CN107828960A

CN107828960A - The collaboration extraction system and its processing method of magnesium and lithium in a kind of salt lake bittern

Info

Publication number: CN107828960A
Application number: CN201711091350.3A
Authority: CN
Inventors: 杨刚; 谢旭阳; 王云山; 杨朝勇; 安学斌
Original assignee: Beijing Jixiang Sightsee Technology Development Co ltd; Institute of Process Engineering of CAS
Current assignee: Beijing Jixiang Sightsee Technology Development Co ltd; Institute of Process Engineering of CAS
Priority date: 2017-11-08
Filing date: 2017-11-08
Publication date: 2018-03-23
Anticipated expiration: 2037-11-08
Also published as: CN107828960B

Abstract

The invention provides the collaboration extraction system and its processing method of magnesium in a kind of salt lake bittern and lithium, the collaboration extraction system mainly includes spray roasting system, dust pelletizing system, slurrying wash mill, equipment for separating liquid from solid, carries magnesium unit, carries lithium unit and smoke processing system；Wherein, the product for carrying magnesium unit includes magnesia, and the product for carrying lithium unit includes magnesium hydrate precipitate and lithium carbonate, and carrying magnesium unit described in the magnesium hydrate precipitate entrance carries out carrying magnesium.Wet method Reaction Separation and pyrogenic process are purified organic coupling by the present invention, the conventional process techniques of salt lake bittern element extraction are integrated, realize the high-valued collaboration extraction of valuable element magnesium and lithium in salt lake bittern, simultaneously fume afterheat is made full use of in extraction process, realize heat cascade utilization, produced without waste water and waste residue, tail gas qualified discharge, belong to a kind of greenization cleaner technology.

Description

The collaboration extraction system and its processing method of magnesium and lithium in a kind of salt lake bittern

Technical field

The invention belongs to salt lake bittern Resource Access field, is related to the collaboration extraction system of magnesium and lithium in a kind of salt lake bittern And its processing method.

Background technology

With petering out for global fossil energy, lithium has become the ideal material of the 21 century energy and alloy in lightweight, It is referred to as the important element for promoting the world to advance, has in fields such as high-energy battery, Aero-Space and nuclear fusion generatings important Purposes.Magnesium is similar with lithium, has the various uses of light metal, and magnesia is a kind of its most important oxide, has excellent The performances such as alkaline-resisting, heat-resisting and insulation, it is widely used.

Salt lake bittern aboundresources, rich in a variety of valuable elements, salt lake bittern passes through salt manufacturing, extraction boron, potassium, bromine, iodine etc. After element, the lithium and most magnesium that there are about 80% or so are stayed in mother liquor.Compared with carrying lithium from ore, salt lake carries lithium more It is easy, cost is lower, therefore, bittern carries lithium substitution ore and carries lithium turns into development trend.

Because element is numerous contained by salt lake bittern, especially two kinds of element physicochemical properties of magnesium and lithium are similar, and separating difficulty is big. At present, have from the main method of extracting lithium from salt lake brine：(1) precipitation method, (2) aluminate method, (3) ion exchange adsorption, (4) Carbonizatin method and (5) solvent extraction.Patent CN 1618997A provide a kind of side of combined extracting magnesium, lithium from salt lake bittern Method, using two sections of magnesium sinkings of ammonia and ammonium hydrogen carbonate, realize that magnesium, lithium efficiently separating and extracting, produce a set of magnesium products and lithium carbonate, This method is related to the circulation of ammonia, and similar with other precipitation method, reliability of technology is preferable, but technological process is more complicated；Patent CN 106430254A discloses a kind of method from extracting lithium from salt lake brine, and the method produces aluminium salt with activation kaolin salt Ore Leaching, It is then added to salt lake bittern to be reacted, obtains precipitating containing lithium, it is similar with other aluminate methods, although alkaline consumption is low, water Evaporation is big, and processing cost is higher；Patent CN 104925836A provide a kind of ion exchange absorption that lithium is carried from bittern containing lithium The problems such as method, this method is selectively good, and the rate of recovery is high, but polymeric adsorbent cost is high, short life and regeneration are difficult turns into main Restraining factors；Patent CN 1335263A provide a kind of method for being carbonized and carrying lithium, and this method adds heavy first in salt lake bittern Shallow lake agent so that Mg²⁺And Li⁺It is precipitated out, then by carbonization or the precipitation dissolving of carbonation lithium, reaches separating magnesium and lithium Effect, is finally made lithium carbonate, and carbonizatin method cost is low, it is easy to accomplish industrialization, but yield is low, carbon dioxide in addition be present Carry out source problem；Patent CN 102001692A provide the synergistic system that a kind of salt lake bittern extraction carries lithium, extraction used Method is selectively preferable, but that equipment corrosion is serious and extractant loss, cost are higher be present.

In summary, existing method focus on more it is single carry lithium, resource utilization is not high, less economical, and exists certain Problem, therefore, such as how easier method, relatively low cost realize the collaboration extraction of magnesium and lithium, realize that Brine resources are efficient Using be salt lake bittern exploitation urgent problem.

The content of the invention

For problems of the prior art, the invention provides the collaboration of magnesium and lithium in a kind of salt lake bittern to extract system System and its processing method.The present invention utilizes hydrometallurgy and the respective advantage of pyrometallurgy, and wet method Reaction Separation and pyrogenic process are carried Pure organic coupling, the conventional process techniques of salt lake bittern element extraction are integrated, realize element magnesium and lithium in salt lake bittern High-valued collaboration extraction；Fume afterheat is made full use of simultaneously, realizes heat cascade utilization, without waste water and waste residue in extraction process Produce, tail gas qualified discharge, belong to a kind of greenization cleaner technology.

To use following technical scheme up to this purpose, the present invention：

On the one hand, the invention provides the collaboration extraction system of magnesium in a kind of salt lake bittern and lithium, the collaboration extraction system System mainly include spray roasting system, dust pelletizing system, slurrying wash mill, equipment for separating liquid from solid, carry magnesium unit, carry lithium unit and Smoke processing system；Wherein, the material outlet of the spray roasting system is connected with the material inlet of the dust pelletizing system, described The exhanst gas outlet of dust pelletizing system is connected with the gas access of the smoke processing system, the solid matter outlet of the dust pelletizing system Be connected successively with the slurrying wash mill and equipment for separating liquid from solid, the solid matter outlet of the equipment for separating liquid from solid with it is described The material inlet for carrying magnesium unit is connected, the liquid outlet of the equipment for separating liquid from solid and the material inlet phase for carrying lithium unit Even, the product for carrying magnesium unit includes magnesia, and the product for carrying lithium unit includes magnesium hydrate precipitate and lithium carbonate, institute State magnesium hydrate precipitate enter described in carry magnesium unit and carry out carrying magnesium.

In the present invention, the collaboration extraction system comprehensive utilization wet method and pyrogenic process purification technique, pass through the phase between each system Connect, effective reuse of material, drastically increase magnesium and the yield of lithium collaboration extraction in salt lake bittern, realize that its is high-valued Utilize.

Currently preferred technical scheme is used as below, but not as the limitation of technical scheme provided by the invention, is passed through Following technical scheme, it can preferably reach and realize the technical purpose and beneficial effect of the present invention.

As currently preferred technical scheme, the spray roasting system includes air compressor machine and spray roasting tower, described The gas vent of air compressor machine is connected with the bottom gas inlet of spray roasting tower.

Preferably, the dust pelletizing system includes cyclone separator and sack cleaner, and the flue gas of the cyclone separator goes out Mouth is connected with the entrance of sack cleaner.

In the present invention, the spray roasting tower outlet material is introduced into cyclone separator, enters back into sack cleaner, so It is higher to be provided in just leaving the temperature of charge of spray roasting tower, in general sack cleaner is difficult to meet the temperature requirement；Institute The solid matter outlet for stating cyclone separator and sack cleaner is connected with the slurrying wash mill, and flue gas by removing twice Dirt so that gas is sufficiently separated with solid, to improve the yield of product.

Preferably, it is described to carry the first slurrying wash mill, the first equipment for separating liquid from solid, that magnesium unit includes being sequentially connected Two slurrying wash mills, the second equipment for separating liquid from solid and calcining furnace, the liquid outlet of first equipment for separating liquid from solid obtain chlorine Change sodium solution, the liquid outlet of second equipment for separating liquid from solid is connected with the top entry of the first slurrying wash mill, described The solid outlet of second equipment for separating liquid from solid is connected with the entrance of calcining furnace.

Preferably, evaporator, the first settler, the 3rd the separation of solid and liquid dress for carrying lithium unit and including being sequentially connected Put, the second settler and the 4th equipment for separating liquid from solid, the evaporator condensation liquid export the top with the second slurrying wash mill Portion's entrance is connected, and the solid outlet of the 3rd equipment for separating liquid from solid is connected with the top entry of the first slurrying wash mill, institute State and conveyer is also associated with after the 4th equipment for separating liquid from solid, it is molten that the liquid outlet of the 4th equipment for separating liquid from solid obtains sodium chloride Liquid.

In the present invention, magnesium hydrate precipitate caused by first settler returns to after separation of solid and liquid described carries magnesium First slurrying wash mill of unit, can effectively improve the recovery rate of magnesium elements in salt lake bittern, avoid the waste of resource, Better economy.

Preferably, before the bottom inlet of the spray roasting tower, between slurrying wash mill and equipment for separating liquid from solid, first Between slurrying wash mill and the first equipment for separating liquid from solid, the second slurrying wash mill and the second separation of solid and liquid dress between, first Between settler and the 3rd equipment for separating liquid from solid pump is equipped between the second settler and the 4th equipment for separating liquid from solid.

As currently preferred technical scheme, the air compressor machine is screw compressor or piston compressor.

Preferably, the cyclone separator includes single tube cyclone dust collectors and/or multi-tube dust cleaner.

Preferably, the equipment for separating liquid from solid, the first equipment for separating liquid from solid, the second equipment for separating liquid from solid, the 3rd solid-liquid point It is filter or centrifugal device, preferably plate and frame filter press from device and the 4th equipment for separating liquid from solid.

Preferably, the evaporator is triple effect falling film evaporator.

Preferably, the pump is any one in centrifugal pump, reciprocating pump, rotary pump or peripheral pump or at least two group Close, the combination is typical but non-limiting examples have：The combination of the combination of centrifugal pump and reciprocating pump, centrifugal pump and rotary pump, it is past The combination of multiple pump and peripheral pump, the combination of reciprocating pump, rotary pump and peripheral pump, combination of centrifugal pump, reciprocating pump and peripheral pump etc..

As currently preferred technical scheme, the smoke processing system includes neutralizing absorption tower and mist projection granulating tower, The outlet at bottom for neutralizing absorption tower is connected with the liquid inlet of mist projection granulating tower, and the outlet of the mist projection granulating tower obtains chlorine Change calcium product.

Preferably, the smoke processing system also includes heat exchanger and calcification sizing device, the heat of the heat exchanger Fluid intake is connected with the exhanst gas outlet of the sack cleaner, and the hot fluid outlet ports of the heat exchanger absorb with described neutralize The bottom gas inlet of tower is connected, and the outlet of the calcification sizing device is connected with the bottom slurry import on neutralization absorption tower.

Preferably, circulating pump, the entrance of the circulating pump and institute are provided between the neutralization absorption tower and mist projection granulating tower The outlet at bottom for stating neutralization absorption tower is connected, the top entry and mist projection granulating tower of the outlet and neutralization absorption tower of the circulating pump Liquid inlet be connected.

As currently preferred technical scheme, the heat exchanger is tubular heat exchanger.

Preferably, the neutralization absorption tower is three-level circulating absorption tower.

Preferably, the circulating pump is any one in centrifugal pump, reciprocating pump, rotary pump or peripheral pump.

Second aspect, the invention provides the processing method of above-mentioned collaboration extraction system, it the described method comprises the following steps：

(a) salt lake bittern is subjected to spray roasting, then removing dust handles to obtain solid material and flue gas；

(b) by solid material that step (a) obtains obtain after slurrying washing and separation of solid and liquid liquid material containing lithium with Solid material containing magnesium；

(c) solid material containing magnesium that step (b) obtains is obtained into magnesium hydroxide after multipolarity plasm scouring and separation of solid and liquid Solid, then obtain magnesia through calcining；

(d) liquid material containing lithium for obtaining step (b) is successively through being concentrated by evaporation, after multi stage precipitation reaction and separation of solid and liquid Magnesium hydroxide and lithium carbonate are obtained, obtained magnesium hydroxide return to step (c) is handled.

As currently preferred technical scheme, step (a) salt lake bittern refers to after extraction potassium, sodium and bromine Based on magnesium chloride, the solution containing lithium chloride and sodium chloride, wherein content of magnesium are 80-150g/L, such as 80g/L, 90g/L, 100g/L, 110g/L, 120g/L, 130g/L, 140g/L or 150g/L etc., it is not limited to cited numerical value, the numerical value In the range of other unrequited numerical value it is equally applicable；Chlorinity is 260-500g/L, for example, 260g/L, 290g/L, 320g/L, 350g/L, 380g/L, 410g/L, 440g/L, 470g/L or 500g/L etc., it is not limited to cited numerical value, the numerical value In the range of other unrequited numerical value it is equally applicable；Lithium content is 4-8g/L, such as 4g/L, 4.5g/L, 5g/L, 5.5g/L, 6g/ L, 6.5g/L, 7g/L, 7.5g/L or 8g/L etc., it is not limited to cited numerical value, other are unrequited in the number range Numerical value it is equally applicable；Sodium content is 1-2g/L, such as 1g/L, 1.2g/L, 1.4g/L, 1.6g/L, 1.8g/L or 2g/L etc., It is not limited to cited numerical value, other interior unrequited numerical value of the number range are equally applicable.

Preferably, step (a) the salt lake bittern feeding temperature be 30-50 DEG C, such as 30 DEG C, 33 DEG C, 36 DEG C, 39 DEG C, 42 DEG C, 45 DEG C, 48 DEG C or 50 DEG C etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range It is equally applicable.

Preferably, step (a) spray roasting is needed to be passed through compressed air, and the compressed air is provided by air compressor machine.

Preferably, the compressed air pressure is 0.4-0.6MPa, for example, 0.4MPa, 0.42MPa, 0.45MPa, 0.48MPa, 0.5MPa, 0.53MPa, 0.55MPa, 0.57MPa or 0.6MPa etc., it is not limited to cited numerical value, should Other unrequited numerical value are equally applicable in number range；Intake air temperature be 30-50 DEG C, such as 30 DEG C, 33 DEG C, 36 DEG C, 39 DEG C, 42 DEG C, 45 DEG C, 48 DEG C or 50 DEG C etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range It is equally applicable.

Preferably, the compressed air and salt lake bittern volume ratio are (90-120):1, such as 90:1、95:1、100:1、 105:1、110:1、115:1 or 120:1 etc., it is not limited to cited numerical value, other are unrequited in the number range Numerical value is equally applicable.

Preferably, step (a) spray roasting is carried out in the case where fuel provides heat condition.

Preferably, the fuel is any one in methanol, diesel oil, liquefied gas or natural gas.

In the present invention, fuel used general single use, it is possible to prevente effectively from fuel is used in mixed way the blast easily caused It is dangerous.

Preferably, step (a) spray roasting is carried out in spray roasting tower.

Preferably, the spray roasting column bottom temperature be 600-800 DEG C, such as 600 DEG C, 630 DEG C, 660 DEG C, 690 DEG C, 720 DEG C, 750 DEG C, 780 DEG C or 800 DEG C etc., it is not limited to cited numerical value, other are unrequited in the number range Numerical value is equally applicable；Head temperature be 350-550 DEG C, such as 350 DEG C, 380 DEG C, 400 DEG C, 430 DEG C, 450 DEG C, 480 DEG C, 500 DEG C, 520 DEG C or 550 DEG C etc., it is not limited to cited numerical value, other unrequited numerical value are equally suitable in the number range With.

Preferably, residence time of material is 2-6s in the spray roasting tower, for example, 2s, 2.5s, 3s, 3.5s, 4s, 4.5s, 5s, 5.5s or 6s etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range are same It is applicable, preferably 3-5s.

Preferably, the spray roasting tower outlet mass temperatures be 300-500 DEG C, such as 300 DEG C, 330 DEG C, 360 DEG C, 390 DEG C, 420 DEG C, 450 DEG C, 480 DEG C or 500 DEG C etc., it is not limited to cited numerical value, in the number range, other are not The numerical value enumerated is equally applicable.

Preferably, step (a) dust removal process is carried out in cyclone separator and sack cleaner respectively.

Preferably, the sack cleaner input gas temperature be 220-320 DEG C, such as 220 DEG C, 240 DEG C, 260 DEG C, 280 DEG C, 300 DEG C or 320 DEG C etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range are same Sample is applicable, preferably 250-300 DEG C.

Preferably, the sack cleaner exit gas temperature be 200-300 DEG C, such as 200 DEG C, 220 DEG C, 240 DEG C, 260 DEG C, 280 DEG C or 300 DEG C etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range are same Sample is applicable, preferably 220-280 DEG C.

In the present invention, the flue-gas temperature into sack cleaner can not be too high, and otherwise sack cleaner is difficult to bear, therefore Need to first pass through cyclone separator separation and cooling；The flue-gas temperature for leaving sack cleaner should not be too low, and temperature is too low, cigarette Acid gas in gas easily becomes acid solution, causes sack cleaner to block.

Preferably, step (b) and step (c) washing are countercurrent washing.

Preferably, step (b) and step (c) separation of solid and liquid are to be separated by filtration.

Preferably, step (b) and the washing of step (c) slurrying and separation of solid and liquid operation temperature are 50-90 DEG C, such as 50 DEG C, 55 DEG C, 60 DEG C, 65 DEG C, 70 DEG C, 75 DEG C, 80 DEG C, 85 DEG C or 90 DEG C etc., it is not limited to cited numerical value, the numerical value In the range of other unrequited numerical value it is equally applicable, preferably 60-80 DEG C.

Preferably, step (c) the multipolarity plasm scouring and separation of solid and liquid are the washing of two-stage slurrying and separation of solid and liquid.

Preferably, step (c) calcining is carried out in calcining furnace.

Preferably, step (c) calcining heat be 400-800 DEG C, such as 400 DEG C, 450 DEG C, 500 DEG C, 550 DEG C, 600 DEG C, 650 DEG C, 700 DEG C, 750 DEG C or 800 DEG C etc., it is not limited to cited numerical value, other are unrequited in the number range Numerical value it is equally applicable, preferably 550-750 DEG C, more preferably 600-700 DEG C.

Preferably, step (c) calcination time is 0.5-2h, such as 0.5h, 0.75h, 1h, 1.25h, 1.5h, 1.75h Or 2h etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range are equally applicable, are preferably 0.8-1.2h。

Preferably, content of magnesia is more than 98wt% in step (c) magnesium oxide product, such as 98.1wt%, 98.4wt%, 98.7wt%, 99.0wt%, 99.3wt%, 99.6wt% or 99.9wt% etc., it is not limited to cited Numerical value, other interior unrequited numerical value of the number range are equally applicable.

Preferably, step (d) evaporation and concentration is carried out in evaporator.

Preferably, step (d) evaporation and concentration is using steam as thermal source.

Preferably, 120-160 DEG C of the inlet steam temperature, for example, 120 DEG C, 125 DEG C, 130 DEG C, 135 DEG C, 140 DEG C, 145 DEG C, 150 DEG C, 155 DEG C or 160 DEG C etc., it is not limited to cited numerical value, other are unrequited in the number range Numerical value is equally applicable, preferably 130-150 DEG C.

Preferably, the steam condensate outlet temperature be 60-90 DEG C, such as 60 DEG C, 65 DEG C, 70 DEG C, 75 DEG C, 80 DEG C, 85 DEG C or 90 DEG C etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range are equally applicable, excellent Elect 70-80 DEG C as.

Preferably, step (d) the multi stage precipitation reaction and separation of solid and liquid are respectively one-level precipitation reaction and separation of solid and liquid And two-stage precipitation reaction and separation of solid and liquid.

Preferably, the one-level precipitation reaction is reacted for magnesium sinking, using sodium hydroxide as precipitating reagent.

Preferably, the one-level precipitation reaction temperature be 50-90 DEG C, such as 50 DEG C, 55 DEG C, 60 DEG C, 65 DEG C, 70 DEG C, 75 DEG C, 80 DEG C, 85 DEG C or 90 DEG C etc., it is not limited to cited numerical value, other unrequited numerical value are same in the number range Sample is applicable, preferably 60-80 DEG C.

Preferably, the one-level precipitation reaction time is 10-40min, for example, 10min, 15min, 20min, 25min, 30min, 35min or 40min etc., it is not limited to cited numerical value, other interior unrequited numerical value of the number range are same Sample is applicable.

Preferably, the two-stage precipitation reaction is reacted for sinker, using sodium carbonate as precipitating reagent.

Preferably, the two-stage precipitation reaction temperature be 50-90 DEG C, such as 50 DEG C, 55 DEG C, 60 DEG C, 65 DEG C, 70 DEG C, 75 DEG C, 80 DEG C, 85 DEG C or 90 DEG C etc., it is not limited to cited numerical value, other unrequited numerical value are same in the number range Sample is applicable, preferably 60-80 DEG C.

Preferably, the precipitation reaction time described in the two level is 20-50min, for example, 20min, 25min, 30min, 35min, 40min, 45min or 50min etc., it is not limited to cited numerical value, other are unrequited in the number range Numerical value is equally applicable.

Preferably, step (d) separation of solid and liquid is is separated by filtration, and operation temperature is 50-90 DEG C, for example, 50 DEG C, 55 DEG C, 60 DEG C, 65 DEG C, 70 DEG C, 75 DEG C, 80 DEG C, 85 DEG C or 90 DEG C etc., it is not limited to cited numerical value, in the number range its His unrequited numerical value is equally applicable, preferably 60-80 DEG C.

As currently preferred technical scheme, the flue gas that step (a) is obtained is handled, its processing method include with Lower step：

(A) flue gas for obtaining step (a) carries out neutralization absorption after heat exchange, obtains calcium chloride solution, and tail gas is up to standard Discharge；

(B) calcium chloride solution that step (A) obtains is obtained into calcium chloride product through mist projection granulating.

As currently preferred technical scheme, step (A) described heat exchange is using air as low-temperature receiver.

Preferably, after step (A) described heat exchange air themperature be 150-230 DEG C, such as 150 DEG C, 160 DEG C, 170 DEG C, 180 DEG C, 190 DEG C, 200 DEG C, 210 DEG C, 220 DEG C or 230 DEG C etc., it is not limited to cited numerical value, in the number range Other unrequited numerical value are equally applicable, preferably 170-210 DEG C.

Preferably, after step (A) described heat exchange flue-gas temperature be 120-180 DEG C, such as 120 DEG C, 130 DEG C, 140 DEG C, 150 DEG C, 160 DEG C, 170 DEG C or 180 DEG C etc., it is not limited to cited numerical value, other are unrequited in the number range Numerical value is equally applicable, preferably 130-150 DEG C.

Preferably, described neutralize of step (A) absorbs in and carried out in absorption tower.

Preferably, described neutralize of step (A) is absorbed using milk of lime as nertralizer, and its mass concentration is 5%-10%, such as 5%th, 5.5%, 6%, 6.5%, 7%, 7.5%, 8%, 8.5%, 9%, 9.5% or 10% etc., it is not limited to cited Numerical value, other unrequited numerical value are equally applicable in the number range.

Preferably, the milk of lime is handled to obtain by lime and water through slurrying.

Preferably, the slurrying processing is carried out in calcification stock tank.

Preferably, step (A) the hydrogen chloride in tail gas content is not more than 10ppm, for example, 10ppm, 9ppm, 8ppm, 7ppm, 6ppm, 5ppm, 4ppm, 3ppm, 2ppm or 1ppm etc., it is not limited to cited numerical value, in the number range its His unrequited numerical value is equally applicable, preferably not greater than 5ppm.

Preferably, step (B) described mist projection granulating is carried out in mist projection granulating tower.

Preferably, step (B) mist projection granulating is using the air after step (A) heat exchange as thermal source.

As currently preferred technical scheme, the described method comprises the following steps：

(I) it is the salt lake bittern that temperature is 30-50 DEG C and the compression that pressure is 0.4-0.6Mpa, temperature is 30-50 DEG C is empty Gas is calcined in the case where fuel provides heat condition into spray roasting tower, and wherein compressed air is with salt lake bittern volume ratio (90-120):1, spray roasting column bottom temperature is 600-800 DEG C, and head temperature is 350-550 DEG C, when material stops in tower Between be 3-5s, spray roasting top of tower outlet mass temperatures are 300-500 DEG C, sequentially enter cyclone separator and sack cleaner Dust removal process is carried out, obtains solid material and flue gas, is 250-300 DEG C into flue-gas temperature during sack cleaner, leaves cloth bag Flue-gas temperature is 220-280 DEG C during deduster；

(II) solid material that step (I) obtains is subjected to slurrying, countercurrent washing and is separated by filtration processing, operation temperature is 60-80 DEG C, obtain liquid material containing lithium and solid material containing magnesium；

(III) flue gas for obtaining step (I) carries out heat exchange with air in a heat exchanger, leaves heat exchanger space-time Temperature degree is 170-210 DEG C, and flue-gas temperature is 130-150 DEG C, and flue gas after leaving, which enters, neutralizes absorption tower, and from calcification The milk of lime contact that the mass concentration of stock tank is 5%-10% carries out neutralization absorption, and emptying hydrogen chloride in tail gas concentration is not higher than 5ppm, resulting solution enter mist projection granulating tower, make thermal source progress mist projection granulating to leave the air of heat exchanger, obtain calcium chloride Product；

(IV) solid material containing magnesium for obtaining step (II) through two-stage slurrying, countercurrent washing and is separated by filtration processing again, Operation temperature is 60-80 DEG C, obtains magnesium hydroxide solid, gained magnesium hydroxide solid is calcined under the conditions of 600-700 DEG C 0.8-1.2h, obtain the high-purity magnesium oxide that content of magnesia is more than 98%；

(V) liquid material containing lithium that step (II) obtains is evaporated concentration in evaporator, with 130-150 DEG C Steam is thermal source, and the solution after concentration carries out magnesium sinking reaction by precipitating reagent of sodium hydroxide, and reaction temperature is 60-80 DEG C, reaction Time is 10-40min, is separated by filtration under the conditions of 60-80 DEG C, and obtained magnesium hydroxide return to step (IV) is handled, and is obtained The solution arrived carries out sinker reaction by precipitating reagent of sodium carbonate again, and reaction temperature is 60-80 DEG C, reaction time 20-50min, It is separated by filtration under the conditions of 60-80 DEG C, obtains lithium carbonate product and sodium chloride solution.

Compared with prior art, the invention has the advantages that：

(1) system of the present invention is mutually combined, and the technical process is mutually integrated, by Reaction Separation with purifying organic coupling Close, realize that the yield of lithium reaches more than 93%, the yield of magnesium in high yield by the extraction of the multi-level collaborative of magnesium in salt lake bittern and lithium Up to more than 98%；

(2) System and method for of the present invention industrializing implementation, products obtained therefrom seriation, high-valued, energy is reasonable Cascade utilization, Atom economy are notable；

(3) present invention produces without waste water and waste residue, waste gas qualified discharge, process cleans environmental protection, is valuable in salt lake bittern The synthesis of element provides new approach.

Brief description of the drawings

Fig. 1 is the device connection diagram that extraction system is cooperateed with described in the embodiment of the present invention 1；

Fig. 2 is the process flow diagram that extraction system is cooperateed with described in the embodiment of the present invention 3；

Wherein, 1- air compressor machines, 2- spray roasting towers, 3- cyclone separators, 4- sack cleaners, 5- heat exchangers, 6- stones Stock tank is ashed, in 7- and absorption tower, 8- mist projection granulating towers, 9- slurrying wash mills, 10- equipment for separating liquid from solid, the slurryings of 11- first Wash mill, the equipment for separating liquid from solid of 12- first, 13- the second slurrying wash mills, the equipment for separating liquid from solid of 14- second, 15- calcinings Stove, 16- evaporators, the settlers of 17- first, the equipment for separating liquid from solid of 18- the 3rd, the settlers of 19- second, the solid-liquids of 20- the 4th Separator, 21- conveyers.

Embodiment

For the present invention is better described, technical scheme is readily appreciated, below to the present invention further specifically It is bright.But following embodiments is only the simple example of the present invention, the scope of the present invention is not represented or limits, this Invention protection domain is defined by claims.

Specific embodiment of the invention part provides magnesium and the collaboration extraction system of lithium and its place in a kind of salt lake bittern Reason method, the collaboration extraction system mainly include spray roasting system, dust pelletizing system, slurrying wash mill 9, separation of solid and liquid dress 10 are put, magnesium unit is carried, carries lithium unit and smoke processing system；Wherein, the material outlet of the spray roasting system removes with described The material inlet of dirt system is connected, and the exhanst gas outlet of the dust pelletizing system is connected with the gas access of the smoke processing system, The solid matter outlet of the dust pelletizing system is connected with the slurrying wash mill 9 and equipment for separating liquid from solid 10 successively, described solid The solid matter outlet of liquid separating apparatus 10 is connected with the material inlet for carrying magnesium unit, the liquid of the equipment for separating liquid from solid 10 Body outlet is connected with the material inlet for carrying lithium unit, and the product for carrying magnesium unit includes magnesia, described to carry lithium unit Product include magnesium hydrate precipitate and lithium carbonate, the magnesium hydrate precipitate enter described in carry magnesium unit and carry out carrying magnesium.

Its processing method comprises the following steps：

It is below present invention typical case but non-limiting example：

Embodiment 1：

The collaboration extraction system of magnesium and lithium in a kind of salt lake bittern is present embodiments provided, as shown in figure 1, the collaboration carries System is taken mainly to include spray roasting system, dust pelletizing system, slurrying wash mill 9, plate and frame filter press 10, carry magnesium unit, carry lithium Unit and smoke processing system；Wherein, the material outlet of the spray roasting system and the material inlet phase of the dust pelletizing system Even, the exhanst gas outlet of the dust pelletizing system is connected with the gas access of the smoke processing system, the solid of the dust pelletizing system Material outlet is connected with the slurrying wash mill 9 and plate and frame filter press 10 successively, the solid material of the plate and frame filter press 10 Outlet is connected with the material inlet for carrying magnesium unit, the liquid outlet of the plate and frame filter press 10 and the thing for carrying lithium unit Material entrance is connected, and the product for carrying magnesium unit includes magnesia, the product for carrying lithium unit include magnesium hydrate precipitate with Lithium carbonate, the magnesium hydrate precipitate enter described in carry magnesium unit and carry out carrying magnesium.

The spray roasting system includes screw compressor 1 and spray roasting tower 2, the gas of the screw compressor 1 Body outlet is connected with the bottom gas inlet of spray roasting tower 2.

The dust pelletizing system includes single tube cyclone dust collectors 3 and sack cleaner 4, the cigarette of the single tube cyclone dust collectors 3 Gas outlet is connected with the entrance of sack cleaner 4.

The first slurrying wash mill 11, the change of the first plate and frame filter press 12, second for carrying magnesium unit and including being sequentially connected Plasm scouring device 13, the second plate and frame filter press 14 and calcining furnace 15, the liquid outlet of first plate and frame filter press 12 obtain chlorine Change sodium solution, the liquid outlet of second plate and frame filter press 14 is connected with the top entry of the first slurrying wash mill 11, institute The solid outlet for stating the second plate and frame filter press 14 is connected with the entrance of calcining furnace 15.

The triple effect falling film evaporator 16, the first settler 17, the 3rd sheet frame pressure for carrying lithium unit and including being sequentially connected Filter 18, the second settler 19 and the 4th plate and frame filter press 20, the condensate outlet of triple effect falling film evaporator 16 and second The top entry of slurrying wash mill 13 is connected, the solid outlet and the first slurrying wash mill of the 3rd plate and frame filter press 18 11 top entry is connected, and conveyer 21, the 4th plate and frame filter press 20 are also associated with after the 4th plate and frame filter press 20 Liquid outlet obtain sodium chloride solution.

Before the bottom inlet of the spray roasting tower 2, between slurrying wash mill 9 and plate and frame filter press 10, the first slurrying Between the plate and frame filter press 12 of wash mill 11 and first, between the second slurrying wash mill 13 and the second plate and frame filter press 14, It is all provided between one settler 17 and the 3rd plate and frame filter press 18 between the second settler 19 and the 4th plate and frame filter press 20 There is centrifugal pump.

The smoke processing system includes tubular heat exchanger 5, calcification sizing device 6, three-level circulating absorption tower 7 and spraying Granulation tower 8, the thermal fluid inlet of the tubular heat exchanger 5 are connected with the exhanst gas outlet of the sack cleaner 4, the tubulation The hot fluid outlet ports of formula heat exchanger 5 are connected with the bottom gas inlet of the three-level circulating absorption tower 7, the calcification sizing device 6 outlet is connected with the bottom slurry import of three-level circulating absorption tower 7, the three-level circulating absorption tower 7 and mist projection granulating tower 8 it Between be provided with centrifugal pump, the entrance of the centrifugal pump is connected with the outlet at bottom of the three-level circulating absorption tower 7, the centrifugal pump Outlet is connected with the top entry of three-level circulating absorption tower 7 and the liquid inlet of mist projection granulating tower 8, the mist projection granulating tower 8 Outlet obtains calcium chloride product.

Embodiment 2：

Present embodiments provide the collaboration extraction system of magnesium and lithium in a kind of salt lake bittern, the device of the system and its company Connect with reference to embodiment 1, differ only in：The air compressor machine 1 is piston compressor, and the cyclone separator 3 is multi-tube dusting Device, the pump are reciprocating pump.

Embodiment 3：

The collaboration extracting method of magnesium and lithium in a kind of salt lake bittern is present embodiments provided, methods described uses embodiment 1 In system carry out, its technological process is as shown in Fig. 2 processing method comprises the following steps：

(I) it is 1m by inlet amount³/ h, temperature are 30 DEG C, content of magnesium 80g/L, lithium content 4g/L, sodium content 1g/ L, chlorinity for 260g/L salt lake bittern and pressure is 0.4Mpa, temperature provides heat for 30 DEG C of compressed air in natural gas Under the conditions of be calcined into spray roasting tower 2, wherein compressed air and salt lake bittern volume ratio are 120:1, spray roasting tower 2 Bottom temp is 600 DEG C, and head temperature is 350 DEG C, and material is 2s in dwell time in the tower, the top exit thing of spray roasting tower 2 Material temperature degree is 300 DEG C, sequentially enters cyclone separator 3 and sack cleaner 4 carries out dust removal process, obtain solid material and cigarette Gas, it is 250 DEG C into flue-gas temperature during sack cleaner 4, flue-gas temperature is 220 DEG C when leaving sack cleaner 4；

(II) solid material that step (I) obtains is subjected to slurrying, countercurrent washing and is separated by filtration processing, operation temperature is 50 DEG C, obtain liquid material containing lithium and solid material containing magnesium；

(III) flue gas for obtaining step (I) carries out heat exchange in heat exchanger 5 with air, into heat exchanger 5 Air temperature is 30 DEG C, and air themperature is 150 DEG C when leaving, and flue-gas temperature is 120 DEG C, and the flue gas after leaving, which enters to neutralize, to be inhaled Tower 7 is received, is contacted with the milk of lime that the mass concentration from calcification stock tank 6 is 5% and carries out neutralization absorption, generation calcium chloride is molten Liquid, tail gas qualified discharge, resulting solution enter mist projection granulating tower 8, and carrying out spraying as thermal source to leave the air of heat exchanger 5 makes Grain, obtains calcium chloride product；

(IV) solid material containing magnesium for obtaining step (II) through two-stage slurrying, countercurrent washing and is separated by filtration processing again, Operation temperature is 50 DEG C, obtains magnesium hydroxide solid, gained magnesium hydroxide solid is calcined into 2h under the conditions of 400 DEG C, obtains oxygen Change magnesium products；

(V) liquid material containing lithium that step (II) obtains is evaporated concentration in evaporator 16, with 120 DEG C of steaming Vapour is thermal source, and condensate outlet temperature is 60 DEG C, and the solution after concentration carries out magnesium sinking reaction, reaction by precipitating reagent of sodium hydroxide Temperature is 50 DEG C, reaction time 40min, is separated by filtration under the conditions of 50 DEG C, obtained magnesium hydroxide return to step (IV) is entered Row processing, obtained solution are again that precipitating reagent carries out sinker reaction using sodium carbonate, and reaction temperature is 50 DEG C, and the reaction time is 50min, it is separated by filtration under the conditions of 50 DEG C, obtains lithium carbonate product and sodium chloride solution.

To handle 1m³Salt lake bittern is foundation, and step (I) the spray roasting magnesium chloride resolution ratio is 80%, and gained is solid Body material is 200kg, is formed as shown in table 1-1.

Solid material forms after table 1-1 spray roastings

Hydrogen chloride in tail gas concentration obtained by step (III) is 5ppm, and it is 290kg to obtain calcium chloride product, and calcium chloride content is 99.1wt%.

Step (II) obtains the 152kg of solid material containing magnesium, the 0.5m of liquid material containing lithium³, its solution composition such as table 1-2 institutes Show.

Table 1-2 liquid materials containing lithium form

Step (V) obtains concentrating salting liquid 0.3m after being concentrated by evaporation³, it is formed as shown in table 1-3, after magnesium sinking reaction To magnesium hydrate precipitate 41kg, salting liquid 0.5m³, it is formed as shown in table 1-4, and obtaining lithium carbonate product after sinker reaction is 20.35kg, carbonic acid lithium content is 97.50wt% in the product, and it is formed as shown in tables 1 to 5, then the yield of lithium is 93.8%.

Salting liquid forms after table 1-3 is concentrated by evaporation

Salting liquid forms after the reaction of table 1-4 magnesium sinkings

Table 1-5 lithium carbonate products form

The 193kg of solid containing magnesium is obtained in step (IV) twice, and magnesium oxide product 133kg is obtained after calcining, oxygen in the product Change content of magnesium is 99.33wt%, and it is formed as shown in table 1-6, then the yield of magnesium reaches 99.1%.

Table 1-6 magnesium oxide products form

Embodiment 4：

The collaboration extracting method of magnesium and lithium in a kind of salt lake bittern is present embodiments provided, methods described uses embodiment 2 In system carry out, processing method comprises the following steps：

(I) it is 1.5m by inlet amount³/ h, temperature are 40 DEG C, content of magnesium 120g/L, lithium content 6g/L, and sodium content is 2g/L, chlorinity for 400g/L salt lake bittern and pressure is 0.5Mpa, temperature provides for 40 DEG C of compressed air in natural gas It is calcined under heat condition into spray roasting tower 2, wherein compressed air and salt lake bittern volume ratio are 100:1, spraying roasting It is 700 DEG C to burn the bottom temp of tower 2, and head temperature is 450 DEG C, and material is 4s in dwell time in the tower, and the top of spray roasting tower 2 goes out Mouthful temperature of charge is 380 DEG C, sequentially enters cyclone separator 3 and sack cleaner 4 carries out dust removal process, obtain solid material and Flue gas, it is 280 DEG C into flue-gas temperature during sack cleaner 4, flue-gas temperature is 250 DEG C when leaving sack cleaner 4；

(II) solid material that step (I) obtains is subjected to slurrying, countercurrent washing and is separated by filtration processing, operation temperature is 70 DEG C, obtain liquid material containing lithium and solid material containing magnesium；

(III) flue gas for obtaining step (I) carries out heat exchange in heat exchanger 5 with air, into heat exchanger 5 Air temperature is 30 DEG C, and air themperature is 190 DEG C when leaving, and flue-gas temperature is 140 DEG C, and the flue gas after leaving, which enters to neutralize, to be inhaled Tower 7 is received, is contacted with the milk of lime that the mass concentration from calcification stock tank 6 is 8% and carries out neutralization absorption, generation calcium chloride is molten Liquid, tail gas qualified discharge, resulting solution enter mist projection granulating tower 8, and carrying out spraying as thermal source to leave the air of heat exchanger 5 makes Grain, obtains calcium chloride product；

(IV) solid material containing magnesium for obtaining step (II) through two-stage slurrying, countercurrent washing and is separated by filtration processing again, Operation temperature is 70 DEG C, obtains magnesium hydroxide solid, gained magnesium hydroxide solid is calcined into 1h under the conditions of 650 DEG C, obtains oxygen Change magnesium products；

(V) liquid material containing lithium that step (II) obtains is evaporated concentration in evaporator 16, with 140 DEG C of steaming Vapour is thermal source, and condensate outlet temperature is 80 DEG C, and the solution after concentration carries out magnesium sinking reaction, reaction by precipitating reagent of sodium hydroxide Temperature is 70 DEG C, reaction time 25min, is separated by filtration under the conditions of 70 DEG C, obtained magnesium hydroxide return to step (IV) is entered Row processing, obtained solution are again that precipitating reagent carries out sinker reaction using sodium carbonate, and reaction temperature is 70 DEG C, and the reaction time is 35min, it is separated by filtration under the conditions of 70 DEG C, obtains lithium carbonate product and sodium chloride solution.

To handle 1m³Salt lake bittern is foundation, and step (I) the spray roasting magnesium chloride resolution ratio is 85%, and gained is solid Body material is 282kg, is formed as shown in table 2-1.

Solid material forms after table 2-1 spray roastings

Hydrogen chloride in tail gas concentration obtained by step (III) is 4ppm, and it is 465kg to obtain calcium chloride product, and calcium chloride content is 99.3wt%.

Step (II) obtains the 245kg of solid material containing magnesium, the 0.65m of liquid material containing lithium³, its solution composition such as table 2-2 institutes Show.

Table 2-2 liquid materials containing lithium form

Step (V) obtains concentrating salting liquid 0.35m after being concentrated by evaporation³, it is formed as shown in table 2-3, after magnesium sinking reaction To magnesium hydrate precipitate 42.8kg, salting liquid 0.5m³, it is formed as shown in Table 2-4, and obtaining lithium carbonate product after sinker reaction is 31.3kg, carbonic acid lithium content is 97.80wt% in the product, and it is formed as shown in table 2-5, then the yield of lithium is 96.5%.

Salting liquid forms after table 2-3 is concentrated by evaporation

Salting liquid forms after the reaction of table 2-4 magnesium sinkings

Table 2-5 lithium carbonate products form

The 287.8kg of solid containing magnesium is obtained in step (IV) twice, and magnesium oxide product 198kg is obtained after calcining, in the product Content of magnesia is 99.52wt%, and it is formed as shown in table 2-6, then the yield of magnesium reaches 98.5%.

Table 2-6 magnesium oxide products form

Embodiment 5：

The collaboration extracting method of magnesium and lithium in a kind of salt lake bittern is present embodiments provided, methods described uses embodiment 1 In system carry out, processing method comprises the following steps：

(I) it is 2m by inlet amount³/ h, temperature are 50 DEG C, content of magnesium 150g/L, lithium content 8g/L, sodium content 2g/ L, chlorinity for 500g/L salt lake bittern and pressure is 0.6Mpa, temperature provides heat for 50 DEG C of compressed air in natural gas Under the conditions of be calcined into spray roasting tower 2, wherein compressed air and salt lake bittern volume ratio are 90:1, spray roasting tower 2 Bottom temp is 800 DEG C, and head temperature is 550 DEG C, and material is 6s in dwell time in the tower, the top exit thing of spray roasting tower 2 Material temperature degree is 450 DEG C, sequentially enters cyclone separator 3 and sack cleaner 4 carries out dust removal process, obtain solid material and cigarette Gas, it is 320 DEG C into flue-gas temperature during sack cleaner 4, flue-gas temperature is 280 DEG C when leaving sack cleaner 4；

(II) solid material that step (I) obtains is subjected to slurrying, countercurrent washing and is separated by filtration processing, operation temperature is 90 DEG C, obtain liquid material containing lithium and solid material containing magnesium；

(III) flue gas for obtaining step (I) carries out heat exchange in heat exchanger 5 with air, into heat exchanger 5 Air temperature is 30 DEG C, and air themperature is 230 DEG C when leaving, and flue-gas temperature is 180 DEG C, and the flue gas after leaving, which enters to neutralize, to be inhaled Tower 7 is received, is contacted with the milk of lime that the mass concentration from calcification stock tank 6 is 10% and carries out neutralization absorption, generation calcium chloride is molten Liquid, tail gas qualified discharge, resulting solution enter mist projection granulating tower 8, and carrying out spraying as thermal source to leave the air of heat exchanger 5 makes Grain, obtains calcium chloride product；

(IV) solid material containing magnesium for obtaining step (II) through two-stage slurrying, countercurrent washing and is separated by filtration processing again, Operation temperature is 90 DEG C, obtains magnesium hydroxide solid, gained magnesium hydroxide solid is calcined into 0.5h under the conditions of 800 DEG C, obtained Magnesium oxide product；

(V) liquid material containing lithium that step (II) obtains is evaporated concentration in evaporator 16, with 160 DEG C of steaming Vapour is thermal source, and condensate outlet temperature is 90 DEG C, and the solution after concentration carries out magnesium sinking reaction, reaction by precipitating reagent of sodium hydroxide Temperature is 90 DEG C, reaction time 10min, is separated by filtration under the conditions of 90 DEG C, obtained magnesium hydroxide return to step (IV) is entered Row processing, obtained solution are again that precipitating reagent carries out sinker reaction using sodium carbonate, and reaction temperature is 90 DEG C, and the reaction time is 20min, it is separated by filtration under the conditions of 90 DEG C, obtains lithium carbonate product and sodium chloride solution.

To handle 1m³Salt lake bittern is foundation, and step (I) the spray roasting magnesium chloride resolution ratio is 90%, and gained is solid Body material is 336kg, is formed as shown in table 3-1.

Solid material forms after table 3-1 spray roastings

Hydrogen chloride in tail gas concentration obtained by step (III) is 4.2ppm, and it is 620kg to obtain calcium chloride product, calcium chloride content For 99.2wt%.

Step (II) obtains the 324kg of solid material containing magnesium, the 0.6m of liquid material containing lithium³, its solution composition such as table 3-2 institutes Show.

Table 3-2 liquid materials containing lithium form

Step (V) obtains concentrating salting liquid 0.3m after being concentrated by evaporation³, it is formed as shown in table 3-3, after magnesium sinking reaction To magnesium hydrate precipitate 35.6kg, salting liquid 0.45m³, it is formed as shown in table 3-4, and lithium carbonate product is obtained after sinker reaction For 42.0kg, carbonic acid lithium content is 97.92wt% in the product, and it is formed as shown in Table 3-5, then the yield of lithium is 97.3%.

Salting liquid forms after table 3-3 is concentrated by evaporation

Salting liquid forms after the reaction of table 3-4 magnesium sinkings

Table 3-5 lithium carbonate products form

The 359.6kg of solid containing magnesium is obtained in step (IV) twice, and magnesium oxide product 248kg is obtained after calcining, in the product Content of magnesia is 99.60wt%, and it is formed as shown in Table 3-6, then the yield of magnesium reaches 98.8%.

Table 3-6 magnesium oxide products form

Comparative example 1：

This comparative example provides the collaboration extraction system and its processing method of magnesium and lithium in a kind of salt lake bittern, the system Device and its connection with reference to embodiment 1, differ only in：The solid outlet of 3rd plate and frame filter press 18 is not changed with first The top entry of plasm scouring device 11 is connected.

Its processing method is carried out with reference to the method in embodiment 3, and now, obtaining magnesium hydrate precipitate after magnesium sinking reaction can not Return in the first slurrying wash mill 11, then carry the magnesium hydroxide solid that magnesium unit obtains and there was only 152kg, now the yield of magnesium Only 78.0%.

Summary embodiment and comparative example can be seen that collaboration extraction system comprehensive utilization wet method of the present invention and fire Method purification technique, by the collocation and connection between each device, integrating and coupling for different process technology, efficiently realize salt The extraction of valuable element in lake bittern water, the yield of lithium reach more than 93%, and the high income of magnesium is up to more than 98%；The present invention fills simultaneously Divide and utilize fume afterheat, realize heat cascade utilization, produced in extraction process without waste water and waste residue, tail gas qualified discharge, cleaning Environmental protection, application prospect are extensive.

Applicant states that the present invention illustrates the detailed system device and process flow of the present invention by above-described embodiment, But the invention is not limited in above-mentioned detailed device and flow, that is, does not mean that the present invention has to rely on above-mentioned detailed device and stream Cheng Caineng is implemented.Person of ordinary skill in the field is it will be clearly understood that any improvement in the present invention, to present system device With the equivalence replacement and servicing unit of process, the addition of composition, the selection of concrete mode etc., the protection of the present invention is all fallen within Within the scope of scope and disclosure.

Claims

1. the collaboration extraction system of magnesium and lithium in a kind of salt lake bittern, it is characterised in that the collaboration extraction system mainly includes Spray roasting system, dust pelletizing system, slurrying wash mill (9), equipment for separating liquid from solid (10), carry magnesium unit, carry lithium unit and cigarette Gas processing system；Wherein, the material outlet of the spray roasting system is connected with the material inlet of the dust pelletizing system, described to remove The exhanst gas outlet of dirt system is connected with the gas access of the smoke processing system, the solid matter outlet of the dust pelletizing system according to It is secondary to be connected with the slurrying wash mill (9) and equipment for separating liquid from solid (10), the solid material of the equipment for separating liquid from solid (10) Outlet is connected with the material inlet for carrying magnesium unit, and the liquid outlet of the equipment for separating liquid from solid (10) carries lithium unit with described Material inlet be connected, the product for carrying magnesium unit includes magnesia, and the product for carrying lithium unit sinks including magnesium hydroxide Form sediment and lithium carbonate, the magnesium hydrate precipitate enter described in carry magnesium unit and carry out carrying magnesium.

2. collaboration extraction system according to claim 1, it is characterised in that the spray roasting system includes air compressor machine (1) it is connected with spray roasting tower (2), the gas vent of the air compressor machine (1) with the bottom gas inlet of spray roasting tower (2)；

Preferably, the dust pelletizing system includes cyclone separator (3) and sack cleaner (4), the cigarette of the cyclone separator (3) Gas outlet is connected with the entrance of sack cleaner (4)；

Preferably, the first slurrying wash mill (11), first equipment for separating liquid from solid for carrying magnesium unit and including being sequentially connected (12), the second slurrying wash mill (13), the second equipment for separating liquid from solid (14) and calcining furnace (15), the first separation of solid and liquid dress The liquid outlet for putting (12) obtains sodium chloride solution, and the liquid outlet of second equipment for separating liquid from solid (14) is washed with the first slurrying The top entry for washing device (11) is connected, the solid outlet of second equipment for separating liquid from solid (14) and the entrance of calcining furnace (15) It is connected；

Preferably, the evaporator (16), the first settler (17), the 3rd separation of solid and liquid for carrying lithium unit and including being sequentially connected Device (18), the second settler (19) and the 4th equipment for separating liquid from solid (20), evaporator (16) condensate outlet and The top entry of two slurrying wash mills (13) is connected, the solid outlet and the first slurrying of the 3rd equipment for separating liquid from solid (18) The top entry of wash mill (11) is connected, and conveyer (21) is also associated with after the 4th equipment for separating liquid from solid (20), described The liquid outlet of 4th equipment for separating liquid from solid (20) obtains sodium chloride solution；

Preferably, before the bottom inlet of the spray roasting tower (2), slurrying wash mill (9) and equipment for separating liquid from solid (10) it Between, between the first slurrying wash mill (11) and the first equipment for separating liquid from solid (12), the second slurrying wash mill (13) and second Between equipment for separating liquid from solid (14), between the first settler (17) and the 3rd equipment for separating liquid from solid (18) and the second settler (19) it is equipped with pump between the 4th equipment for separating liquid from solid (20).

3. collaboration extraction system according to claim 1 or 2, it is characterised in that the air compressor machine (1) is screw-compression Machine or piston compressor；

Preferably, the cyclone separator (3) includes single tube cyclone dust collectors and/or multi-tube dust cleaner；

Preferably, the equipment for separating liquid from solid (10), the first equipment for separating liquid from solid (12), the second equipment for separating liquid from solid (14), Three equipment for separating liquid from solid (18) and the 4th equipment for separating liquid from solid (20) are filter or centrifugal device, preferably plate compression Machine；

Preferably, the evaporator (16) is triple effect falling film evaporator；

Preferably, the pump is any one in centrifugal pump, reciprocating pump, rotary pump or peripheral pump or at least two combination.

4. according to the collaboration extraction system described in claim any one of 1-3, it is characterised in that the smoke processing system includes Neutralize absorption tower (7) and mist projection granulating tower (8), the liquid of the outlet at bottom and mist projection granulating tower (8) for neutralizing absorption tower (7) Entrance is connected, and the outlet of the mist projection granulating tower (8) obtains calcium chloride product；

Preferably, the smoke processing system also includes heat exchanger (5) and calcification sizing device (6), the heat exchanger (5) Thermal fluid inlet be connected with the exhanst gas outlet of the sack cleaner (4), the hot fluid outlet ports of the heat exchanger (5) and institute The bottom gas inlet for stating neutralization absorption tower (7) is connected, and the outlet of the calcification sizing device (6) is with neutralizing absorption tower (7) Bottom slurry import is connected；

Preferably, described neutralize is provided with circulating pump between absorption tower (7) and mist projection granulating tower (8), the entrance of the circulating pump and The outlet at bottom for neutralizing absorption tower (7) is connected, the outlet of the circulating pump and the top entry and the spray that neutralize absorption tower (7) The liquid inlet of mist granulation tower (8) is connected.

5. collaboration extraction system according to claim 4, it is characterised in that the heat exchanger (5) exchanges heat for shell and tube Device；

Preferably, described neutralize absorption tower (7) are three-level circulating absorption tower；

6. the processing method of the collaboration extraction system according to claim any one of 1-5, it is characterised in that methods described bag Include following steps：

(b) liquid material containing lithium is obtained after the solid material that step (a) obtains being carried out into slurrying washing and separation of solid and liquid and containing magnesium Solid material；

(c) solid material containing magnesium that step (b) obtains is obtained into magnesium hydroxide solid after multipolarity plasm scouring and separation of solid and liquid, Again magnesia is obtained through calcining；

(d) liquid material containing lithium for obtaining step (b) obtains through being concentrated by evaporation, after multi stage precipitation reaction and separation of solid and liquid successively Magnesium hydroxide and lithium carbonate, obtained magnesium hydroxide return to step (c) is handled.

7. according to the method for claim 6, it is characterised in that step (a) salt lake bittern refers to by extracting potassium, sodium With based on magnesium chloride, the solution containing lithium chloride and sodium chloride, wherein content of magnesium are 80-150g/L after bromine, chlorinity is 260-500g/L, lithium content 4-8g/L, sodium content 1-2g/L；

Preferably, step (a) the salt lake bittern feeding temperature is 30-50 DEG C；

Preferably, step (a) spray roasting is needed to be passed through compressed air, and the compressed air is provided by air compressor machine (1)；

Preferably, the compressed air pressure is 0.4-0.6MPa, and intake air temperature is 30-50 DEG C；

Preferably, the compressed air and salt lake bittern volume ratio are (90-120):1；

Preferably, step (a) spray roasting is carried out in the case where fuel provides heat condition；

Preferably, the fuel is any one in methanol, diesel oil, liquefied gas or natural gas；

Preferably, step (a) spray roasting is carried out in spray roasting tower (2)；

Preferably, spray roasting tower (2) bottom temp is 600-800 DEG C, and head temperature is 350-550 DEG C；

Preferably, the interior residence time of material of the spray roasting tower (2) is 2-6s, preferably 3-5s；

Preferably, spray roasting tower (2) outlet mass temperatures are 300-500 DEG C；

Preferably, step (a) dust removal process is carried out in cyclone separator (3) and sack cleaner (4) respectively；

Preferably, sack cleaner (4) input gas temperature is 220-320 DEG C, preferably 250-300 DEG C；

Preferably, sack cleaner (4) exit gas temperature is 200-300 DEG C, preferably 220-280 DEG C；

Preferably, step (b) and step (c) washing are countercurrent washing；

Preferably, step (b) and step (c) separation of solid and liquid are to be separated by filtration；

Preferably, step (b) and step (c) the slurrying washing and separation of solid and liquid operation temperature are 50-90 DEG C, preferably 60- 80℃；

Preferably, step (c) the multipolarity plasm scouring and separation of solid and liquid are the washing of two-stage slurrying and separation of solid and liquid；

Preferably, step (c) calcining is carried out in calcining furnace (15)；

Preferably, step (c) calcining heat is 400-800 DEG C, preferably 550-750 DEG C, more preferably 600-700 ℃；

Preferably, step (c) calcination time is 0.5-2h, preferably 0.8-1.2h；

Preferably, content of magnesia is more than 98wt% in step (c) magnesium oxide product；

Preferably, described be concentrated by evaporation of step (d) is carried out in evaporator (16)；

Preferably, step (d) evaporation and concentration is using steam as thermal source；

Preferably, 120-160 DEG C of the inlet steam temperature, preferably 130-150 DEG C；

Preferably, the steam condensate outlet temperature is 60-90 DEG C, preferably 70-80 DEG C；

Preferably, step (d) the multi stage precipitation reaction and separation of solid and liquid are respectively one-level precipitation reaction and separation of solid and liquid and two Level precipitation reaction and separation of solid and liquid；

Preferably, the one-level precipitation reaction is reacted for magnesium sinking, using sodium hydroxide as precipitating reagent；

Preferably, the one-level precipitation reaction temperature is 50-90 DEG C, preferably 60-80 DEG C；

Preferably, the one-level precipitation reaction time is 10-40min；

Preferably, the two-stage precipitation reaction is reacted for sinker, using sodium carbonate as precipitating reagent；

Preferably, the two-stage precipitation reaction temperature is 50-90 DEG C, preferably 60-80 DEG C；

Preferably, the precipitation reaction time described in the two level is 20-50min；

Preferably, for step (d) separation of solid and liquid to be separated by filtration, operation temperature is 50-90 DEG C, preferably 60-80 DEG C.

8. the method according to claim 6 or 7, it is characterised in that the flue gas for obtaining step (a) is handled, at it Reason method comprises the following steps：

(A) flue gas for obtaining step (a) carries out neutralization absorption after heat exchange, obtains calcium chloride solution, tail gas qualified discharge；

9. according to the method for claim 8, it is characterised in that step (A) described heat exchange is using air as low-temperature receiver；

Preferably, air themperature is 150-230 DEG C, preferably 170-210 DEG C after step (A) described heat exchange；

Preferably, flue-gas temperature is 120-180 DEG C, preferably 130-150 DEG C after step (A) described heat exchange；

Preferably, described neutralize of step (A) absorbs in and carried out in absorption tower (7)；

Preferably, described neutralize of step (A) is absorbed using milk of lime as nertralizer, and its mass concentration is 5%-10%；

Preferably, the milk of lime is handled to obtain by lime and water through slurrying；

Preferably, the slurrying processing is carried out in calcification stock tank (6)；

Preferably, step (A) the hydrogen chloride in tail gas content is not more than 10ppm, preferably not greater than 5ppm；

Preferably, step (B) mist projection granulating is carried out in mist projection granulating tower (8)；

10. according to the method described in claim any one of 6-9, it is characterised in that the described method comprises the following steps：

(I) salt lake bittern that temperature is 30-50 DEG C and the compressed air that pressure is 0.4-0.6Mpa, temperature is 30-50 DEG C are existed Fuel provides to be calcined under heat condition into spray roasting tower (2), and wherein compressed air is with salt lake bittern volume ratio (90-120):1, spray roasting tower (2) bottom temp is 600-800 DEG C, and head temperature is 350-550 DEG C, and material stops in tower It is 3-5s to stay the time, and spray roasting tower (2) top exit temperature of charge is 300-500 DEG C, sequentially enter cyclone separator (3) and Sack cleaner (4) carries out dust removal process, obtains solid material and flue gas, is into flue-gas temperature when sack cleaner (4) 250-300 DEG C, flue-gas temperature is 220-280 DEG C when leaving sack cleaner (4)；

(II) solid material that step (I) obtains is subjected to slurrying, countercurrent washing and is separated by filtration processing, operation temperature 60- 80 DEG C, obtain liquid material containing lithium and solid material containing magnesium；

(III) flue gas that step (I) obtains is subjected to heat exchange in heat exchanger (5) with air, when leaving heat exchanger (5) Air themperature is 170-210 DEG C, and flue-gas temperature is 130-150 DEG C, and flue gas after leaving, which enters, neutralizes absorption tower (7), with from The milk of lime contact that the mass concentration of calcification stock tank (6) is 5-10% carries out neutralization absorption, empties hydrogen chloride in tail gas concentration Not higher than 5ppm, resulting solution enters mist projection granulating tower (8), and carrying out spraying as thermal source to leave the air of heat exchanger (5) makes Grain, obtains calcium chloride product；

(IV) solid material containing magnesium for obtaining step (II) through two-stage slurrying, countercurrent washing and is separated by filtration processing again, operation Temperature is 60-80 DEG C, obtains magnesium hydroxide solid, gained magnesium hydroxide solid is calcined into 0.8- under the conditions of 600-700 DEG C 1.2h, obtain the high-purity magnesium oxide that content of magnesia is more than 98%；

(V) liquid material containing lithium that step (II) obtains is evaporated concentration in evaporator (16), with 130-150 DEG C Steam is thermal source, and the solution after concentration carries out magnesium sinking reaction by precipitating reagent of sodium hydroxide, and reaction temperature is 60-80 DEG C, reaction Time is 10-40min, is separated by filtration under the conditions of 60-80 DEG C, and obtained magnesium hydroxide return to step (IV) is handled, and is obtained The solution arrived carries out sinker reaction by precipitating reagent of sodium carbonate again, and reaction temperature is 60-80 DEG C, reaction time 20-50min, It is separated by filtration under the conditions of 60-80 DEG C, obtains lithium carbonate product and sodium chloride solution.