CN110777271A - Method for adsorbing gallium from fly ash alkaline process aluminum extraction mother liquor by simulated moving bed - Google Patents
Method for adsorbing gallium from fly ash alkaline process aluminum extraction mother liquor by simulated moving bed Download PDFInfo
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- 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
- C22B58/00—Obtaining gallium or indium
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- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
- C22B3/24—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition by adsorption on solid substances, e.g. by extraction with solid resins
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- C—CHEMISTRY; METALLURGY
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- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/005—Separation by a physical processing technique only, e.g. by mechanical breaking
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- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
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Abstract
The invention discloses a method for adsorbing gallium from fly ash alkaline process aluminum extraction mother liquor by using a simulated moving bed adsorption column, which takes seed precipitation mother liquor circularly enriched with gallium in the high-alumina fly ash alkaline process aluminum extraction process as raw liquor, and realizes selective adsorption and extraction of gallium ions in the seed precipitation mother liquor through continuous adsorption of gallium extraction resin of a continuous fixed bed; when the initial adsorption column reaches balance, the elution mixed liquor can be adopted in a split mode to carry out elution independently, washing is carried out after elution is finished, an activating agent is adopted for regeneration and activation, cyclic absorption and desorption can be further carried out after activation, and continuous and stable resin adsorption, elution and regeneration processes are realized by switching valves of different material inlet and outlet. The method disclosed by the invention has the advantages of simple process, low energy consumption, high gallium enrichment efficiency and capability of realizing the whole flow of continuous adsorption-desorption-regeneration, effectively solves the difficult problem of high-efficiency selective recycling of gallium metal, has outstanding environmental and economic benefits and has wide industrial popularization prospect.
Description
Technical Field
The invention relates to a selective extraction and separation technology of low-concentration valuable metal elements in solid waste, in particular to a method for adsorbing gallium from fly ash alkaline process aluminum extraction mother liquor by using a simulated moving bed adsorption column.
Background
Gallium is a rare metal, widely used in photovoltaic and integrated circuits, light emitting diodes and thin-film solar cells, and as the consumption scale of gallium products is continuously enlarged, the demand of gallium will further increase, and the european union committee has listed gallium as one of the important mineral raw materials in short supply. Gallium is not concentrated in the natural world, has the characteristics of less single finished ore, easy symbiosis with aluminum and the like, and is usually associated with bauxite and sphalerite. At present, the industrial gallium product mainly comes from aluminum extraction mother liquor in the production process of aluminum oxide, and a small amount of gallium product comes from zinc smelting waste residue.
The gallium content in the fly ash is low, and the direct extraction economic value is not high, so that the synergic extraction research is mainly carried out by relying on the fly ash aluminum extraction process. The process engineering research institute of Chinese academy of sciences provides a novel process for synergistic utilization of aluminum, lithium, gallium and silicon by a fly ash pre-desilication-Bayer sub-molten salt combination method based on a sub-molten salt platform technology, desilication fly ash is subjected to two-step hydrothermal reaction, further crystallization and seed separation are carried out to obtain alumina, and a crystallization mother liquor is subjected to adsorption separation to obtain metal gallium. The gallium content in the high-alumina fly ash is low, the direct extraction is economic, the environmental benefit is poor, the synergistic extraction method is adopted, the synergistic utilization of various resources of the high-alumina fly ash can be realized, and the method is an important direction for the resource utilization of the fly ash in the future.
At present, the key point of the separation in the process of extracting gallium from fly ash is the separation of gallium and aluminum, and a precipitation method, an extraction method and an adsorption method are commonly used. Patent publication No. CN106986361B discloses a method for separating aluminum and gallium in the process of extracting alumina from fly ash by acid method, N-dimethyl dithiocarbamate [ (CH)
3)
2NCSSM·2H
2O ] according to Fe
3+：M
+The molar ratio is 1: 0.5-6, gradually adding the mixture into an acid aqueous solution of aluminum salt, controlling the reaction temperature to be 5-40 ℃, reacting to generate black precipitate, and performing solid-liquid separation to obtain an aluminum-containing solution and a gallium-containing precipitate slag, wherein the extraction rate of gallium can reach about 93.24% at most, and the loss rate of aluminum is very low and is below 1%. The patent publication No. CN107758714A discloses a method for synergistically extracting aluminum, silicon, lithium and gallium in fly ash by a combined method, and the publication No. CN103382531B discloses a method for enriching gallium in aluminum oxide mother liquor produced by using high-alumina fly ash, wherein the aluminum extraction mother liquor in the combined method process and the seed precipitation mother liquor with lower gallium concentration in the process of producing aluminum oxide by using high-alumina fly ash are respectively adopted as raw materials, the ion exchange and process strengthening technology is adopted, gallium enriched liquor is obtained after adsorption and elution, and metal gallium can be obtained after further treatment and electrolysis. The adsorption method has high enrichment efficiency on low-concentration gallium solution, simple production process, rich raw material sources and obvious economic and environmental benefits.
Because the concentration of gallium in the aluminum extraction mother liquor is low, the adsorption time in the adsorption process is long, and the structural efficiency of a pure adsorption tower is low, the resin adsorption method is an effective method for realizing selective enrichment and separation of low-concentration gallium, and the method needs to be developed in a targeted manner, is quick and efficient, and needs to be developed for a continuous and efficient selective adsorption device for gallium.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a method for adsorbing gallium from a fly ash alkaline process aluminum extraction mother liquor by using a simulated moving bed adsorption column, which has mild process conditions, can continuously adsorb, leach and regenerate and activate, greatly reduces energy consumption and production cost, and has better industrial application prospect.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for adsorbing gallium from fly ash alkaline process aluminum extraction mother liquor by a simulated moving bed comprises the following steps:
(1) adsorption: conveying the gallium-containing seed separation mother liquor to a feed inlet of an adsorption column of a simulated moving bed by a pump, continuously adsorbing by using chelate resin, and respectively obtaining saturated adsorption resin according to different adsorption columns;
(2) leaching: after the adsorption in the step (1) is carried out for a certain time, the adsorption column is saturated, the inlet valve and the outlet valve are switched, and the saturated adsorption resin obtained in the step (1) is leached by adopting leacheate to obtain leacheate and leached resin;
(3) regeneration and activation: washing the leached resin obtained in the step (2) after leaching is finished by adopting a washing solution respectively, and then carrying out continuous regeneration activation by adopting a regeneration activation solution to obtain activated resin;
(4) circulating adsorption: and (3) the activated resin in the step (3) is subjected to adsorption, leaching in the step (2) and regeneration and activation in the step (3) again in sequence, so that the continuous adsorption-leaching-regeneration and activation-adsorption circulation process of the simulated moving bed adsorption column is realized.
Preferably, the adsorption column of the simulated moving bed in the step (1) is an adsorption column combination which can realize mutual switching between series connection and parallel connection;
preferably, the number of the adsorption columns in the step (1) is 2-10, such as 2, 3, 4, 5, 6, 7, 8, 9 or 10;
preferably, the chelating resin in the step (1) is an adsorption resin containing amidoxime group chelating adsorption functional diagram and an organic framework;
preferably, the flow rate of the seed separation mother liquor in the step (1) is 1-10BV/h, such as 1BV/h, 2BV/h, 3BV/h, 4BV/h, 5BV/h, 6BV/h, 7BV/h, 8BV/h, 9BV/h, 10BV/h and the like;
preferably, the temperature of the adsorption reaction of the seed precipitation solution in the step (1) is 20-80 ℃, for example, 20 ℃, 25 ℃, 30 ℃, 35 ℃, 40 ℃, 45 ℃, 50 ℃, 55 ℃, 60 ℃, 65 ℃, 70 ℃, 75 ℃, 80 ℃ and the like;
preferably, the leacheate in the leaching process in the step (2) is a mixed solution of sodium hydroxide and sodium sulfide;
preferably, the concentration of sodium hydroxide in the leacheate obtained in the leaching process in the step (2) is 0.5-3mol/L, such as 0.5 mol/L, 1.0 mol/L, 1.5 mol/L, 2.0 mol/L, 2.5 mol/L, 3.0 mol/L and the like;
preferably, the concentration of sodium sulfide in the leacheate obtained in the leaching process in the step (2) is 0.5-3mol/L, such as 0.5 mol/L, 1.0 mol/L, 1.5 mol/L, 2.0 mol/L, 2.5 mol/L, 3.0 mol/L and the like;
preferably, the temperature of the leaching process in the step (2) is 20-60 ℃;
preferably, the flow rate of the leaching solution in the leaching process in the step (2) is 1-4BV/h, for example, 1BV/h, 1.5BV/h, 2BV/h, 2.5BV/h, 3BV/h, 3.5BV/h, 4BV/h, etc.
Preferably, the washing solution in the step (3) is water or a sodium hydroxide solution with a mass concentration of 1-10%, and may be, for example, water, a 1% sodium hydroxide solution, a 2% sodium hydroxide solution, a 3% sodium hydroxide solution, a 4% sodium hydroxide solution, a 5% sodium hydroxide solution, a 6% sodium hydroxide solution, a 7% sodium hydroxide solution, an 8% sodium hydroxide solution, a 9% sodium hydroxide solution, a 10% sodium hydroxide solution, or the like;
preferably, the temperature of the washing process in the step (3) is 20-60 deg.C, such as 20 deg.C, 25 deg.C, 30 deg.C, 35 deg.C, 40 deg.C, 45 deg.C, 50 deg.C, 55 deg.C, 60 deg.C, etc.;
preferably, the flow rate of the washing liquid in the washing process in the step (3) is 1-3BV/h, for example, 1BV/h, 1.5BV/h, 2BV/h, 2.5BV/h, 3BV/h, etc.
Preferably, the washing liquid used in the washing process in the step (3) is 0.5 to 3 times of the volume of the adsorption column packed resin, for example, 0.5 times, 1 time, 1.5 times, 2 times, 2.5 times, 3 times, etc.;
preferably, the activating solution in the activating process in the step (3) is a sodium hydroxide solution with a mass fraction of 5-25%, for example, the mass fraction can be 5%, 10%, 15%, 20%, 25%, etc.;
preferably, the temperature of the activation process in the step (3) is 25-60 deg.C, such as 20 deg.C, 25 deg.C, 30 deg.C, 35 deg.C, 40 deg.C, 45 deg.C, 50 deg.C, 55 deg.C, 60 deg.C, etc.;
preferably, the flow rate of the activating solution in step (3) is 0.5-3BV/h, such as 0.5BV/h, 1BV/h, 1.5BV/h, 2BV/h, 2.5BV/h, 3BV/h, etc.
Preferably, the volume of the activating solution in the step (3) is 0.5 to 3 times of the volume of the resin bed layer, for example, 0.5 times, 1 time, 1.5 times, 2 times, 2.5 times, 3 times, etc.
Preferably, in the cyclic adsorption process in the step (4), the whole cyclic process of adsorption-leaching-regeneration activation-adsorption is realized by changing valves at the front and the rear of the adsorption column.
Compared with the prior art, the invention has the advantages that:
the method effectively realizes the recycling of gallium in the seed precipitation mother liquor generated in the process of extracting alumina from fly ash, has mild reaction conditions, simple process and low equipment requirement, adopts a simulated moving bed adsorption column to adsorb gallium ions, has high adsorption rate, can realize continuous adsorption-leaching-regeneration activation, and is easy to realize industrial production.
Drawings
FIG. 1 is a schematic process flow diagram of a method for adsorbing gallium from fly ash alkaline process aluminum extraction mother liquor by a simulated moving bed according to embodiment 1 of the invention;
description of the drawings: in the figure, 1 is a liquid inlet barrel for containing absorption, leaching, washing or regeneration liquid inlet, and 7, 8 and 9 are liquid outlet barrels for containing absorption, leaching, washing or regeneration liquid outlet. 4. 5 and 6 are adsorption columns which can be used in series or in parallel, and the adsorption, leaching and regeneration can be carried out simultaneously. 2, a constant temperature groove is used for the outer layer heat preservation of the adsorption column; and 3, a peristaltic pump.
Detailed Description
The technical scheme of the invention is further explained by the specific implementation mode in combination with the attached drawings.
The invention is described in detail below with reference to the figures and the embodiments. The following examples are only illustrative of the present invention, and the scope of the present invention shall include the full contents of the claims, and not be limited to the following examples. Table 1 shows the main ion contents of the aluminum-extracting mother liquor in examples 1 to 6. In the embodiment examples 1-6, the amidoxime group chelating adsorption functional diagram and the styrene-divinylbenzene organic framework adsorption resin are adopted to carry out the gallium adsorption, leaching, regeneration and activation integrated cycle.
Table 1 extracts the composition of the aluminum mother liquor.
| Composition (I) | Al 2O 3 | GaO 2 - | NaOH |
| Content g/L | 120 | 0.1 | 250 |
Example 1
The simulated moving bed adopts a series connection mode of 3 adsorption columns for adsorption, and adopts a parallel connection mode for leaching, regeneration and activation.
(1) Adsorption: the aluminum extraction mother liquor sequentially flows through 3 adsorption columns at the flow rate of 2.5BV/h, the temperature in the adsorption process is 50 ℃, and the resin adsorption is balanced after the concentration of gallium in the adsorption effluent liquid is unchanged;
(2) leaching: after the first adsorption column is saturated in adsorption, the switching valve switches the inlet pipe and the outlet pipe of the first adsorption column to the leaching passage, and a mixed solution of sodium sulfide and sodium hydroxide is used as a leaching solution to absorb the saturated adsorption resinIn which Na is attached
2The concentration of S is 2mol/L, the concentration of NaOH is 2mol/L, the flow rate of the leaching solution is 2BV/h, the leaching temperature is 25 ℃, and leaching is stopped when the outlet concentration is lower than 300 ppm;
(3) regeneration and activation: washing the washed resin with water at normal temperature, wherein the flow rate of the water is 1BV/h, the using amount of the water is 1 time of the mass of the filled resin, the washed resin is activated by using 8% of sodium hydroxide solution as an activating solution, the flow rate of the activating solution is 2BV/h, the using amount of the activating solution is 1 time of the volume of a resin bed layer, and the temperature of the activation process is 25 ℃;
the adsorption extraction rate of gallium can be realized to 63.8% in the simulated moving bed adsorption experimental process adopted in the embodiment.
Example 2
The simulated moving bed adopts a series connection mode of 6 adsorption columns for adsorption, and adopts a parallel connection mode for leaching, regeneration and activation.
(1) Adsorption: the aluminum extraction mother liquor flows through 6 adsorption columns in sequence at the flow rate of 2.5BV/h, the temperature in the adsorption process is 50 ℃, and the resin adsorption is balanced after the concentration of gallium in the adsorption effluent liquid is unchanged;
(2) leaching: after the first adsorption column is saturated in adsorption, switching the inlet pipe and the outlet pipe of the first adsorption column to the leaching passage by a switching valve, and adsorbing the saturated adsorption resin by using a mixed solution of sodium sulfide and sodium hydroxide as a leaching solution, wherein Na is contained in the saturated adsorption resin
2The concentration of S is 2mol/L, the concentration of NaOH is 2mol/L, the flow rate of the leaching solution is 2BV/h, the leaching temperature is 25 ℃, and leaching is stopped when the outlet concentration is lower than 300 ppm;
(3) regeneration and activation: washing the washed resin with water at normal temperature, wherein the flow rate of the water is 1BV/h, the using amount of the water is 1 time of the mass of the filled resin, the washed resin is activated by using 8% of sodium hydroxide solution as an activating solution, the flow rate of the activating solution is 2BV/h, the using amount of the activating solution is 1 time of the volume of a resin bed layer, and the temperature of the activation process is 25 ℃;
the adsorption extraction rate of gallium can be realized by the simulated moving bed adsorption experimental process adopted in the embodiment to be 80.6%.
Example 3
The simulated moving bed adopts a series connection mode of 10 adsorption columns for adsorption, and adopts a parallel connection mode for leaching, regeneration and activation.
(1) Adsorption: the aluminum extraction mother liquor sequentially flows through 10 adsorption columns at the flow rate of 2.5BV/h, the temperature in the adsorption process is 50 ℃, and the resin adsorption is balanced after the concentration of gallium in the adsorption effluent liquid is unchanged;
(2) leaching: after the first adsorption column is saturated in adsorption, switching the inlet pipe and the outlet pipe of the first adsorption column to the leaching passage by a switching valve, and adsorbing the saturated adsorption resin by using a mixed solution of sodium sulfide and sodium hydroxide as a leaching solution, wherein Na is contained in the saturated adsorption resin
2The concentration of S is 2mol/L, the concentration of NaOH is 2mol/L, the flow rate of the leaching solution is 2BV/h, the leaching temperature is 25 ℃, and leaching is stopped when the outlet concentration is lower than 300 ppm;
(3) regeneration and activation: washing the washed resin with water at normal temperature, wherein the flow rate of the water is 1BV/h, the using amount of the water is 1 time of the mass of the filled resin, the washed resin is activated by using 8% of sodium hydroxide solution as an activating solution, the flow rate of the activating solution is 2BV/h, the using amount of the activating solution is 1 time of the volume of a resin bed layer, and the temperature of the activation process is 25 ℃;
the simulated moving bed adsorption experimental process adopted in the embodiment can realize that the adsorption extraction rate of gallium is 95%. Example 4
The simulated moving bed adopts 3 regeneration adsorption columns in the example 1 to carry out adsorption in series, and adopts a parallel connection mode to carry out leaching and regeneration activation.
(1) Adsorption: the aluminum extraction mother liquor sequentially flows through 3 adsorption columns at the flow rate of 2.5BV/h, the temperature in the adsorption process is 50 ℃, and the resin adsorption is balanced after the concentration of gallium in the adsorption effluent liquid is unchanged;
(2) leaching: after the first adsorption column is saturated in adsorption, switching the inlet pipe and the outlet pipe of the first adsorption column to the leaching passage by a switching valve, and adsorbing the saturated adsorption resin by using a mixed solution of sodium sulfide and sodium hydroxide as a leaching solution, wherein Na is contained in the saturated adsorption resin
2The concentration of S is 2mol/L, the concentration of NaOH is 2mol/L, the flow rate of the leaching solution is 2BV/h, the leaching temperature is 25 ℃, and leaching is stopped when the outlet concentration is lower than 300 ppm;
(3) regeneration and activation: washing the washed resin with water at normal temperature, wherein the flow rate of the water is 1BV/h, the using amount of the water is 1 time of the mass of the filled resin, the washed resin is activated by using 8% of sodium hydroxide solution as an activating solution, the flow rate of the activating solution is 2BV/h, the using amount of the activating solution is 1 time of the volume of a resin bed layer, and the temperature of the activation process is 25 ℃;
the adsorption extraction rate of gallium can be realized by the simulated moving bed adsorption experimental process adopted in the embodiment to be 50%. Example 5
The simulated moving bed adopts the serial connection mode of 10 regeneration adsorption columns in the embodiment 3 to carry out adsorption, and adopts the parallel connection mode to carry out leaching and regeneration activation.
(1) Adsorption: the aluminum extraction mother liquor sequentially flows through 10 adsorption columns at the flow rate of 2.5BV/h, the temperature in the adsorption process is 50 ℃, and the resin adsorption is balanced after the concentration of gallium in the adsorption effluent liquid is unchanged;
(2) leaching: after the first adsorption column is saturated in adsorption, switching the inlet pipe and the outlet pipe of the first adsorption column to the leaching passage by a switching valve, and adsorbing the saturated adsorption resin by using a mixed solution of sodium sulfide and sodium hydroxide as a leaching solution, wherein Na is contained in the saturated adsorption resin
2The concentration of S is 2mol/L, the concentration of NaOH is 2mol/L, the flow rate of the leaching solution is 2BV/h, the leaching temperature is 25 ℃, and leaching is stopped when the outlet concentration is lower than 300 ppm;
(3) regeneration and activation: washing the washed resin with water at normal temperature, wherein the flow rate of the water is 1BV/h, the using amount of the water is 1 time of the mass of the filled resin, the washed resin is activated by using 8% of sodium hydroxide solution as an activating solution, the flow rate of the activating solution is 2BV/h, the using amount of the activating solution is 1 time of the volume of a resin bed layer, and the temperature of the activation process is 25 ℃;
the adsorption extraction rate of gallium can be realized by the simulated moving bed adsorption experimental process adopted in the embodiment to be 42%.
Example 6
The simulated moving bed adopts 1 adsorption column for adsorption, and uses leacheate for elution and then regeneration and activation.
(1) Adsorption: the aluminum extraction mother liquor sequentially flows through 1 adsorption column at the flow rate of 2.5BV/h, the temperature in the adsorption process is 50 ℃, and the resin adsorption is balanced after the concentration of gallium in the adsorption effluent liquid is unchanged;
(2) leaching: after the adsorption column is adsorbed to saturation, the saturated adsorption resin is adsorbed by using a mixed solution of sodium sulfide and sodium hydroxide as an eluent, wherein Na is contained in the saturated adsorption resin
2The concentration of S is 2mol/L, the concentration of NaOH is 2mol/L, the flow rate of the leaching solution is 2BV/h, the leaching temperature is 25 ℃, and leaching is stopped when the outlet concentration is lower than 300 ppm;
(3) regeneration and activation: washing the washed resin with water at normal temperature, wherein the flow rate of the water is 1BV/h, the using amount of the water is 1 time of the mass of the filled resin, the washed resin is activated by using 8% of sodium hydroxide solution as an activating solution, the flow rate of the activating solution is 2BV/h, the using amount of the activating solution is 1 time of the volume of a resin bed layer, and the temperature of the activation process is 25 ℃;
the simulated moving bed adsorption experimental process adopted in the embodiment can realize that the adsorption extraction rate of gallium is 33%.
Claims (5)
1. A method for adsorbing gallium from fly ash alkaline process aluminum extraction mother liquor by a simulated moving bed is characterized by comprising the following steps:
(1) adsorption: conveying the gallium-containing seed separation mother liquor to a feed inlet of an adsorption column of a simulated moving bed by a pump, continuously adsorbing by using chelate resin, and respectively obtaining saturated adsorption resin according to different adsorption columns;
(2) leaching: after the adsorption in the step (1) is carried out for a certain time, the adsorption column is saturated, the inlet valve and the outlet valve are switched, and the saturated adsorption resin obtained in the step (1) is leached by adopting leacheate to obtain leacheate and leached resin;
(3) regeneration and activation: washing the leached resin obtained in the step (2) after leaching is finished by adopting a washing solution respectively, and then carrying out continuous regeneration activation by adopting a regeneration activation solution to obtain activated resin;
(4) circulating adsorption: and (3) the activated resin in the step (3) is subjected to adsorption, leaching in the step (2) and regeneration and activation in the step (3) again in sequence, so that the continuous adsorption-leaching-regeneration and activation-adsorption circulation process of the simulated moving bed adsorption column is realized.
2. The method according to claim 1, characterized in that the simulated moving bed adsorption column in the step (1) adopts an adsorption column combination which can realize mutual switching between series connection and parallel connection;
preferably, the number of the adsorption columns in the step (1) is 2-10;
preferably, the chelating resin in the step (1) is an adsorption resin containing amidoxime group chelating adsorption functional diagram and an organic framework;
preferably, the flow rate of the seed precipitation mother liquor in the step (1) is 1-10 BV/h;
preferably, the adsorption reaction temperature of the seed precipitation mother liquor in the step (1) is 20-80 ℃.
3. The method according to claim 1 or 2, wherein the leacheate in the leaching process in the step (2) is prepared from a mixed solution of sodium hydroxide and sodium sulfide;
preferably, the concentration of sodium hydroxide in the leacheate obtained in the leaching process in the step (2) is 0.5-3 mol/L;
preferably, the concentration of sodium sulfide in the leacheate obtained in the leaching process in the step (2) is 0.5-3 mol/L;
preferably, the temperature of the leaching process in the step (2) is 20-60 ℃;
preferably, the flow rate of the leaching solution in the leaching process in the step (2) is 1-4 BV/h.
4. The method according to any one of claims 1 to 3, wherein the washing liquid in the step (3) is water or a sodium hydroxide solution with a mass concentration of 1 to 10%;
preferably, the temperature of the washing process in the step (3) is 20-60 ℃;
preferably, the flow rate of the washing liquid in the washing process in the step (3) is 1-3 BV/h;
preferably, the amount of the washing liquid in the washing process in the step (3) is 0.5-3 times of the volume of the resin filled in the adsorption column;
preferably, the activating solution in the activating process in the step (3) is a sodium hydroxide solution with the mass fraction of 5-25%;
preferably, the temperature of the activation process in the step (3) is 25-60 ℃;
preferably, the flow rate of the activating solution in the step (3) is 0.5-3 BV/h;
preferably, the volume of the activating solution in the step (3) is 0.5-3 times of the volume of the resin bed layer.
5. The method according to any one of claims 1 to 4, wherein the cyclic adsorption process in the step (4) realizes an adsorption-leaching-regeneration activation-adsorption integrated cyclic process by changing valves before and after the adsorption column.
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| CN114892025A (en) * | 2022-06-02 | 2022-08-12 | 北京万邦达环保技术股份有限公司 | Simulated moving bed lithium extraction adsorption process |
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| CN114892025A (en) * | 2022-06-02 | 2022-08-12 | 北京万邦达环保技术股份有限公司 | Simulated moving bed lithium extraction adsorption process |
| CN114892025B (en) * | 2022-06-02 | 2023-11-21 | 北京万邦达环保技术股份有限公司 | Simulated moving bed lithium extraction adsorption process |
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Application publication date: 20200211 |