CN111634925A - Method for separating mixed salt containing sodium chloride and sodium sulfate of organic matters after carbonization - Google Patents
Method for separating mixed salt containing sodium chloride and sodium sulfate of organic matters after carbonization Download PDFInfo
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- CN111634925A CN111634925A CN202010514093.5A CN202010514093A CN111634925A CN 111634925 A CN111634925 A CN 111634925A CN 202010514093 A CN202010514093 A CN 202010514093A CN 111634925 A CN111634925 A CN 111634925A
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- sodium sulfate
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- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 title claims abstract description 118
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 title claims abstract description 61
- 229910052938 sodium sulfate Inorganic materials 0.000 title claims abstract description 61
- 235000011152 sodium sulphate Nutrition 0.000 title claims abstract description 61
- 239000011780 sodium chloride Substances 0.000 title claims abstract description 59
- 150000003839 salts Chemical class 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000003763 carbonization Methods 0.000 title claims abstract description 14
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 230000008014 freezing Effects 0.000 claims description 36
- 238000007710 freezing Methods 0.000 claims description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 239000013078 crystal Substances 0.000 claims description 30
- 239000000243 solution Substances 0.000 claims description 20
- 238000001704 evaporation Methods 0.000 claims description 16
- 230000008020 evaporation Effects 0.000 claims description 15
- 238000001914 filtration Methods 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 14
- 239000000110 cooling liquid Substances 0.000 claims description 13
- 238000002425 crystallisation Methods 0.000 claims description 13
- 230000008025 crystallization Effects 0.000 claims description 13
- 239000012530 fluid Substances 0.000 claims description 13
- 239000012452 mother liquor Substances 0.000 claims description 9
- 238000005406 washing Methods 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000012266 salt solution Substances 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 4
- 238000004090 dissolution Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- 238000004806 packaging method and process Methods 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims 4
- 239000002351 wastewater Substances 0.000 abstract description 10
- 239000000126 substance Substances 0.000 abstract description 9
- 238000005516 engineering process Methods 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 239000002910 solid waste Substances 0.000 abstract description 4
- 238000010276 construction Methods 0.000 abstract description 2
- 239000000575 pesticide Substances 0.000 abstract description 2
- 230000002035 prolonged effect Effects 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 10
- 238000001816 cooling Methods 0.000 description 8
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 6
- 239000011575 calcium Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000011777 magnesium Substances 0.000 description 6
- 235000011121 sodium hydroxide Nutrition 0.000 description 5
- 230000007547 defect Effects 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 239000010409 thin film Substances 0.000 description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- 241001274216 Naso Species 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 229910001424 calcium ion Inorganic materials 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000012267 brine Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000001728 nano-filtration Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 230000017260 vegetative to reproductive phase transition of meristem Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/08—Preparation by working up natural or industrial salt mixtures or siliceous minerals
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
- C01P2006/82—Compositional purity water content
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a separation method of mixed salt containing sodium chloride and sodium sulfate after carbonization, which ensures that the sodium sulfate and sodium chloride in carbonized polluted salt can be treated once to meet the national standard industrial salt and no new solid waste is generated; zero discharge of waste water; the method solves the problems of high energy cost and complex equipment construction, and aims at the salt separation technology after carbonization of the polluted salt containing sodium sulfate and sodium chloride of organic matters generated in the production process of food factories and pesticide factories; in the solubility range of sodium chloride and sodium sulfate, the mixed salt of solutions with different concentrations is prepared, and the application range is wide; NaOH is added to adjust the pH value, so that substances easy to scale are removed, the production period of the evaporator cavity is prolonged, and the production cost is reduced; no wastewater is generated, and zero discharge of wastewater is realized; does not generate secondary solid waste, and completely realizes the harmless treatment of the polluted salt.
Description
Technical Field
The invention relates to the technical field of separation after carbonization of mixed salt, in particular to a separation method after carbonization of mixed salt containing sodium chloride and sodium sulfate.
Background
As shown in fig. 1, the conventional process and system for separating, concentrating and elutriating sodium chloride and sodium sulfate in concentrated salt wastewater mainly comprise a sodium chloride separation and concentration process section, a sodium sulfate elutriation, separation and concentration process section and a reuse water collection system; removing hardness of the strong brine, feeding the strong brine into a first-grade salt separation device, concentrating produced water of the first-grade salt separation device, then selectively carrying out COD (chemical oxygen demand) removal, desiliconization, decarburization or turbidity reduction treatment, feeding the concentrated produced water into a second-grade salt separation device, and evaporating and crystallizing the produced water to prepare sodium chloride; the concentrated water of the secondary salt separating device and part of the reuse water are mixed in proportion and then enter the primary elutriation device, and the generated concentrated water is mixed with the concentrated water of the primary salt separating device, then is subjected to COD removal or turbidity reduction treatment, and is then mixed with the reuse water in proportion.
However, the process and the system for separating, concentrating and elutriating sodium chloride and sodium sulfate in the concentrated salt wastewater have the following defects: 1. a small amount of mixed salt is generated at the end point, and the complete separation cannot be realized; 2. organic matters cannot be completely removed, and the quality of collected salt cannot be completely stable; 3. the evaporation and primary concentration proportion is small (30-40 percent), and the cost is high; 4. low heat energy utilization rate and the like.
Sodium sulfate and sodium chloride are separated and extracted from the high-salinity wastewater in the coal chemical industry, and the two salts are primarily separated through a nanofiltration process; then removing COD in the solution by an electrolytic oxidation technology; obtaining a product by adopting thermal crystallization and freezing technologies; as shown in fig. 1:
however, sodium sulfate and sodium chloride are separated and extracted from the high-salt wastewater in the coal chemical industry, the two salts are primarily separated through a nanofiltration process, and the electrolytic oxidation technology has the defects that: 1. the operation cost is high, and the energy consumption of electrolysis is large; the safety requirement level of the electrolytic oxidation process is high, and the operation risk is high; 3. the investment cost is high.
In addition, the direct concentration and separation technology of the MVR or multi-effect evaporator mainly utilizes different solubilities of sodium sulfate and sodium chloride to concentrate and separate salt. But the direct concentration technology has the following defects: 1. salt separation cannot be carried out thoroughly; 2. organic matters cannot be removed; 3. the product salt is a hazardous waste solid.
Disclosure of Invention
In order to overcome the defects, the invention provides a separation method of mixed salt containing sodium chloride and sodium sulfate after carbonization, so that the sodium sulfate and sodium chloride in the carbonized polluted salt can be treated once to meet the national standard industrial salt without generating new solid waste; zero discharge of waste water; the problems of high energy cost and complex equipment construction are solved.
The technical scheme adopted by the invention for solving the technical problem is as follows: a separation method of mixed salt containing sodium chloride and sodium sulfate, which is obtained after carbonization, comprises the following steps:
1) firstly, adding carbonized polluted salt into water for dissolution to dissolve the polluted salt, and filtering the dissolved polluted salt to obtain a mixed salt solution;
2) freezing the filtered mixed salt solution in a freezing crystallizer in a freezing crystallization mode to separate out sodium sulfate crystals; centrifuging and filtering the solution after the sodium sulfate crystal is separated out to obtain a sodium sulfate crystal, then performing secondary purification by using sodium sulfate as washing water, washing the sodium sulfate crystal, and removing sodium chloride in the crystal entrainment solution;
3) part of the refrigerating fluid after centrifugal filtration enters a refrigerating fluid collecting pool, and the other part of the refrigerating fluid is used as cooling water of a freezing crystallizer after evaporation and concentration and returns to the collecting pool after use;
4) circularly heating the cooling liquid of the freezing liquid collecting pool by the returned cooling liquid of the cold freezing crystallizer in the step 3), then feeding the cooling liquid into an evaporation concentrator, feeding condensed water generated in the concentration process into a condensed water collecting tank as water for dissolving salt in the step 1), and when the volume of the solution is concentrated to 1/4 of the original volume, feeding the solution into a sodium chloride freezing crystallizer to cool and separate out sodium chloride crystals;
5) and (3) centrifugally drying and washing the sodium chloride, then packaging the product, and returning the crystallization mother liquor to the step 1) for circular treatment.
As a further improvement of the invention, the water for dissolution in the step 1) adopts condensed water generated by concentration and sodium chloride crystallization mother liquor.
As a further improvement of the invention, in the step 2), the mixture is frozen in a freezing crystallizer to a temperature of-3 to-5 ℃.
As a further improvement of the invention, the concentration of sodium sulfate in the step 2) is 1%.
As a further improvement of the method, NaOH is added in the step 1) to adjust the pH value of the solution to be 8.5-9.0, so that the easy scaling substances are ensured to generate precipitates in the evaporation crystallization process, and the precipitates are dissolved, filtered and separated in fixed carbon, and the alkaline solution has high corrosivity on equipment in the processes of freezing crystallization and evaporation crystallization, so that the equipment is protected.
The invention has the beneficial effects that: compared with the prior separation technology, the invention has the following advantages:
1. the method aims at the salt separation technology after carbonization of the polluted salt containing sodium sulfate and sodium chloride of organic matters generated in the production process of food factories and pesticide factories;
2. in the solubility range of sodium chloride and sodium sulfate, the mixed salt of solutions with different concentrations is prepared, and the application range is wide;
3. NaOH is added to adjust the pH value, so that substances easy to scale are removed, the production period of the evaporator cavity is prolonged, and the production cost is reduced;
4. no wastewater is generated, and zero discharge of wastewater is realized;
5. secondary solid waste is not generated, and the harmless treatment of the polluted salt is completely realized;
6. reasonable utilization of energy, and about 30 percent reduction of production cost (mainly means that after freezing and centrifuging sodium sulfate, a refrigerating fluid is used as cooling water, and a sodium chloride centrifugal mother solution is returned for salt dissolving treatment to realize heat source utilization.)
Drawings
FIG. 1 is a prior art schematic;
FIG. 2 is a schematic flow chart of the present invention;
Detailed Description
For the purpose of enhancing the understanding of the present invention, the present invention will be further described in detail with reference to the following examples and the accompanying drawings, which are only used for explaining the present invention and are not to be construed as limiting the scope of the present invention.
FIG. 2 shows an embodiment of the present invention of sodium chloride containing organic substance, a method for separating sodium sulfate mixed salt after carbonization, which is characterized in that: the method comprises the following steps:
1) firstly, adding carbonized polluted salt into water for dissolution to dissolve the polluted salt, and filtering the dissolved polluted salt to obtain a mixed salt solution;
2) freezing the filtered mixed salt solution in a freezing crystallizer in a freezing crystallization mode to separate out sodium sulfate crystals; centrifuging and filtering the solution after the sodium sulfate crystal is separated out to obtain a sodium sulfate crystal, then performing secondary purification by using sodium sulfate as washing water, washing the sodium sulfate crystal, and removing sodium chloride in the crystal entrainment solution;
3) part of the refrigerating fluid after centrifugal filtration enters a refrigerating fluid collecting pool, and the other part of the refrigerating fluid is used as cooling water of a freezing crystallizer after evaporation and concentration and returns to the collecting pool after use;
4) circularly heating the cooling liquid of the freezing liquid collecting pool by the returned cooling liquid of the cold freezing crystallizer in the step 3), then feeding the cooling liquid into an evaporation concentrator, feeding condensed water generated in the concentration process into a condensed water collecting tank as water for dissolving salt in the step 1), and when the volume of the solution is concentrated to 1/4 of the original volume, feeding the solution into a sodium chloride freezing crystallizer to cool and separate out sodium chloride crystals;
5) and (3) centrifugally drying and washing the sodium chloride, then packaging the product, and returning the crystallization mother liquor to the step 1) for circular treatment.
The water for dissolving in the step 1) adopts condensed water generated by concentration and sodium chloride crystallization mother liquor.
Freezing the mixture in a freezing crystallizer in the step 2) to-3 to-5 ℃.
The concentration of sodium sulfate in the step 2) is 1%.
Adding NaOH to adjust the pH value of the solution to be 8.5-9.0 in the step 1).
The first embodiment is as follows:
after the waste salt generated by a certain food factory is carbonized, the content of sodium chloride is as follows: 94.15%, sodium sulfate: 2.85%, carbide: 2.94%, the rest: 0.06 percent. Firstly, preparing 150g/l sodium chloride concentration, 4.54g/l sodium sulfate solubility, carrying out 5m cultivation, carrying out 2.3Kg caustic soda consumption, stirring for 20 minutes, filtering, separating, freezing to-4.5 ℃ in a 1.5m cultivation reaction kettle, wherein no crystal is separated out, and carrying out secondary filtration on a cooling liquid to enter a 3m cultivation refrigerating liquid collecting pool for later use.
Transferring the freezing solution into a 1.5m evaporation concentration kettle for carrying out evaporation and concentration by adopting steam heating (negative pressure), concentrating until the residual volume is about 400L, and starting to have crystals, and transferring the condensed water generated in the concentration process into a 5m cultivation storage tank for collection. And when about 250L of rest powder is left in the kettle, transferring the powder into a 1m cooling reaction kettle for cooling by using subsequent refrigerating fluid, and when the temperature reaches 38 ℃, performing centrifugal drying separation on sodium chloride. The centrifugal mother liquor returns to the salt dissolving process for preparation.
After the preparation liquid is circulated for three cycles, sodium sulfate solid is generated and collected in a freezing and crystallizing link, and no crystal is generated and no pipeline blockage phenomenon occurs when the liquid after the sodium sulfate crystal is centrifugally spun off and used for cooling liquid.
The detection result of the product sodium sulfate decahydrate (acid-free sodium sulfate) is as follows:
| item | Index (I) |
| Sodium sulfate (NaSO)4) Mass fraction% | 97.5% |
| Calcium and magnesium (calculated as Mg) content mass fraction% | 0.3 |
| Sodium chloride (in terms of Cl) | 0.8 |
| Moisture (%) | 1.4% |
And (3) detecting a product sodium chloride:
| item | Index (I) |
| Sodium chloride (%) | 97.9 |
| Moisture (%) | 0.6 |
| Water-insoluble substance (%) | 0.1 |
| Total amount of calcium and magnesium ions (%) | 0.6 |
| Sulfate ion (%) | 0.8 |
Case two
After the waste salt generated by a certain food factory is carbonized, the content of sodium chloride is as follows: 35.5%, sodium sulfate: 57.01%, carbide: 2.44%, the rest: 0.05 percent. Firstly, preparing 143g/l sodium chloride concentration, 230g/l sodium sulfate solubility, 4m, stirring 1.8Kg caustic soda for 30 minutes, filtering, separating, freezing to-5 ℃ in a 1.5m thin-film labor reaction kettle, separating out sodium sulfate crystals, filtering the cooling liquid for the second time, and then entering a 3m thin-film labor refrigerating liquid collecting pool for later use.
Transferring the freezing solution into a 1.5m evaporation concentration kettle for carrying out evaporation and concentration by adopting steam heating (negative pressure), concentrating until the residual volume is about 350L, and starting to have crystals, and transferring the condensed water generated in the concentration process into a 5m cultivation storage tank for collection. And when about 260L of rest is left in the kettle, transferring to a 1m cooling reaction kettle for cooling by using subsequent refrigerating fluid, and when the temperature is up to 40 ℃, performing centrifugal drying separation on sodium chloride. The centrifugal mother liquor returns to the salt dissolving process for preparation.
After the sodium sulfate crystals are centrifugally spin-dried, no crystals are generated in the process of using the liquid for cooling the liquid, and the phenomenon of pipeline blockage is avoided.
The detection result of the product sodium sulfate decahydrate (acid-free sodium sulfate) is as follows:
| item | Index (I) |
| Sodium sulfate (NaSO)4) Mass fraction% | 97.3% |
| Calcium and magnesium (calculated as Mg) content mass fraction% | 0.35 |
| Sodium chloride (in terms of Cl) | 0.85 |
| Moisture (%) | 1.5% |
And (3) detecting a product sodium chloride:
| item | Index (I) |
| Sodium chloride (%) | 98.5 |
| Moisture (%) | 0.5 |
| Water-insoluble substance (%) | 0.1 |
| Total amount of calcium and magnesium ions (%) | 0.1 |
| Sulfate ion (%) | 0.8 |
Case three
After the waste salt generated by a certain food factory is carbonized, the content of sodium chloride is as follows: 15.5%, sodium sulfate: 82.01%, carbide: 2.44%, the rest: 0.05 percent. Firstly, preparing 49.14g/l sodium chloride concentration, 260.3g/l sodium sulfate solubility, carrying out 4m heavy labor, stirring 2.05Kg alkali consumption for 25 minutes, filtering, separating, freezing to-3.5 ℃ in a 1.5m thin-film flowering reaction kettle, separating out sodium sulfate crystals, carrying out secondary filtration on a cooling liquid, then entering a 3m thin-film flowering refrigerating liquid collecting pool for later use, and directly returning the first three batches of refrigerating liquids to prepare the dissolving liquid.
Transferring the freezing solution into a 1.5m evaporation concentration kettle for carrying out evaporation and concentration by adopting steam heating (negative pressure), concentrating until the residual volume is about 380L, and starting to have crystals, and transferring the condensed water generated in the concentration process into a 5m cultivation storage tank for collection. And when the rest of 230L is left in the kettle, transferring to a 1m cooling reaction kettle for cooling by using subsequent refrigerating fluid, and when the temperature is up to 40 ℃, performing centrifugal drying separation on sodium chloride. The centrifugal mother liquor returns to the salt dissolving process for preparation.
After the sodium sulfate crystals are centrifugally spin-dried, no crystals are generated in the process of using the liquid for cooling the liquid, and the phenomenon of pipeline blockage is avoided.
The detection result of the product sodium sulfate decahydrate (acid-free sodium sulfate) is as follows:
| item | Index (I) |
| Sodium sulfate (NaSO)4) Mass fraction% | 97.8% |
| Calcium and magnesium (calculated as Mg) content mass fraction% | 0.4 |
| Sodium chloride (in terms of Cl) | 0.8 |
| Moisture (%) | 1.0% |
And (3) detecting a product sodium chloride:
| item | Index (I) |
| Sodium chloride (%) | 98.2 |
| Moisture (%) | 0.8 |
| Water insoluble matter (%） | 0.12 |
| Total amount of calcium and magnesium ions (%) | 0.4 |
| Sulfate ion (%) | 0.48 |
Claims (5)
1. A separation method of mixed salt containing sodium chloride and sodium sulfate which is carbonized is characterized in that: the method comprises the following steps:
1) firstly, adding carbonized polluted salt into water for dissolution to dissolve the polluted salt, and filtering the dissolved polluted salt to obtain a mixed salt solution;
2) freezing the filtered mixed salt solution in a freezing crystallizer in a freezing crystallization mode to separate out sodium sulfate crystals; centrifuging and filtering the solution after the sodium sulfate crystal is separated out to obtain a sodium sulfate crystal, then performing secondary purification by using sodium sulfate as washing water, washing the sodium sulfate crystal, and removing sodium chloride in the crystal entrainment solution;
3) part of the refrigerating fluid after centrifugal filtration enters a refrigerating fluid collecting pool, and the other part of the refrigerating fluid is used as cooling water of a freezing crystallizer after evaporation and concentration and returns to the collecting pool after use;
4) circularly heating the cooling liquid of the freezing liquid collecting pool by the returned cooling liquid of the cold freezing crystallizer in the step 3), then feeding the cooling liquid into an evaporation concentrator, feeding condensed water generated in the concentration process into a condensed water collecting tank as water for dissolving salt in the step 1), and when the volume of the solution is concentrated to 1/4 of the original volume, feeding the solution into a sodium chloride freezing crystallizer to cool and separate out sodium chloride crystals;
5) and (3) centrifugally drying and washing the sodium chloride, then packaging the product, and returning the crystallization mother liquor to the step 1) for circular treatment.
2. The method for separating the mixed salt containing the sodium chloride and the sodium sulfate as the organic matter after carbonization according to the claim 1, is characterized in that: the water for dissolving in the step 1) adopts condensed water generated by concentration and sodium chloride crystallization mother liquor.
3. The method for separating the mixed salt containing the sodium chloride and the sodium sulfate as the organic matter after carbonization according to the claim 1, is characterized in that: freezing the mixture in a freezing crystallizer in the step 2) to-3 to-5 ℃.
4. The method for separating the mixed salt containing the sodium chloride and the sodium sulfate as the organic matter after carbonization according to the claim 1, is characterized in that: the concentration of sodium sulfate in the step 2) is 1%.
5. The method for separating the mixed salt containing the sodium chloride and the sodium sulfate as the organic matter after carbonization according to the claim 1, is characterized in that: adding NaOH to adjust the pH value of the solution to be 8.5-9.0 in the step 1).
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| CN113860334A (en) * | 2021-11-02 | 2021-12-31 | 山东金城晖瑞环保科技有限公司 | Method for separating sodium sulfate and sodium chloride from industrial waste salt |
| CN113880117A (en) * | 2021-12-09 | 2022-01-04 | 中国科学院过程工程研究所 | Separation method of mixed waste salt containing sodium sulfate and sodium chloride |
| CN115246650A (en) * | 2021-08-09 | 2022-10-28 | 江苏美东环境科技有限公司 | Method for preparing industrial potassium sulfate from hazardous organic waste salt containing potassium chloride and sodium sulfate |
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| CN102105399A (en) * | 2008-07-22 | 2011-06-22 | 阿克佐诺贝尔股份有限公司 | Sodium chloride production process |
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