至镁片生产车间的溢流老 卤占溢流老卤总质量的 5〜8%， 送至老卤池回填的占 15〜18%， 送至冷注剂储罐 的占 75〜80%； 控制浓密机下部底流固体物料质量占物料总质量的 35%〜55%， 过滤分离， 所得滤饼即光 ¾石返回歩骤 （1)， 滤液汇入溢流老卤； (4) 井采注剂配制
将歩骤 （2 ) 结晶器的闪发二次蒸汽导入冷注剂储罐， 与来自歩骤 （3 ) 的 溢流老卤质量分数的 75〜80%混合， 加热到 55〜60°C， 再送至热注剂储罐， 用 蒸汽预热至 85〜95°C， 形成井采热注剂；
( 5 ) 热溶、 结晶
热溶： 将来自歩骤 （1 ) 的钾石盐滤饼和本歩骤的二级热溶母液进行一级 热溶， 控制一级热溶时间 15〜30分钟， 热溶温度 90〜95°C， 一级热溶料浆进入 浓密机增稠， 控制底流固体物料质量占物料总质量的 35%〜55 %， 浓密机顶部溢 流送入高温母液槽， 底流料浆经二级预热加热到 105〜110°C送入二级搅拌槽， 后续氯化钾结晶离心分离歩骤的滤液， 亦返回加入到二级热溶搅拌槽进行二级 热溶， 控制二级热溶时间 15〜30分钟， 热溶温度 90〜95°C， 二级热溶料浆送至 旋流器， 旋流器顶流即二级热溶母液返回一级热溶槽， 控制旋流器底流固体物 料质量占物料总质量的 47〜53 %， 底流固体物料送往歩骤 （6) 洗盐工序； 结晶： 将高温母液槽里的热溶料浆用泵送至三级串联的氯化钾结晶器， 控 制一、 二、 三级结晶母液温度分别为 70〜75°C、 57〜63 °C、 30〜40°C， 料浆从 第三级结晶器用泵排出至浓密机增稠， 控制浓密机底流固体物料质量占物料总 质量的 35%〜55 %， 增稠后的底流物料送至离心机进行离心分离， 滤液自流至低 温母液储罐， 滤饼送入氯化钾洗盐槽， 控制洗涤时间 15〜30分钟， 固液质量比 控制为 1： 2〜3， 料浆送至旋流器； 控制旋流器底流固体物料质量占物料总质量 的 45〜55 %， 底流物料进入精钾离心机过滤， 滤液返回氯化钾洗盐槽，滤饼送往 歩骤 （6) 氯化钾干燥工序；
浓密机溢流母液及离心机离心分离的滤液至低温母液储罐后， 与来自二级 结晶器的二次蒸汽混合加热至 40〜50°C， 与来自一级结晶器的二次蒸汽混合加 热至 60〜70°C， 再用来自歩骤 （2 ) 蒸发罐的冷凝水加热至 85〜95°C后， 进入 热溶工序的二级热溶搅拌槽；
(6) 洗盐及干燥
来自歩骤 （5 ) 热溶工序的旋流器底流盐浆进入离心机进行离心分离， 滤液 返回一级热溶槽，滤饼进入两级串联氯化钠洗盐槽用淡水洗盐，洗盐时间 30〜50 分钟， 洗盐固液质量比控制在 1： 2〜3， 料浆送至本歩骤旋流器； 旋流器顶流进 入沉降器， 沉降器底流返回一级洗盐槽， 沉降器溢流排入废水地槽； 控制旋流 器底流固体物料质量占物料总质量的 45〜55 %， 进入离心机离心分离， 滤液返 回一级洗盐槽， 氯化钠滤饼进入流化干燥冷却机， 干燥后得到含水量 0. 5wt %、 NaCl含量 98. 5wtQ/^ 氯化钠产品；
来自歩骤 （5 ) 结晶工序的湿氯化钾进入氯化钾干燥冷却机， 干燥后得到的 氯化钾产品， 含水量 1 wt % , KC1 ^95 wt %;
( 7) 镁片加工
将来自歩骤 （3) 光卤石分离工序的老卤送入两效蒸发系统， 控制 I效蒸发 室压力为 0. 11〜0. 13Mpa， 温度为 102〜108 °C， II效蒸发室压力为 0. 11〜 0. 13Mpa， 温度为 57〜63°C， 采用 II效逆流进料， I效排料，排料控制点为 MgCl2 质量分数 45%〜48%， 排料进入冷却 /切片机， 制成镁片。
2、 根据权利要求 1所述利用光卤石矿井采卤水生产氯化钾、 镁片及氯化钠 的方法，其特征在于，歩骤（1)中，所述卤水： 光卤石的质量比为 1： 0. 2〜0. 25。
3、 根据权利要求 1或 2所述利用光卤石矿井采卤水生产氯化钾、 氯化钠及 镁片的方法， 歩骤 (4)中， 所述送至热注剂储罐蒸汽预热至 90〜93°C。
PCT/CN2012/081014 2011-12-22 2012-09-05 利用光卤石矿井采卤水生产氯化钾、氯化钠及镁片的方法 WO2013091403A1 (zh)

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