CN107308662A - The MVR evaporating, concentrating and crystallizing techniques of lithium are extracted from salt lake bittern - Google Patents
The MVR evaporating, concentrating and crystallizing techniques of lithium are extracted from salt lake bittern Download PDFInfo
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- 238000001704 evaporation Methods 0.000 title claims abstract description 233
- 238000000034 method Methods 0.000 title claims abstract description 94
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 72
- 241001131796 Botaurus stellaris Species 0.000 title abstract 3
- 230000008020 evaporation Effects 0.000 claims abstract description 210
- 238000002425 crystallisation Methods 0.000 claims abstract description 109
- 230000008025 crystallization Effects 0.000 claims abstract description 107
- 230000008569 process Effects 0.000 claims abstract description 86
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 51
- 230000006835 compression Effects 0.000 claims abstract description 30
- 238000007906 compression Methods 0.000 claims abstract description 30
- 239000013078 crystal Substances 0.000 claims abstract description 27
- 239000011780 sodium chloride Substances 0.000 claims abstract description 25
- 238000005516 engineering process Methods 0.000 claims abstract description 11
- 239000000243 solution Substances 0.000 claims description 123
- 239000012452 mother liquor Substances 0.000 claims description 65
- 238000010438 heat treatment Methods 0.000 claims description 57
- 239000000463 material Substances 0.000 claims description 39
- 239000012267 brine Substances 0.000 claims description 38
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 38
- 239000010408 film Substances 0.000 claims description 33
- 230000009194 climbing Effects 0.000 claims description 32
- 239000011552 falling film Substances 0.000 claims description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 239000007789 gas Substances 0.000 claims description 24
- 239000002562 thickening agent Substances 0.000 claims description 18
- 239000011550 stock solution Substances 0.000 claims description 17
- 150000003839 salts Chemical class 0.000 claims description 15
- 238000002360 preparation method Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- 238000000605 extraction Methods 0.000 claims description 12
- 239000000047 product Substances 0.000 claims description 12
- 230000000694 effects Effects 0.000 claims description 10
- 239000006228 supernatant Substances 0.000 claims description 9
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 claims description 8
- 229910001416 lithium ion Inorganic materials 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 7
- 230000009977 dual effect Effects 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 claims description 4
- 229910052808 lithium carbonate Inorganic materials 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 3
- 239000010413 mother solution Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 238000005660 chlorination reaction Methods 0.000 abstract 1
- 159000000000 sodium salts Chemical class 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 12
- 229910003002 lithium salt Inorganic materials 0.000 description 5
- 159000000002 lithium salts Chemical class 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 230000008719 thickening Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005008 domestic process Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 229910052629 lepidolite Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005185 salting out Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0094—Evaporating with forced circulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/04—Evaporators with horizontal tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/2803—Special features relating to the vapour to be compressed
-
- 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
- C22B26/12—Obtaining lithium
-
- 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
- C22B9/00—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals
- C22B9/02—Refining by liquating, filtering, centrifuging, distilling, or supersonic wave action including acoustic waves
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Life Sciences & Earth Sciences (AREA)
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Abstract
The present invention relates to a kind of MVR evaporating, concentrating and crystallizing techniques that lithium is extracted from salt lake bittern, including stoste preheating, MVR evaporating, concentrating and crystallizings and the part of MVR both vapor compressions three.Technology utilization MVR steam recompression technologies are concentrated by evaporation salt lake bittern, there is a small amount of sodium chloride crystallization to separate out in evaporating concentration process, which reduce energy consumption and operating cost, improve technology advanced, avoid Multi-effect Evaporation Processes equipment from only undertaking lithium solution concentrating function, and high-purity chlorination crystals of sodium salt problem can not be separated out.
Description
Technical Field
The invention relates to an MVR evaporation concentration crystallization process for extracting lithium from salt lake brine, in particular to a process for concentrating salt lake brine by using an MVR evaporation concentration crystallization method to extract lithium.
Background
In recent years, the application of the demand of basic lithium salt in the fields of new energy automobiles, electric tools, electric bicycles, communication base station backup power sources, power grid energy storage and the like keeps a rapid growth momentum, and especially the explosive growth occurs in the field of new energy automobiles. Through investment and construction in recent years, domestic lithium ore resources, brine resources and lithium extraction technology of lepidolite are developed gradually to form scale, lithium salt production enterprises fully utilize two resources at home and abroad, and the lithium salt capacity is gradually released to meet domestic requirements for lithium salts.
With the rising of lithium salt price and the expansion of productivity, many enterprises plan to create a new set of brine concentration and lithium extraction equipment. At present, the domestic method for extracting lithium carbonate from brine mainly comprises a precipitation method, an extraction method, an ion exchange adsorption method and a carbonization method, and the method applied in industry is mainly an evaporation-crystallization-precipitation method. The evaporation method generally comprises single-effect evaporation, multiple-effect evaporation and MVR evaporation, wherein the single-effect evaporation and the multiple-effect evaporation need to consume a large amount of steam, the investment cost is high, the operation cost is high, and the application of the evaporation method is limited to a certain extent; the Mechanical Vapor Recompression (MVR) technology introduces a Vapor compressor or a compression fan, recycles a large amount of latent heat of secondary Vapor, basically does not need to supplement Vapor, only consumes a small amount of electric energy, is one of energy-saving and environment-friendly technologies which are mainly popularized in China, is listed as a national key energy-saving technology popularization catalogue (the third batch) (published by the national development and improvement commission No. 33 2010), and is widely applied to the water evaporation concentration or crystallization industry.
Disclosure of Invention
The invention aims to solve the technical problems that in the existing process for extracting lithium from salt lake brine, the evaporation concentration section has high energy consumption and high operation cost, the secondary pollution is high and is unfavorable for the environment, and the like, and provides a plurality of processes for evaporating and concentrating salt lake brine by using the MVR steam recompression technology (a small amount of sodium chloride is crystallized and separated out in the evaporation concentration process), so that the energy consumption and the operation cost are reduced, the process technology advancement is improved, and the problem that high-purity sodium chloride salt crystals cannot be separated out because equipment only bears the lithium solution concentration function in the multi-effect evaporation process is solved.
In order to achieve the purpose, according to the first aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine comprises three parts, namely stock solution preheating, MVR evaporation concentration crystallization and MVR steam compression; the MVR evaporation concentration crystallization process adopts a first-stage forced circulation MVR evaporation concentration process,
the system is characterized in that the stock solution preheating part comprises a noncondensable gas preheating part and a condensed water preheating part, and the stock solution is preheated by fully utilizing the waste heat of the system;
in the MVR evaporation concentration crystallization part, the preheated stock solution enters an MVR primary forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the stock solution, and the solution starts to be evaporated and concentrated; after the solution is concentrated to a certain concentration, discharging the crystal mush into a thickener through an online control system, preliminarily separating mother liquor and the crystal mush in the thickener, allowing supernatant to flow into a mother liquor tank for storage, allowing the thickened crystal mush to enter a centrifuge for preliminary separation, allowing salt obtained by separation to serve as a NaCl product, returning the centrifuged mother liquor to the mother liquor tank, and conveying the mother liquor to a lithium making workshop through a mother liquor pump;
wherein, the evaporation temperature of the MVR primary forced circulation evaporation concentration part is 90 ℃, the effective temperature difference is 6 ℃, the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa;
in the MVR steam compression part, all secondary steam generated by the MVR forced circulation evaporative crystallization system enters a steam compressor, the compressor applies work to the secondary steam and compresses the secondary steam, the temperature and the pressure of the secondary steam are increased, then the secondary steam is conveyed to a shell pass of a forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
According to the second aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine adopts a two-stage forced circulation MVR evaporation concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR primary forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR secondary forced circulation evaporation crystallizer, heating the solution by using secondary steam compressed by a steam compressor, and continuously evaporating and concentrating the solution;
wherein, the evaporation temperature of the MVR primary forced circulation evaporation concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR secondary forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa;
in the MVR steam compression part, secondary steam generated by an MVR first-stage forced circulation evaporative crystallization system and a secondary forced circulation evaporative crystallization system completely enters a steam compressor, after the compressor applies work to the secondary steam for compression, the temperature and the pressure of the steam are improved, then the steam is conveyed to a first-stage forced circulation heater and a second-stage forced circulation heater, the shell pass of the first-stage forced circulation heater and the shell pass of the second-stage forced circulation heater are used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to.
According to the third aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine adopts a two-effect forced circulation MVR evaporation concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR one-effect forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR two-effect forced circulation evaporation crystallizer, supplying secondary steam generated by the first effect to a shell pass of a two-effect forced circulation heater, heating the solution, and continuously evaporating and concentrating the solution;
wherein, the evaporation temperature of the MVR one-effect forced circulation evaporation concentration part is 90 ℃, the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR dual-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%.
In the MVR steam compression part, the secondary steam generated by the MVR two-effect forced circulation evaporative crystallization system completely enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to a shell pass of a one-effect forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
According to the fourth aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine adopts a first-level falling film + second-level forced circulation MVR evaporation concentration process; it is characterized in that the preparation method is characterized in that,
the MVR evaporation concentration crystallization part comprises a falling film evaporation concentration part and a forced circulation evaporation crystallization part; the preheated solution enters an MVR falling film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; evaporating to a certain concentration, transferring the material to an MVR forced circulation evaporation crystallizer, heating the solution by utilizing secondary steam compressed by a steam compressor, continuously evaporating and concentrating the solution, separating out a small amount of sodium chloride crystals in the process, discharging crystal mush into a thickener through an online control system after the solution is concentrated to a certain concentration, preliminarily separating mother liquor and the crystal mush in the thickener, allowing supernatant to flow into a mother liquor tank for storage, allowing the thickened crystal mush to enter a centrifuge for separation, allowing the separated salt to be used as a NaCl product, returning the centrifuged mother liquor to the mother liquor tank, and conveying the mother liquor to a lithium making process workshop through a mother liquor pump;
wherein, the evaporation temperature of the MVR falling film evaporation concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa;
in the MVR steam compression part, all secondary steam generated by the MVR falling film evaporation concentration system and the MVR forced circulation evaporation crystallization system enters a steam compressor, the compressor applies work to compress the secondary steam, the temperature and the pressure of the steam are improved, then the steam is conveyed to a shell pass of a falling film evaporator and a forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
According to the fifth aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine adopts a first-level climbing film and a second-level forced circulation MVR evaporation concentration process; it is characterized in that the preparation method is characterized in that,
the MVR evaporation concentration crystallization part comprises a climbing film evaporation concentration part and a forced circulation evaporation crystallization part; the preheated solution enters an MVR climbing film evaporation device, secondary steam compressed by a steam compressor is used for heating the MVR climbing film evaporation device, and the solution starts to be evaporated and concentrated; evaporating to a certain concentration, transferring the material to an MVR forced circulation evaporation crystallizer, heating the solution by utilizing secondary steam compressed by a steam compressor, continuously evaporating and concentrating the solution, separating out a small amount of sodium chloride crystals in the process, discharging crystal mush into a thickener through an online control system after the solution is concentrated to a certain concentration, preliminarily separating mother liquor and the crystal mush in the thickener, allowing supernatant to flow into a mother liquor tank for storage, allowing the thickened crystal mush to enter a centrifuge for separation, allowing the separated salt to be used as a NaCl product, returning the centrifuged mother liquor to the mother liquor tank, and conveying the mother liquor to a lithium making process workshop through a mother liquor pump;
wherein, the evaporation temperature of the MVR climbing film evaporation concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa;
in the MVR steam compression part, all secondary steam generated by the MVR climbing film evaporation concentration system and the MVR forced circulation evaporation crystallization system enters a steam compressor, the compressor applies work to compress the secondary steam, the temperature and the pressure of the steam are improved, then the steam is conveyed to a climbing film evaporator and a shell pass of a forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
According to the sixth aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine adopts a one-effect climbing film and a two-effect forced circulation MVR evaporation concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR one-effect climbing film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR two-effect forced circulation evaporation crystallizer, supplying secondary steam generated by the first effect to a shell pass of a two-effect forced circulation heater, heating the solution, and continuously evaporating and concentrating the solution;
wherein, the evaporation temperature of the MVR one-effect climbing film evaporation concentration part is 90 ℃, the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR double-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%;
in the MVR steam compression part, all secondary steam generated by the MVR two-effect forced circulation evaporation crystallization system enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to the shell pass of the one-effect climbing film evaporator to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
According to the seventh aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine adopts a one-effect falling film + two-effect forced circulation MVR evaporation concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR one-effect falling film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR two-effect forced circulation evaporation crystallizer, supplying secondary steam generated by the first effect to a shell pass of a two-effect forced circulation heater, heating the solution, and continuously evaporating and concentrating the solution;
wherein, the evaporation temperature of the MVR single-effect falling film evaporation concentration part is 90 ℃, the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR double-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%;
in the MVR steam compression part, all secondary steam generated by the MVR two-effect forced circulation evaporation crystallization system enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to the shell pass of the one-effect falling film evaporator to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
According to the eighth aspect of the invention, the MVR evaporation concentration crystallization process for extracting lithium from salt lake brine adopts an MVR evaporation concentration crystallization extraction lithium + MVR reflux lithium mother liquor evaporation concentration extraction process; it is characterized in that the preparation method is characterized in that,
the preheating part preheats the stock solution by adopting the self heat of a recovery system to a set evaporation temperature value;
the MVR evaporation concentration crystallization part adopts an MVR high-efficiency energy-saving evaporation concentration technology to crystallize and separate the sodium chloride in the mixed salt to obtain salt, and the high-purity lithium-containing salt lake brine after the sodium chloride is extracted is subjected to a back-end process;
in the lithium-containing concentrated solution treatment part, treating the lithium-containing concentrated solution meeting the requirements to obtain a finished product of lithium carbonate and lithium-containing mother solution with low lithium ion concentration;
in the MVR reflux lithium mother liquor concentration part, the lithium ion mother liquor with high purity and low content enters an MVR evaporation concentration system for concentration, and when the concentration is increased to a proper concentration, the lithium ion mother liquor returns to the former stage process for reuse.
Compared with the prior art, the invention has the following beneficial effects: the system is stable, and the production continuity is good; the controllability of the discharge concentration of the concentrated solution is good; energy conservation and environmental protection; low operation cost and small occupied area, and realizes the standard-reaching concentration of the lithium solution and the salting-out effect of the sodium chloride high-purity crystal.
Drawings
The MVR evaporation concentration crystallization process for extracting lithium from salt lake brine is mainly used for extracting lithium from salt lake brine. The following figures show several routes of MVR evaporation concentration crystallization lithium extraction process. Wherein,
FIG. 1 is a flow diagram of a one-stage forced circulation MVR evaporative concentration process according to the present invention;
FIG. 2 is a flow diagram of a two-stage forced circulation MVR evaporative concentration process according to the present invention;
FIG. 3 is a flow diagram of a two-effect forced circulation MVR evaporative concentration process according to the present invention;
figure 4 is a flow diagram of a primary falling film + secondary forced circulation MVR evaporative concentration process according to the present invention;
FIG. 5 is a flow diagram of a one-stage climbing film + two-stage forced circulation MVR evaporative concentration process according to the present invention;
FIG. 6 is a flow diagram of a one-effect lift membrane + two-effect forced circulation MVR evaporative concentration process according to the present invention;
FIG. 7 is a flow diagram of a one-effect falling film + two-effect forced circulation MVR evaporation concentration process according to the present invention;
FIG. 8 is a flow chart of the MVR evaporative concentration crystallization extraction lithium + MVR refluxing lithium mother liquor evaporative concentration extraction process according to the present invention.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention.
The MVR evaporation concentration crystallization process for extracting lithium from salt lake brine provided by the invention provides several salt lake brine concentration crystallization methods, which can crystallize part of sodium chloride, reduce energy consumption and reduce operation cost.
In order to achieve the purpose, the MVR evaporation and concentration process of the salt lake brine comprises three parts, namely raw solution preheating, MVR evaporation, concentration and crystallization and MVR steam compression, and the specific implementation mode is as follows:
FIG. 1 is a flow chart of a one-stage forced circulation MVR evaporation concentration process according to the present invention, wherein a stock solution preheating part comprises a noncondensable gas preheating part and a condensed water preheating part, such that waste heat of the system is fully utilized, additional heat energy is not required, and heat energy consumption is reduced.
MVR evaporative concentration crystallization fraction: the preheated stock solution enters a first-stage forced circulation evaporation crystallization part, the concentration-boiling point rising relation is fully utilized, the investment is saved, the energy consumption is reduced, and the stable operation of the system is ensured.
The preheated solution enters an MVR first-stage forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is concentrated to a certain concentration, the magma is discharged into the thickener through the online control system, the mother liquor and the magma are preliminarily separated in the thickener, the supernatant flows into the mother liquor tank for storage, the thickened magma enters the centrifuge for separation, the separated salt is used as a NaCl product, the centrifuged mother liquor returns to the mother liquor tank and is conveyed to a lithium making workshop through the mother liquor pump.
Wherein, the evaporation temperature of the MVR primary forced circulation evaporation concentration part is 90 ℃, the effective temperature difference is 6 ℃, the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa.
MVR vapor compression section: all secondary steam generated by the MVR forced circulation evaporative crystallization system enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to a shell pass of a forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to a material feeding preheating part to be used as a heat source for feeding preheating.
FIG. 2 is a flow diagram of a two-stage forced circulation MVR evaporative concentration process according to the present invention, with the stock solution preheat section as described in FIG. 1.
MVR evaporative concentration crystallization fraction: the preheated solution enters an MVR first-stage forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, the material is transferred to an MVR two-stage forced circulation evaporation crystallizer, secondary steam compressed by a steam compressor is used for heating the solution, the solution is continuously evaporated and concentrated, and the rest processes are the same as the description of the figure 1.
Wherein, the evaporation temperature of the MVR primary forced circulation evaporation concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR secondary forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa.
MVR vapor compression section: the secondary steam generated by the MVR first-stage and second-stage forced circulation evaporative crystallization systems completely enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to a first-stage forced circulation heater and a second-stage forced circulation heater, the shell pass of the first-stage forced circulation heater and the second-stage forced circulation heater is used for heating the steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to a material feeding preheating part to be used as a heat source for feeding preheating.
FIG. 3 is a flow diagram of a two-way forced circulation MVR evaporative concentration process according to the present invention, with the dope preheating section as described in FIG. 1.
MVR evaporative concentration crystallization fraction: the preheated solution enters an MVR one-effect forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, the material is transferred to an MVR two-effect forced circulation evaporation crystallizer, secondary steam generated by one effect is used for a shell pass of a two-effect forced circulation heater, the solution is heated, the solution is continuously evaporated and concentrated, and the rest processes are the same as the description of the figure 1.
Wherein the evaporation temperature of the MVR one-effect forced circulation evaporation concentration part is 90 ℃, the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR dual-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%.
MVR vapor compression section: the secondary steam generated by the MVR two-effect forced circulation evaporative crystallization system completely enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to the shell pass of the one-effect forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
Fig. 4 is a flow diagram of a primary falling film + secondary forced circulation MVR evaporative concentration process according to the present invention, with the dope preheating section as described in fig. 1.
MVR evaporative concentration crystallization fraction: the system comprises a falling film evaporation concentration part and a forced circulation evaporation crystallization part, and fully utilizes the relation of concentration-boiling point rise to save investment and reduce energy consumption and ensure the stable operation of the system. The preheated solution enters an MVR falling film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; evaporate and change material to MVR forced circulation evaporation crystallizer behind the certain concentration, the secondary steam after utilizing vapor compressor compression heats the solution, solution continues evaporative concentration, this process has a small amount of sodium chloride crystal to separate out, after solution concentration to certain concentration, discharge the magma into the thickener through on-line control system, mother liquor and magma are primary separation in the thickener, the supernatant flows into the mother liquor jar and stores, the magma of thickening gets into centrifuge and separates, salt after the separation is as the NaCl product, mother liquor after the centrifugation returns the mother liquor jar, deliver to lithium manufacturing process workshop through the mother liquor pump.
Wherein the evaporation temperature of the MVR falling film evaporation concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa.
MVR vapor compression section: and after the compressor applies work to the secondary steam and compresses the secondary steam, the temperature and the pressure of the secondary steam are increased, the secondary steam is conveyed to the shell pass of the falling film evaporator and the forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
FIG. 5 is a flow diagram of a one-stage climbing film + two-stage forced circulation MVR evaporation concentration process according to the present invention, with the stock solution preheating part as described in FIG. 1.
MVR evaporative concentration crystallization fraction: the system comprises a climbing film evaporation concentration part and a forced circulation evaporation crystallization part, and fully utilizes the concentration-boiling point rising relation to save investment and reduce energy consumption and ensure the stable operation of the system. The preheated solution enters an MVR climbing film evaporation device, secondary steam compressed by a steam compressor is used for heating the MVR climbing film evaporation device, and the solution starts to be evaporated and concentrated; evaporate and change material to MVR forced circulation evaporation crystallizer behind the certain concentration, the secondary steam after utilizing vapor compressor compression heats the solution, solution continues evaporative concentration, this process has a small amount of sodium chloride crystal to separate out, after solution concentration to certain concentration, discharge the magma into the thickener through on-line control system, mother liquor and magma are primary separation in the thickener, the supernatant flows into the mother liquor jar and stores, the magma of thickening gets into centrifuge and separates, salt after the separation is as the NaCl product, mother liquor after the centrifugation returns the mother liquor jar, deliver to lithium manufacturing process workshop through the mother liquor pump.
Wherein, the evaporation temperature of the MVR climbing film evaporation concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa.
MVR vapor compression section: and after the compressor applies work to the secondary steam and compresses the secondary steam, the temperature and the pressure of the secondary steam are increased, the secondary steam is conveyed to the shell passes of the climbing film evaporator and the forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
FIG. 6 is a flow chart of a one-effect climbing film + two-effect forced circulation MVR evaporation concentration process according to the present invention, wherein the pre-heating part of the stock solution is the same as that described in FIG. 1.
MVR evaporative concentration crystallization fraction: the preheated solution enters an MVR one-effect climbing film evaporation device, secondary steam compressed by a steam compressor is used for heating the preheated solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, the material is transferred to an MVR two-effect forced circulation evaporation crystallizer, secondary steam generated by one effect is used for a shell pass of a two-effect forced circulation heater, the solution is heated, the solution is continuously evaporated and concentrated, and the rest processes are the same as the description of the figure 1.
Wherein the evaporation temperature of the MVR one-effect climbing film evaporation concentration part is 90 ℃, the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR dual-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%.
MVR vapor compression section: and after the compressor applies work to the secondary steam and compresses the secondary steam, the temperature and the pressure of the secondary steam are both improved, the secondary steam is conveyed to the shell pass of the one-effect climbing-film evaporator to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
Fig. 7 is a flow diagram of a one-effect falling film + two-effect forced circulation MVR evaporation concentration process according to the present invention, with the pre-heating portion of the dope as described in fig. 1.
MVR evaporative concentration crystallization fraction: the preheated solution enters an MVR (mechanical vapor recompression) one-effect falling film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, the material is transferred to an MVR two-effect forced circulation evaporation crystallizer, secondary steam generated by one effect is used for a shell pass of a two-effect forced circulation heater, the solution is heated, the solution is continuously evaporated and concentrated, and the rest processes are the same as the description of the figure 1.
Wherein, the evaporation temperature of the MVR single-effect falling film evaporation concentration part is 90 ℃, the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR dual-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%.
MVR vapor compression section: and after the compressor applies work to the secondary steam and compresses the secondary steam, the temperature and the pressure of the secondary steam are both improved, the secondary steam is conveyed to the shell pass of the one-effect falling-film evaporator to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
FIG. 8 is a flow chart of the MVR evaporative concentration crystallization extraction lithium + MVR refluxing lithium mother liquor evaporative concentration extraction process according to the present invention.
Preheating part: the raw liquid is preheated by the self heat of the recovery system to a set evaporation temperature value.
MVR evaporative concentration crystallization fraction: the method adopts an MVR high-efficiency energy-saving evaporation concentration technology to crystallize and separate sodium chloride in the mixed salt to obtain salt, and the high-purity lithium-containing salt lake brine from which the sodium chloride is extracted is subjected to a back-end process.
Lithium-containing concentrated solution treatment part: and processing the lithium-containing concentrated solution meeting the requirements to obtain a finished product of lithium carbonate and lithium-containing mother liquor with low lithium ion concentration.
MVR refluxing lithium mother liquor concentration part: and the high-purity low-content lithium ion mother liquor enters an MVR evaporation concentration system for concentration, and returns to the previous stage process for reuse when the concentration is increased to a proper concentration.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (15)
1. An MVR evaporation concentration crystallization process for extracting lithium from salt lake brine comprises three parts, namely stock solution preheating, MVR evaporation concentration crystallization and MVR steam compression; the MVR evaporation concentration crystallization process adopts a first-stage forced circulation MVR evaporation concentration process,
the system is characterized in that the stock solution preheating part comprises a noncondensable gas preheating part and a condensed water preheating part, and the stock solution is preheated by fully utilizing the waste heat of the system;
in the MVR evaporation concentration crystallization part, the preheated stock solution enters an MVR primary forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the stock solution, and the solution starts to be evaporated and concentrated; after the solution is concentrated to a certain concentration, discharging the crystal mush into a thickener through an online control system, preliminarily separating mother liquor and the crystal mush in the thickener, allowing supernatant to flow into a mother liquor tank for storage, allowing the thickened crystal mush to enter a centrifuge for preliminary separation, allowing salt obtained by separation to serve as a NaCl product, returning the centrifuged mother liquor to the mother liquor tank, and conveying the mother liquor to a lithium making workshop through a mother liquor pump;
in the MVR steam compression part, all secondary steam generated by the MVR forced circulation evaporative crystallization system enters a steam compressor, the compressor applies work to the secondary steam and compresses the secondary steam, the temperature and the pressure of the secondary steam are increased, then the secondary steam is conveyed to a shell pass of a forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
2. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, wherein the evaporation temperature of the MVR primary forced circulation evaporative concentration part is 90 ℃, the effective temperature difference is 6 ℃, the discharging concentration is 42.2%, and the vacuum degree is-0.3 MPa.
3. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, which adopts a two-stage forced circulation MVR evaporative concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR primary forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR secondary forced circulation evaporation crystallizer, heating the solution by using secondary steam compressed by a steam compressor, and continuously evaporating and concentrating the solution;
in the MVR steam compression part, secondary steam generated by an MVR first-stage forced circulation evaporative crystallization system and a secondary forced circulation evaporative crystallization system completely enters a steam compressor, after the compressor applies work to the secondary steam for compression, the temperature and the pressure of the steam are improved, then the steam is conveyed to a first-stage forced circulation heater and a second-stage forced circulation heater, the shell pass of the first-stage forced circulation heater and the shell pass of the second-stage forced circulation heater are used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to.
4. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 3, wherein the evaporation temperature of the MVR primary forced circulation evaporative concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR secondary forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa.
5. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, which adopts a two-effect forced circulation MVR evaporative concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR one-effect forced circulation evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR two-effect forced circulation evaporation crystallizer, supplying secondary steam generated by the first effect to a shell pass of a two-effect forced circulation heater, heating the solution, and continuously evaporating and concentrating the solution;
in the MVR steam compression part, the secondary steam generated by the MVR two-effect forced circulation evaporative crystallization system completely enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to a shell pass of a one-effect forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
6. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 5, wherein the MVR single-effect forced circulation evaporative concentration part has an evaporation temperature of 90 ℃, a discharge concentration of 24% and a vacuum degree of-0.3 MPa; the evaporation temperature of the MVR dual-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%.
7. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, which adopts a first-level falling film + second-level forced circulation MVR evaporative concentration process; it is characterized in that the preparation method is characterized in that,
the MVR evaporation concentration crystallization part comprises a falling film evaporation concentration part and a forced circulation evaporation crystallization part; the preheated solution enters an MVR falling film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; evaporating to a certain concentration, transferring the material to an MVR forced circulation evaporation crystallizer, heating the solution by utilizing secondary steam compressed by a steam compressor, continuously evaporating and concentrating the solution, separating out a small amount of sodium chloride crystals in the process, discharging crystal mush into a thickener through an online control system after the solution is concentrated to a certain concentration, preliminarily separating mother liquor and the crystal mush in the thickener, allowing supernatant to flow into a mother liquor tank for storage, allowing the thickened crystal mush to enter a centrifuge for separation, allowing the separated salt to be used as a NaCl product, returning the centrifuged mother liquor to the mother liquor tank, and conveying the mother liquor to a lithium making process workshop through a mother liquor pump;
in the MVR steam compression part, all secondary steam generated by the MVR falling film evaporation concentration system and the MVR forced circulation evaporation crystallization system enters a steam compressor, the compressor applies work to compress the secondary steam, the temperature and the pressure of the steam are improved, then the steam is conveyed to a shell pass of a falling film evaporator and a forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
8. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 7, wherein the evaporation temperature of the MVR falling film evaporative concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa.
9. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, which adopts a primary climbing film + secondary forced circulation MVR evaporative concentration process; it is characterized in that the preparation method is characterized in that,
the MVR evaporation concentration crystallization part comprises a climbing film evaporation concentration part and a forced circulation evaporation crystallization part; the preheated solution enters an MVR climbing film evaporation device, secondary steam compressed by a steam compressor is used for heating the MVR climbing film evaporation device, and the solution starts to be evaporated and concentrated; evaporating to a certain concentration, transferring the material to an MVR forced circulation evaporation crystallizer, heating the solution by utilizing secondary steam compressed by a steam compressor, continuously evaporating and concentrating the solution, separating out a small amount of sodium chloride crystals in the process, discharging crystal mush into a thickener through an online control system after the solution is concentrated to a certain concentration, preliminarily separating mother liquor and the crystal mush in the thickener, allowing supernatant to flow into a mother liquor tank for storage, allowing the thickened crystal mush to enter a centrifuge for separation, allowing the separated salt to be used as a NaCl product, returning the centrifuged mother liquor to the mother liquor tank, and conveying the mother liquor to a lithium making process workshop through a mother liquor pump;
in the MVR steam compression part, all secondary steam generated by the MVR climbing film evaporation concentration system and the MVR forced circulation evaporation crystallization system enters a steam compressor, the compressor applies work to compress the secondary steam, the temperature and the pressure of the steam are improved, then the steam is conveyed to a climbing film evaporator and a shell pass of a forced circulation heater to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
10. The MVR evaporative concentration crystallization process of claim 9, wherein the evaporation temperature of the MVR climbing film evaporative concentration part is 90 ℃; the effective temperature difference is 11 ℃; the discharge concentration is 24 percent, and the vacuum degree is-0.3 MPa; the evaporation temperature of the MVR forced circulation evaporation crystallization part is 90 ℃; the effective temperature difference is 5.6 ℃; the discharge concentration is 42.2 percent, and the vacuum degree is-0.3 MPa.
11. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, which adopts a one-effect climbing film + two-effect forced circulation MVR evaporative concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR one-effect climbing film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR two-effect forced circulation evaporation crystallizer, supplying secondary steam generated by the first effect to a shell pass of a two-effect forced circulation heater, heating the solution, and continuously evaporating and concentrating the solution;
in the MVR steam compression part, all secondary steam generated by the MVR two-effect forced circulation evaporation crystallization system enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to the shell pass of the one-effect climbing film evaporator to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
12. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 11, wherein the MVR single-effect climbing film evaporative concentration part has an evaporation temperature of 90 ℃, a discharge concentration of 24% and a vacuum degree of-0.3 MPa; the evaporation temperature of the MVR dual-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%.
13. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, which adopts a one-effect falling film + two-effect forced circulation MVR evaporative concentration process; it is characterized in that the preparation method is characterized in that,
in the MVR evaporation concentration crystallization part, the preheated solution enters an MVR one-effect falling film evaporation device, secondary steam compressed by a steam compressor is used for heating the solution, and the solution starts to be evaporated and concentrated; after the solution is evaporated to a certain concentration, transferring the material to an MVR two-effect forced circulation evaporation crystallizer, supplying secondary steam generated by the first effect to a shell pass of a two-effect forced circulation heater, heating the solution, and continuously evaporating and concentrating the solution;
in the MVR steam compression part, all secondary steam generated by the MVR two-effect forced circulation evaporation crystallization system enters a steam compressor, the temperature and the pressure of the steam are improved after the compressor applies work and compresses the secondary steam, then the steam is conveyed to the shell pass of the one-effect falling film evaporator to be used as heating steam, and high-temperature condensed water and non-condensable gas formed after the steam is condensed are returned to the material feeding preheating part to be used as a heat source for feeding preheating.
14. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 13, wherein the MVR single-effect falling film evaporative concentration part has an evaporation temperature of 90 ℃, a discharge concentration of 24% and a vacuum degree of-0.3 MPa; the evaporation temperature of the MVR dual-effect forced circulation evaporation crystallization part is 70 ℃, and the discharge concentration is 42.2%.
15. The MVR evaporative concentration crystallization process for extracting lithium from salt lake brine according to claim 1, which adopts an MVR evaporative concentration crystallization extraction lithium + MVR refluxing lithium mother liquor evaporative concentration extraction process, and comprises a preheating part, a lithium-containing concentrated liquor treatment part and an MVR refluxing lithium mother liquor concentration part; it is characterized in that the preparation method is characterized in that,
the preheating part preheats the stock solution by adopting the self heat of a recovery system to a set evaporation temperature value;
the MVR evaporation concentration crystallization part adopts an MVR high-efficiency energy-saving evaporation concentration technology to crystallize and separate the sodium chloride in the mixed salt to obtain salt, and the high-purity lithium-containing salt lake brine after the sodium chloride is extracted is subjected to a back-end process;
in the lithium-containing concentrated solution treatment part, treating the lithium-containing concentrated solution meeting the requirements to obtain a finished product of lithium carbonate and lithium-containing mother solution with low lithium ion concentration;
in the MVR reflux lithium mother liquor concentration part, the lithium ion mother liquor with high purity and low content enters an MVR evaporation concentration system for concentration, and when the concentration is increased to a proper concentration, the lithium ion mother liquor returns to the former stage process for reuse.
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