CN111533143A - Industrial-grade anhydrous sodium sulfate preparation device and method - Google Patents
Industrial-grade anhydrous sodium sulfate preparation device and method Download PDFInfo
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- CN111533143A CN111533143A CN202010507954.7A CN202010507954A CN111533143A CN 111533143 A CN111533143 A CN 111533143A CN 202010507954 A CN202010507954 A CN 202010507954A CN 111533143 A CN111533143 A CN 111533143A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/004—Preparation in the form of granules, pieces or other shaped products
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/18—Dehydration
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Abstract
The invention discloses a device and a method for preparing industrial anhydrous sodium sulphate, which relate to the field of recovering sodium sulphate as the industrial anhydrous sodium sulphate by dilute brine. Wherein the membrane concentration system is used for concentrating light brine containing sodium sulfate and discharging concentrated solution containing supersaturated sodium sulfate; the continuous flow salting-out crystallization system is mainly used for crystallizing and separating out large-particle sodium sulfate crystals from sodium sulfate in supersaturated sodium sulfate concentrated solution discharged from the membrane concentration system through a salting-out method and accurately controlling the degree of supersaturation at normal temperature, meanwhile, the purity of anhydrous sodium sulphate is ensured by utilizing a reflux design, and a centrifuge and a dryer system are used for drying. The invention realizes the continuous preparation of the large-particle high-purity anhydrous sodium sulphate, and has small equipment investment and low energy consumption at normal temperature.
Description
Technical Field
The invention relates to the field of recovering sodium sulfate from dilute brine as industrial anhydrous sodium sulfate, in particular to a device and a method for preparing industrial anhydrous sodium sulfate.
Background
Sulfate radicals in the fresh brine after electrolysis in the chlor-alkali industry need to be removed, otherwise the electrolysis efficiency is influenced, and the main process for removing the sulfate radicals in the fresh brine in the early stage is a barium method or a calcium salt-chemical precipitation method or a membrane concentration and freezing process.
The chemical precipitation method is characterized in that the added medicament is mainly barium salt or calcium salt, the barium salt has toxicity, the environment and people can be greatly damaged, serious environment pollution can be caused, calcium sulfate scaling phenomenon is easy to occur in the chemical precipitation method production of the calcium salt, a pipeline is blocked, the operation strength is high, and the chemical precipitation method is not used by manufacturers at present.
A membrane method concentration and freezing process is a process which is commonly adopted at present, sodium sulfate is concentrated to 40-80g/L, and then mirabilite is separated out by a freezing method, but the separated mirabilite is provided with 10 crystal water, the temperature is higher than 33 ℃, the mirabilite can be dissolved by the crystal water per se to become a mixture of aqueous solution and the mirabilite, the transportation and the storage are not good, particularly, the problem is more prominent in summer, because the mirabilite is provided with 10 crystal water, namely, mirabilite particles contain about 55 percent of water, the industrial use is relatively limited, the mirabilite can be recycled only by preparing the mirabilite into anhydrous sodium sulfate, and a method for preparing the product is to remove the crystal water of the mirabilite by evaporation to prepare anhydrous sodium sulfate, namely, the anhydrous sodium sulfate can be sold.
Patent CN106745093A discloses a method for preparing anhydrous sodium sulphate by dehydrating mirabilite decahydrate in chlor-alkali production and related equipment for melting sodium sulphate, which removes crystal water of mirabilite by evaporation, however, because the vaporization heat of water is relatively large, the material for processing the equipment is required to be higher by heating at high temperature in a sodium chloride system with high concentration, the one-time investment of the equipment is large, the energy consumption and the operation cost are high, and in addition, patent CN102557081A discloses a method for recycling byproduct mirabilite in the caustic soda production process.
Patent ZL201610069549.5 discloses equipment and a method for preparing anhydrous sodium sulfate, ZL201711426345.3 discloses an integrated energy-saving anhydrous sodium sulfate recovery and manufacturing method, which is a method for preparing anhydrous sodium sulfate-anhydrous sodium sulfate from brine at low temperature, and overcomes the defects of the processes. However, in the above process, sodium chloride is often added in an excessive amount during the sodium chloride precipitation operation, so that the product purity is reduced and the product purity cannot meet the requirements of industrial processes, in addition, the sodium chloride addition is controlled by adopting a weight ratio in the salting-out process, the operation error is large, and the operation process is discontinuous, so that the sodium chloride addition is excessive, the supersaturation degree is excessive, a large amount of fine sodium sulfate crystals are precipitated from the system, the generation of large-particle anhydrous sodium sulfate cannot be well realized, and the fine anhydrous sodium sulfate particles generate dust during drying and subsequent use, thereby polluting the environment.
Therefore, those skilled in the art have made an effort to develop a method for preparing anhydrous sodium sulphate of technical grade, which can ensure the production of anhydrous sodium sulphate with high purity and large particles, and simultaneously realize continuous and stable operation.
Disclosure of Invention
In view of the above-mentioned drawbacks of the prior art, the present invention provides an apparatus and a method for desulfating dilute brine with low energy consumption and economic efficiency, and can produce large-particle anhydrous sodium sulfate-anhydrous sodium sulfate at room temperature.
In order to achieve the purpose, the invention provides an industrial-grade anhydrous sodium sulphate preparation device which is characterized by comprising a membrane concentration system, a continuous flow salting-out crystallization system, a centrifugal machine and a drying machine system, wherein the membrane concentration system, the continuous flow salting-out crystallization system, the centrifugal machine and the drying machine system are sequentially connected.
Further, the continuous flow salting-out crystallization system comprises a salt washing and mixing liquid tank, a first crystallization settler, a first crystallization tank, a second crystallization settler, a reflux circulating pump, a first salt adding device and a second salt adding device, wherein the salt washing and mixing liquid tank, the first crystallization settler, the first crystallization tank, the second crystallization settler and the reflux circulating pump are sequentially connected, the first salt adding device is connected with the first crystallization tank, and the second salt adding device is connected with the second crystallization tank.
Further, the first crystallization settler is connected with the centrifuge and dryer system, and the washing salt and liquid mixture tank is connected with the membrane concentration system.
Further, the first crystallization settler comprises a particle screener, and the first crystallization tank and the second crystallization tank comprise an online conductivity detection device and a stirrer, wherein the online conductivity detection device is used for controlling the first salt adding device and the second salt adding device.
Further, the method comprises the steps of: step 1, carrying out high-pressure concentration on a sodium sulfate solution and a saturated sodium chloride-containing solution in a membrane concentration system, and then dividing the sodium sulfate solution and the saturated sodium chloride-containing solution into two streams of water, wherein one stream is a concentrated solution containing supersaturated sodium sulfate, and the other stream is a membrane concentration system produced water containing lower sodium sulfate; step 2, putting the concentrated solution containing supersaturated sodium sulfate into a continuous flow salting-out crystallization system for salting out and reflux purification to obtain large-particle sodium sulfate crystal feed liquid; and 3, drying the large-particle sodium sulfate crystal feed liquid in the centrifugal machine and a dryer system to obtain a high-purity and large-particle anhydrous sodium sulfate product.
Further, the step 2 further comprises: step 2.1, stirring and mixing the supersaturated sodium sulfate-containing concentrated solution and the large-particle sodium sulfate crystal-containing backflow feed liquid generated by the second crystallization settler in the salt washing and mixing tank, wherein the supersaturated sodium sulfate-containing concentrated solution contains low sodium chloride, and the large-particle sodium sulfate crystal mixed with the sodium chloride particles in the backflow feed liquid generated by the second crystallization settler can be cleaned and dissolved, so that the purity of the sodium sulfate crystal is improved, and the cleaned large-particle sodium sulfate crystal feed liquid is obtained; 2.2, allowing the cleaned large-particle sodium sulfate crystal feed liquid to enter a first crystallization settler, allowing the feed liquid containing large-particle sodium sulfate crystals to settle and enter a centrifuge and dryer system for drying under the action of a particle screener to obtain a high-purity and large-particle anhydrous sodium sulfate product, and allowing the rest feed liquid containing saturated sodium sulfate and fine sodium sulfate particles to sequentially enter a first crystallization tank and a second crystallization tank; step 2.3, when the partial feed liquid containing saturated sodium sulfate and fine sodium sulfate particles sequentially enters the first crystallization tank and the second crystallization tank, sequentially and continuously adding sodium chloride solids into the first crystallization tank and the second crystallization tank through the first salt adding device and the second salt adding device, so that a supersaturated sodium sulfate solution is formed in the second crystallization tank, large-particle sodium sulfate crystals are separated out, and a solid-liquid mixture is obtained; and 2.4, allowing the solid-liquid mixture to enter the second crystallization settler, allowing the generated sodium sulfate crystal reflux feed liquid to enter a salt washing and mixing tank after the generated sodium sulfate crystal reflux feed liquid is settled, and allowing the rest part of the saturated sodium chloride supernatant to enter a membrane concentration system.
Further, the flow ratio of the concentrated solution containing supersaturated sodium sulfate in the step 2.1 to the reflux feed liquid containing sodium sulfate crystals generated by the second crystallization settler is 1: 2-1: 5.
Further, the retention time of the cleaned sodium sulfate crystal feed liquid in the step 2.2 in the first crystallization settler is controlled within 30-60 minutes, so that large-particle sodium sulfate crystals are settled.
Further, step 2.3 when the first crystallization jar and the second crystallization jar added the sodium chloride solid in proper order in succession, utilize on-line conductivity check out test set control sodium chloride solid adds slowly, avoids once only adding excessive sodium chloride, causes the supersaturation too big, produces a large amount of fine crystals, forms tiny sodium sulfate crystal, finally makes to separate out the sodium sulfate crystal and can all slowly grow up on the crystal nucleus, realizes the preparation of large granule sodium sulfate crystal.
Further, the residence time of the solid-liquid mixture in the second crystallization settler in the step 2.4 is controlled to be 60-90 minutes, so that all particles including sodium sulfate crystals and undissolved sodium chloride particles are settled.
The invention has the following technical effects:
1) the supersaturated sodium sulfate concentrated solution discharged from the membrane concentration system is crystallized and separated out large-particle sodium sulfate crystals at normal temperature by a salting-out method and accurately controlling the supersaturation degree in a continuous flow salting-out crystallization system, and simultaneously the purity of the anhydrous sodium sulfate is ensured by utilizing a reflux design, thereby overcoming the problems that the purity is reduced because sodium chloride particles are mixed in the anhydrous sodium sulfate caused by improper addition of sodium chloride in the product in the production of the anhydrous sodium sulfate by a common salting-out method, the crystallized particles of the salted-out anhydrous sodium sulfate are too small, and a large amount of dust is formed in industrial use,
2) compared with the existing method of firstly preparing mirabilite and then carrying out hot melting, evaporative crystallization or salting out to prepare anhydrous sodium sulfate, the method for recycling sodium sulfate in the dilute brine does not need the step of firstly generating mirabilite, and the whole process is carried out at normal temperature, so that the method has the advantages of low equipment investment, low energy consumption, good product quality and good economic value.
The conception, the specific structure and the technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, the features and the effects of the present invention.
Drawings
FIG. 1 is a schematic diagram of a membrane concentration system of an industrial-grade anhydrous sodium sulfate preparation device according to a preferred embodiment of the present invention;
FIG. 2 is a schematic diagram of a continuous-flow salting-out crystallization system and a centrifuge and dryer system of an apparatus for preparing technical-grade anhydrous sodium sulfate according to a preferred embodiment of the present invention;
wherein: 1-sodium sulfate-containing fresh brine raw water, 2-membrane concentration system water production, 3-supersaturated sodium sulfate-containing concentrated solution, 4-membrane concentration system, 5-saturated sodium chloride-containing solution, 6-mixed salt solution washing tank, 7-first crystallization settler, 8-first crystallization tank, 8-1-online conductivity detection equipment, 8-2-stirrer, 9-second crystallization tank, 9-1-online conductivity detection equipment, 9-2-stirrer, 10-second crystallization settler, 11-large-particle sodium sulfate crystal-containing reflux feed liquid, 12-centrifuge and dryer system, 13-1-first salt adding device, 13-2-second salt adding device and 14-reflux circulating pump.
Detailed Description
The technical contents of the preferred embodiments of the present invention will be more clearly and easily understood by referring to the drawings attached to the specification. The present invention may be embodied in many different forms of embodiments and the scope of the invention is not limited to the embodiments set forth herein.
In the drawings, structurally identical elements are represented by like reference numerals, and structurally or functionally similar elements are represented by like reference numerals throughout the several views. The size and thickness of each component shown in the drawings are arbitrarily illustrated, and the present invention is not limited to the size and thickness of each component. The thickness of the components may be exaggerated where appropriate in the figures to improve clarity.
Example 1
As shown in fig. 1 and 2, the industrial-grade anhydrous sodium sulphate preparation device is formed by sequentially connecting a membrane concentration system 4, a salt-washing mixed liquid tank 1, a first crystallization settler 7, a first crystallization tank 8, a second crystallization tank 9, a second crystallization settler 10 and a reflux circulating pump 14 in a continuous flow salting-out crystallization system, wherein the first salt adding device 13-1 is connected with the first crystallization tank 8, the second salt adding device 13-2 is connected with the second crystallization tank 9, and the first crystallization settler 7 is connected with the centrifuge and dryer system 12. The first crystallization tank 8 comprises an on-line conductivity detection device 8-1 and a stirrer 8-2, and the second crystallization tank 9 comprises an on-line conductivity detection device 9-1 and a stirrer 9-2.
Mixing sodium sulfate-containing light brine raw water 1 and a saturated sodium chloride-containing solution 5, passing through a membrane concentration system 4, and dividing into two streams of water under the action of high pressure, wherein one stream is membrane concentration system produced water 2, and the other stream is supersaturated sodium sulfate-containing concentrated solution 3.
The supersaturated sodium sulfate-containing concentrated solution 3 generated by the membrane concentration system 4 enters a salt washing and mixing solution tank 6 of a continuous flow salting-out crystallization system, and is mixed with the return feed solution 11 containing large-particle sodium sulfate crystals generated by the second crystallization settler 10 under the action of hydraulic stirring, and based on the relation between saturation and unsaturation, the supersaturated sodium sulfate-containing concentrated solution 3 dilutes sodium chloride mixed in the return feed solution 11 containing large-particle sodium sulfate crystals and dissolves trace sodium chloride fine solids, and controls the flow of the supersaturated sodium sulfate-containing concentrated solution 3: the flow rate of the reflux feed liquid 11 containing large-particle sodium sulfate crystals is 1: 2-1: 5, avoiding the phenomenon of back dissolution of sodium sulfate crystals in a salt washing mixed solution tank 6, wherein the flow rate of the supersaturated sodium sulfate concentrated solution 3 is 1.3L/h (200 g/L of sodium chloride, 170g/L of sodium sulfate).
The large-particle sodium sulfate crystal feed liquid cleaned by the salt washing liquid-mixing tank 6 enters a first crystallization settler 7 under the stirring disturbance effect, the tank body of the first crystallization settler 7 is small, the water flow disturbance fluctuation is large, the large-particle anhydrous sodium sulfate is settled at the cone bottom, and then the large-particle anhydrous sodium sulfate crystal feed liquid enters a centrifuge and dryer system 12, so that the anhydrous sodium sulfate product with the water content lower than 0.1% and the purity higher than 99% is obtained.
Under the action of water flow disturbance, a first crystallization settler 7 contains a saturated sodium sulfate and fine sodium sulfate particle part feed liquid, namely a first crystallization tank 8, wherein the small sodium sulfate particles are used as seed crystals; an online conductivity detection device 8-1 and a stirrer 8-2 are arranged in the first crystallization tank 8, the conductivity of the first crystallization tank 8 is maintained at low conductivity, the online conductivity detection device 8-1 controls the first salt adding device 13-1 in a linkage manner, a sodium chloride-sodium sulfate-water three-phase coexistence system, the first crystallization tank 8 and the first crystallization settler 7 provide enough crystal surfaces, sodium chloride is dissolved along with the addition of sodium chloride and the mechanical stirring action, sodium sulfate crystal nuclei are separated and attached to the crystal surfaces, the supersaturation is consumed in a spontaneous nucleation process to avoid the supersaturation, a large amount of fine particles are formed, and the online conductivity detection device 8-1 controls the addition amount of the sodium chloride of the first salt adding device 13-1.
The mixed feed liquid carrying a large number of sodium sulfate particles in the first crystallization tank 8 enters the second crystallization tank 9, the second crystallization tank 9 is internally provided with an online conductivity detection device 9-1 and a stirrer 9-2, the second crystallization tank 9 is utilized to provide enough crystal surface, the online conductivity detection device 9-1 is linked to instruct the second salt adding device 13-2 to slowly add sodium chloride solid, the sodium sulfate particles further grow up, the sodium sulfate separated out by the first crystallization tank 8 and the second crystallization tank 9 can be completely grown on the crystal surface, the supersaturation of the solution cannot exceed the maximum supersaturation of the solution, so that the supersaturation of the solute is eliminated in a nucleation process, and a large number of crystal nuclei cannot be generated.
Large-particle sodium sulfate liquid attached in the second crystallization tank 9 enters a second crystallization settler 10 under the action of a stirrer 9-2, return liquid 11 containing large-particle sodium sulfate crystals settles at the cone bottom and is pumped into a salt washing mixed liquid tank 6 through a return circulating pump 14, and saturated sodium chloride solution 5 and sodium sulfate-containing fresh brine raw water 1 are mixed and enter a membrane concentration system 4.
The water content of a centrifugal product is up to 5%, the water content of the centrifugal product is lower than 0.1% after drying, the purity of sodium sulfate is higher than 99%, the product meets the requirements of class I powder first-class products of industrial anhydrous sodium sulfate in national standard GBT6009-2014, the particle size of the product is larger than 0.425mm and is 2.25%, the particle size of the product is 74.13% between 0.2mm and 0.425mm, and the particle size of the product is 23.62% between 0.154mm and 0.2 mm.
The foregoing detailed description of the preferred embodiments of the invention has been presented. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the present teachings without departing from the inventive concepts. Therefore, the technical solutions available to those skilled in the art through logic analysis, reasoning and limited experiments based on the prior art according to the concept of the present invention should be within the scope of protection defined by the claims.
Claims (10)
1. The device for preparing the industrial anhydrous sodium sulphate is characterized by comprising a membrane concentration system, a continuous flow salting-out crystallization system, a centrifugal machine and a drying machine system which are sequentially connected.
2. The apparatus for preparing anhydrous sodium sulphate of industrial grade according to claim 1, wherein the continuous flow salting-out crystallization system comprises a mixed salt-washing liquid tank, a first crystallization settler, a second crystallization settler, a reflux circulation pump, a first salt adding device and a second salt adding device, the mixed salt-washing liquid tank, the first crystallization settler, the second crystallization settler and the reflux circulation pump are connected in sequence, the first salt adding device is connected with the first crystallization settler, and the second salt adding device is connected with the second crystallization settler.
3. The apparatus of claim 2, wherein the first crystallization settler is connected to the centrifuge and dryer system, and the mixed salt washing tank is connected to the membrane concentration system.
4. The apparatus of claim 3, wherein the first crystallization settler comprises a particle screener, and the first and second crystallization tanks comprise an on-line conductivity detection device for controlling the first and second salt adding devices and an agitator.
5. A method for preparing technical-grade anhydrous sodium sulfate using the technical-grade anhydrous sodium sulfate preparation device according to claim 4, wherein the method comprises the steps of:
step 1, carrying out high-pressure concentration on a sodium sulfate solution and a saturated sodium chloride-containing solution in a membrane concentration system, and then dividing the sodium sulfate solution and the saturated sodium chloride-containing solution into two streams of water, wherein one stream is a concentrated solution containing supersaturated sodium sulfate, and the other stream is a membrane concentration system produced water containing lower sodium sulfate;
step 2, putting the concentrated solution containing supersaturated sodium sulfate into a continuous flow salting-out crystallization system for salting out and reflux purification to obtain large-particle sodium sulfate crystal feed liquid;
and 3, drying the large-particle sodium sulfate crystal feed liquid in the centrifugal machine and a dryer system to obtain a high-purity and large-particle anhydrous sodium sulfate product.
6. The method for preparing technical-grade anhydrous sodium sulphate by the technical-grade anhydrous sodium sulphate preparation device according to claim 5, wherein the step 2 further comprises the following steps:
step 2.1, stirring and mixing the supersaturated sodium sulfate-containing concentrated solution and the large-particle sodium sulfate crystal-containing backflow feed liquid generated by the second crystallization settler in the salt washing and mixing tank, wherein the supersaturated sodium sulfate-containing concentrated solution contains low sodium chloride, and the large-particle sodium sulfate crystal mixed with the sodium chloride particles in the backflow feed liquid generated by the second crystallization settler can be cleaned and dissolved, so that the purity of the sodium sulfate crystal is improved, and the cleaned large-particle sodium sulfate crystal feed liquid is obtained;
2.2, allowing the cleaned large-particle sodium sulfate crystal feed liquid to enter a first crystallization settler, allowing the feed liquid containing large-particle sodium sulfate crystals to settle and enter a centrifuge and dryer system for drying under the action of a particle screener to obtain a high-purity and large-particle anhydrous sodium sulfate product, and allowing the rest feed liquid containing saturated sodium sulfate and fine sodium sulfate particles to sequentially enter a first crystallization tank and a second crystallization tank;
step 2.3, when the partial feed liquid containing saturated sodium sulfate and fine sodium sulfate particles sequentially enters the first crystallization tank and the second crystallization tank, sequentially and continuously adding sodium chloride solids into the first crystallization tank and the second crystallization tank through the first salt adding device and the second salt adding device, so that a supersaturated sodium sulfate solution is formed in the second crystallization tank, large-particle sodium sulfate crystals are separated out, and a solid-liquid mixture is obtained;
and 2.4, allowing the solid-liquid mixture to enter the second crystallization settler, allowing the generated sodium sulfate crystal reflux feed liquid to enter a salt washing and mixing tank after the generated sodium sulfate crystal reflux feed liquid is settled, and allowing the rest part of the saturated sodium chloride supernatant to enter a membrane concentration system.
7. The method for preparing the technical-grade anhydrous sodium sulphate by the technical-grade anhydrous sodium sulphate preparation device according to claim 6, wherein the flow ratio of the concentrated solution containing the supersaturated sodium sulphate to the reflux liquid containing the sodium sulphate crystals generated by the second crystallization settler in the step 2.1 is 1: 2-1: 5.
8. The method for preparing technical-grade anhydrous sodium sulphate by the technical-grade anhydrous sodium sulphate preparation device according to claim 6, wherein the retention time of the cleaned sodium sulphate crystal feed liquid in the step 2.2 in the first crystallization settler is controlled within 30-60 minutes, so that large-particle sodium sulphate crystals are settled.
9. The method for preparing anhydrous sodium sulphate of technical grade according to claim 6, wherein in step 2.3, when the first and second crystallization tanks continuously add solid sodium chloride in turn, the online conductivity detection device is used to control the slow addition of solid sodium chloride, so as to avoid excessive sodium chloride being added at one time, resulting in excessive supersaturation, large amount of fine crystals being generated, and fine sodium sulphate crystals being formed, and finally the precipitated sodium sulphate crystals can all slowly grow on crystal nuclei, thus realizing the preparation of large-particle sodium sulphate crystals.
10. The method for preparing technical-grade anhydrous sodium sulphate by using the technical-grade anhydrous sodium sulphate preparation device according to claim 6, wherein the residence time of the solid-liquid mixture in the second crystallization settler in the step 2.4 is controlled to be 60-90 minutes, so that all particles including sodium sulphate crystals and undissolved sodium chloride particles are settled.
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