CN111011820B - Production process for refining low-sodium salt and alkaline water by adopting brine - Google Patents
Production process for refining low-sodium salt and alkaline water by adopting brine Download PDFInfo
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- CN111011820B CN111011820B CN201911354706.7A CN201911354706A CN111011820B CN 111011820 B CN111011820 B CN 111011820B CN 201911354706 A CN201911354706 A CN 201911354706A CN 111011820 B CN111011820 B CN 111011820B
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- 239000012267 brine Substances 0.000 title claims abstract description 133
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 133
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 117
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 238000007670 refining Methods 0.000 title claims abstract description 10
- 238000001704 evaporation Methods 0.000 claims abstract description 74
- 230000008020 evaporation Effects 0.000 claims abstract description 67
- 238000001914 filtration Methods 0.000 claims abstract description 61
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 46
- 238000004062 sedimentation Methods 0.000 claims abstract description 36
- 238000000034 method Methods 0.000 claims abstract description 34
- 150000003839 salts Chemical class 0.000 claims abstract description 25
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 23
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 23
- 238000005273 aeration Methods 0.000 claims abstract description 19
- 239000012535 impurity Substances 0.000 claims abstract description 18
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000001816 cooling Methods 0.000 claims abstract description 16
- 239000011575 calcium Substances 0.000 claims abstract description 15
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 15
- 159000000000 sodium salts Chemical class 0.000 claims abstract description 15
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000011777 magnesium Substances 0.000 claims abstract description 12
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 12
- 239000012452 mother liquor Substances 0.000 claims abstract description 12
- 230000001954 sterilising effect Effects 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 55
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 19
- 235000013162 Cocos nucifera Nutrition 0.000 claims description 14
- 244000060011 Cocos nucifera Species 0.000 claims description 14
- 239000004576 sand Substances 0.000 claims description 14
- 229910052799 carbon Inorganic materials 0.000 claims description 13
- 238000009287 sand filtration Methods 0.000 claims description 13
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 10
- 239000011591 potassium Substances 0.000 claims description 10
- 229910052700 potassium Inorganic materials 0.000 claims description 10
- 239000013535 sea water Substances 0.000 claims description 10
- 238000005276 aerator Methods 0.000 claims description 8
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 6
- 238000005119 centrifugation Methods 0.000 claims description 6
- 238000005868 electrolysis reaction Methods 0.000 claims description 6
- 239000011734 sodium Substances 0.000 claims description 6
- 229910052708 sodium Inorganic materials 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 5
- 239000006004 Quartz sand Substances 0.000 claims description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 21
- 239000011780 sodium chloride Substances 0.000 abstract description 13
- 241000894006 Bacteria Species 0.000 abstract description 4
- 238000004659 sterilization and disinfection Methods 0.000 abstract description 2
- 235000019605 sweet taste sensations Nutrition 0.000 abstract 1
- 235000002639 sodium chloride Nutrition 0.000 description 36
- 238000007664 blowing Methods 0.000 description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- 238000002425 crystallisation Methods 0.000 description 8
- 230000008025 crystallization Effects 0.000 description 8
- 238000001179 sorption measurement Methods 0.000 description 8
- 239000002893 slag Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 description 4
- 230000001877 deodorizing effect Effects 0.000 description 4
- 239000000945 filler Substances 0.000 description 4
- 230000002209 hydrophobic effect Effects 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 235000020188 drinking water Nutrition 0.000 description 3
- 239000003651 drinking water Substances 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- -1 salt sodium chloride Chemical class 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- 230000002378 acidificating effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 235000010755 mineral Nutrition 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000010413 mother solution Substances 0.000 description 2
- 239000000654 additive Substances 0.000 description 1
- 235000012206 bottled water Nutrition 0.000 description 1
- 238000009298 carbon filtering Methods 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002366 mineral element Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L27/00—Spices; Flavouring agents or condiments; Artificial sweetening agents; Table salts; Dietetic salt substitutes; Preparation or treatment thereof
- A23L27/40—Table salts; Dietetic salt substitutes
-
- 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
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
- A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Nutrition Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Physical Water Treatments (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a production process for refining low sodium salt and alkaline water by brine, which comprises the steps of adopting underground brine, carrying out sedimentation aeration, filtration, carbon dioxide removal and fine filtration, preheating, then removing evaporation, carrying out evaporation concentration to 20-30 baume degree, cooling and crystallizing a brine mixture obtained by evaporation, and then centrifuging to obtain low sodium salt and mother liquor; removing impurities from the crude low-sodium salt to obtain refined low-sodium salt; the steam condensate water in the evaporation process is subjected to reverse osmosis to obtain primary target water; adding mother liquor into primary target water to obtain mixed liquor with the conductivity of 20-30 us/cm and the total hardness of less than or equal to 50ppm; then electrolyzing to obtain alkaline ionized water with the pH value of 8.0-9.5 and the total hardness of 1-50 ppm; and then the alkaline water is obtained after bacteria filtration and ultraviolet sterilization. The edible salt prepared by the method can obviously improve the content of calcium and magnesium and reduce the content of sodium chloride; the prepared alkaline water has low hardness and sweet taste.
Description
Technical Field
The invention relates to the technical field of brine refining, in particular to a technology for refining low-sodium salt and alkaline water by using brine.
Background
The current common salt production market in China generally takes well mineral salt and sea salt as main materials, and the main technology is as follows: the well salt is poured into brine with saturated concentration to dissolve underground salt mine, and then the brine is extracted to be evaporated and crystallized into salt. The sea salt is prepared into large evaporation pond, small evaporation pond and crystallization pond in large area, and through sunlight exposure, crystallization to form coarse salt, washing, stoving and grinding into fine edible salt.
Spring water is used as drinking water in the market, and bottled water is prepared by sterilizing and packaging. The water quality is mainly acidic neutral water, and the weak alkaline water on the market is water in an alkaline state prepared by artificially adding additives, so that the safety is poor, and the taste of the water is poor.
In the salt production method by the process, the content of well mineral salt sodium chloride prepared and produced from underground brine is generally more than 99.10 percent, and the production of solarized sea salt is influenced by weather, the yield is unstable, the quality is easily polluted by the environment and a large amount of labor is needed. The two processes for producing the edible salt have high salt content and are too salty, so the two processes do not meet the health requirements of modern people, and other components are required to be added manually when the salt is improved into the low-salt, so that the proportion of the sodium chloride is controlled, the cost is high, and the process is complex.
In the aspect of drinking water, the existing production mode can achieve the sterilization effect through the process, but the water cannot be identified by naked eyes, and the components suffering from environmental pollution are difficult to remove and control. And generally has higher hardness and poor mouthfeel, and most of the hardness is in an acidic range.
In conclusion, the existing brine refining process has the following defects: (1) salt and alkaline water cannot be produced simultaneously; (2) The obtained salt is high in sodium content and beneficial to mineral elements, and is not beneficial to human health.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: aiming at the defects in the prior art, the process for producing the low-sodium salt and the alkaline water by brine refining is provided, the process adopts underground brine, and can simultaneously prepare the low-sodium salt and the alkaline water, wherein the obtained low-sodium salt contains 83-90% of sodium chloride, 0.5-2% of calcium, 0.01-2% of potassium, 0.01-1.5% of magnesium and 3-10% of water; the pH value of the prepared alkaline water is 8.0-9.5, and the total hardness is below 50 ppm.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a production process for refining low-sodium salt and alkaline water by using brine comprises the steps of adopting underground brine, settling, aerating, filtering, removing carbon dioxide, finely filtering, preheating and evaporating;
firstly, further filtering the preheated brine, wherein the filtering precision is more than or equal to 0.2 mu m; then leading to an evaporation platform, and evaporating and concentrating brine to 20-30 Baume degrees; cooling and crystallizing the brine mixture obtained by evaporation, and then centrifuging to obtain crude low sodium salt and mother liquor; condensing the steam in the evaporation process to obtain condensed water;
removing impurities from the crude low-sodium salt to obtain refined low-sodium salt;
performing reverse osmosis on the condensed water to obtain primary target water, wherein the pH value of the primary target water is 6.5-7.5, and the conductivity is less than or equal to 10us/cm;
adding the mother solution obtained by centrifugation into the primary target water, wherein the conductivity of the mixed solution is 20-30 us/cm, and the total hardness is less than or equal to 50ppm; then sending the water to a water ionizer, and obtaining alkaline ionized water with the pH value of 8.0-9.5 and the total hardness of 1-50 ppm through electrolysis;
and (3) filtering the alkaline ionized water, and sterilizing by ultraviolet rays to obtain the alkaline water product.
As a preferred technical scheme, a bag filter is adopted when the preheated brine is firstly subjected to further filtration.
Preferably, the underground brine contains 0.1 to 0.4 percent of calcium, 0.1 to 0.5 percent of magnesium, 1 to 3 percent of sodium, 0.01 to 0.1 percent of potassium, 1 to 2.5 percent of chloride ion and 0.2 to 1 percent of sulfate radical; the concentration is 4-6 Baume degree, the conductivity is 4000-6000 mus/cm, and the salt content is 8000-12000 mg/L.
As a preferred technical scheme, the sedimentation aeration is to introduce underground brine into a sedimentation tank to naturally settle the brine in an overflow mode; then leading the settled brine into an aeration device, wherein the brine treatment speed of the aeration device is 10-15 m 3 And h, deodorizing the brine in an aerator in a manner of air blowing and activated carbon adsorption.
Preferably, the filtering comprises sand filtering and activated carbon filtering; the sand filtration is to lead the seawater after sedimentation and aeration into a sand filter tank, quartz sand with the granularity of 2-8 meshes is filled in the sand filter tank, and the sand filtration speed is 10-15 m 3 H; the brine is processed for 5-10 min. The active carbon filtration is to filter the seawater after sand filtration by coconut shell active carbon, the granularity of the coconut shell active carbon is 10 to 20 meshes, and the filtering speed is 10 to 15m 3 The time for passing the brine through the coconut shell activated carbon is 5-10 min.
Preferably, the carbon dioxide removal is to introduce the filtered brine into a carbon remover to remove carbon dioxide in the brine so as to reduce the generation of precipitates such as calcium carbonate in the brine, and the concentration of carbon dioxide in the brine after carbon removal is less than 5ppm.
Preferably, the decarbonizer blows off brine from the lower part of the decarbonizer in a blowing mode, and the top end of the decarbonizer is vented. The upper end of the carbon remover is provided with a water distributor for spraying brine, the middle of the carbon remover is provided with an adsorption filler, and air is blown from the lower end.
As a preferable technical scheme, the method further comprises a secondary sedimentation step before the fine filtration, wherein the secondary sedimentation is to introduce the brine without carbon dioxide into a sedimentation tank, and the sedimentation tank is settled for 1 to 3 days.
Preferably, the fine filtration is to perform fine filtration on the brine after the secondary sedimentation in a fine filter, wherein the filtration precision is more than or equal to 1 μm.
Preferably, the preheating is carried out by utilizing the steam hydrophobic temperature of 80-100 ℃, and the brine preheating temperature is 55-65 ℃.
As a preferred technical scheme, the evaporation comprises three-stage evaporation, the preheated brine after being further filtered is led to an evaporation platform to be subjected to two-stage parallel evaporation, and then the concentrated brine after the two-stage evaporation is subjected to third-stage evaporation for 2-4 hours.
As a preferred technical scheme, the evaporation is steam heat tracing type evaporation, the steam pressure is 0.3-0.6 Mpa, and the temperature is 150-200 ℃.
As a preferable technical scheme, the pH value of condensed water obtained after steam in the evaporation process is condensed is between 6.5 and 7.5, and the conductivity is less than or equal to 150us/cm.
Preferably, the step of removing impurities from the crude low-sodium salt comprises the step of carrying out black residue collection treatment on the crude low-sodium salt, and collecting impurities such as residues and calcium residues.
Due to the adoption of the technical scheme, the invention has the beneficial effects that:
the invention relates to a production process for refining low-sodium salt and alkaline water by brine, which adopts underground brine, and is subjected to sedimentation aeration, filtration, carbon dioxide removal and fine filtration, then preheating and evaporation removal; cooling and crystallizing the brine mixture obtained by evaporation, and then centrifuging to obtain crude low sodium salt and mother liquor; condensing the steam in the evaporation process to obtain condensed water; removing impurities from the crude low-sodium salt to obtain refined low-sodium salt; performing reverse osmosis on the condensed water to obtain primary target water, adding the mother solution obtained by centrifugation, wherein the conductivity of the mixed solution is 20-30 us/cm, and the total hardness is less than or equal to 50ppm; then sending the water to an electrolytic water machine, and obtaining alkaline ionized water with the pH value of 8.0-9.5 and the total hardness of 1-50 ppm through electrolysis; filtering the alkaline ionized water, and sterilizing by ultraviolet rays to obtain the product alkaline water with the pH value of 8.0-9.5 and the total hardness of less than or equal to 50 ppm. The edible salt prepared by the method can obviously improve the content of calcium and magnesium and reduce the content of sodium chloride; the obtained low sodium salt contains 83 to 90 percent of sodium chloride, 0.5 to 2 percent of calcium, 0.01 to 2 percent of potassium, 0.01 to 1.5 percent of magnesium and 3 to 10 percent of water; the pH value of the prepared alkaline water reaches 8.0-9.5, and the total hardness is below 50ppm; and the taste is sweet compared with the common drinking water sold in the market after being drunk for a plurality of times.
Detailed Description
The invention is further illustrated by the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention can be made by those skilled in the art after reading the teaching of the present invention, and these equivalents also fall within the scope of the claims appended to the present application.
In the present application, unless otherwise specified, the percentages are by weight.
Example 1
Preparing brine: underground brine is adopted, wherein the underground brine contains 0.2% of calcium, 0.2% of magnesium, 1.2% of sodium, 0.03% of potassium, 1.5% of chloride ions and 0.4% of sulfate radicals; the concentration is 4 Baume degrees, the conductivity is 4500 mus/cm, and the salt content is 9000mg/L.
Sedimentation and aeration: leading underground brine into a settling pond, and naturally settling the brine in an overflow mode; then introducing the settled brine into an aeration device, wherein the brine treatment speed of the aeration device is 12m 3 And h, deodorizing the brine in an aerator in a mode of air blast and activated carbon adsorption.
Sand filtration: guiding the seawater after sedimentation and aeration into a sand filter tank, wherein quartz sand with the granularity of 3-4 meshes is filled in the sand filter tank, and the sand filtering speed is 12m 3 H; the brine is soaked for 7min.
Filtering with activated carbon: filtering the seawater after sand filtration by coconut shell activated carbon, wherein the granularity of the coconut shell activated carbon is 10-12 meshes, and the filtering speed is 12m 3 And h, the time for passing the brine through the coconut shell activated carbon is 7min.
Removing carbon dioxide: guiding the filtered brine into a decarbonizer, arranging a water distributor at the upper end of the decarbonizer for spraying brine, arranging an adsorption filler in the middle, blowing air from the lower end, blowing off the brine from the lower part of the decarbonizer, and discharging air from the top end. Removing carbon dioxide in the water to reduce the generation of calcium carbonate and other precipitates in the brine, wherein the concentration of the carbon dioxide in the brine is 4.5ppm after carbon removal.
Secondary sedimentation: and (4) introducing the brine from which the carbon dioxide is removed into a settling tank, and settling for 2 days in the settling tank.
Fine filtering: and (3) allowing the brine subjected to secondary sedimentation to enter a fine filter for fine filtration, wherein the filtration precision is 1 mu m.
Preheating: the preheating is carried out by utilizing the steam hydrophobic temperature of 90 ℃, and the preheating temperature of the brine is 58 ℃.
And (3) evaporation: introducing the preheated brine into a bag filter, and further filtering with the filtering precision of 0.2 mu m; then leading to an evaporation platform, carrying out two-stage parallel evaporation, and concentrating the brine to 12 Baume degrees, wherein the evaporation time is 2.5 hours; collecting the concentrated brine subjected to the two-stage evaporation into a third-stage evaporation tank, performing third-stage evaporation, and evaporating and concentrating the brine to 22 Baume degrees, wherein the evaporation time is 2.5 hours; the evaporation adopts steam heat tracing type evaporation, the steam pressure is 0.3Mpa, and the temperature is 200 ℃.
Cooling and crystallizing: transferring the salt water mixture obtained by evaporation to a cooling crystallization tank, standing for sedimentation, cooling for crystallization, cooling for 2 hours, pumping away supernatant after sedimentation is finished, and centrifuging the residual salt in a centrifuge to obtain crude low-sodium salt and mother liquor; removing impurities from the crude low-sodium salt to obtain refined low-sodium salt; condensing the steam in the evaporation process to obtain condensed water; the pH value of the condensed water is 6.8, and the conductivity is 130us/cm.
Removing impurities: removing impurities from the crude low-sodium salt comprises selecting black slag from the crude low-sodium salt, and selecting impurities such as residue, calcium slag and the like to obtain refined low-sodium salt; the low sodium salt contains 84% of sodium chloride, 1.2% of calcium, 0.8% of potassium, 1.0% of magnesium and 3% of water.
Preparing primary target water: and (3) performing reverse osmosis on the condensed water to obtain primary target water, wherein the pH value of the primary target water is 6.8, and the conductivity of the primary target water is 8us/cm.
Electrolysis: adding mother liquor obtained by centrifugation into the primary target water, wherein the conductivity of mixed liquor is 22us/cm, and the total hardness is 46ppm; then the water is sent to a water ionizer to be electrolyzed to obtain alkaline ionized water with the pH value of 8.5 and the total hardness of 40 ppm.
Preparing alkaline water: and (3) sterilizing the alkaline ionized water by using filter bacteria (the filter precision is 0.2 um) and ultraviolet rays to obtain the product alkaline water with the pH value of 8.5 and the total hardness of 40 ppm.
Example 2
Preparing brine: underground brine is adopted, wherein the underground brine contains 0.3% of calcium, 0.4% of magnesium, 2% of sodium, 0.07% of potassium, 2% of chloride ions and 0.8% of sulfate radicals; the concentration is 6 Baume degrees, the conductivity is 5000 mus/cm, and the salt content is 10000mg/L.
Sedimentation and aeration: leading underground brine into a settling pond, and naturally settling the brine in an overflow mode; then introducing the settled brine into an aeration device, wherein the brine treatment speed of the aeration device is 13m 3 And h, deodorizing the brine in an aerator in a manner of air blowing and activated carbon adsorption.
Sand filtration: guiding the seawater after sedimentation and aeration into a sand filter tank, wherein quartz sand with the granularity of 5-6 meshes is filled in the sand filter tank, and the sand filtering speed is 13m 3 H; the brine is taken for 6min.
Filtering with activated carbon: filtering the seawater after sand filtration by coconut shell activated carbon, wherein the granularity of the coconut shell activated carbon is 16-17 meshes, and the filtering speed is 13m 3 The time for passing the brine through the coconut shell activated carbon is 6min.
Removing carbon dioxide: guiding the filtered brine into a decarbonizer, arranging a water distributor at the upper end of the decarbonizer for spraying brine, arranging an adsorption filler in the middle, blowing air from the lower end, blowing off the brine from the lower part of the decarbonizer, and discharging air from the top end. And removing carbon dioxide in the water to reduce the generation of precipitates such as calcium carbonate and the like in the brine, wherein the concentration of the carbon dioxide in the brine is 4.5ppm after carbon removal.
Secondary sedimentation: and (4) introducing the brine from which the carbon dioxide is removed into a settling tank, and settling for 1.5 days in the settling tank.
Fine filtering: allowing the brine after secondary sedimentation to enter a fine filter for fine filtration, wherein the filtration precision is 1 mu m; the pump head of the fine filter is 20 m, the flow is 15m 3 And h, a pipeline DN50 is used for ensuring that the pressure of the brine entering the fine filter is 0.15MPa.
Preheating: the preheating is carried out by utilizing the steam hydrophobic temperature of 95 ℃, and the preheating temperature of the brine is 60 ℃.
And (3) evaporation: introducing the preheated brine into a bag filter, and further filtering with the filtering precision of 0.2 mu m; then leading to an evaporation platform, carrying out two-stage parallel evaporation, concentrating the brine to 15 Baume degrees, and carrying out evaporation for 3 hours; collecting the concentrated brine subjected to the two-stage evaporation into a third-stage evaporation tank, performing third-stage evaporation, and evaporating and concentrating the brine to 25 Baume degrees for 3 hours; the evaporation adopts steam heat tracing type evaporation, the steam pressure is 0.3Mpa, and the temperature is 200 ℃.
Cooling and crystallizing: transferring the salt water mixture obtained by evaporation to a cooling crystallization tank, standing for sedimentation, cooling for crystallization, cooling for 2 hours, pumping away supernatant after sedimentation is finished, and centrifuging the residual salt in a centrifuge to obtain crude low-sodium salt and mother liquor; removing impurities from the crude low-sodium salt to obtain refined low-sodium salt; condensing the steam in the evaporation process to obtain condensed water; the pH value of the obtained condensed water is 7.2, and the conductivity is 145us/cm.
Removing impurities: removing impurities from the crude low-sodium salt comprises selecting black slag from the crude low-sodium salt, and selecting impurities such as residues and calcium slag to obtain refined low-sodium salt; the low sodium salt contains 83.5% of sodium chloride, 1.0% of calcium, 1.0% of potassium, 1.1% of magnesium and 3.4% of water.
Preparing primary target water: and (3) performing reverse osmosis on the condensed water to obtain primary target water, wherein the pH value of the primary target water is 7.0, and the conductivity is 9us/cm.
Electrolysis: adding mother liquor obtained by centrifugation into the primary target water, wherein the conductivity of mixed liquor is 25us/cm, and the total hardness is 45ppm; then the water is sent to a water ionizer to be electrolyzed to obtain alkaline ionized water with the pH value of 8.8 and the total hardness of 30 ppm.
Preparing alkaline water: and (3) sterilizing the alkaline ionized water by using filter bacteria (the filter precision is 0.2 um) and ultraviolet rays to obtain the product alkaline water with the pH value of 8.8 and the total hardness of 30 ppm.
Example 3
Preparing brine: adopting underground brine, wherein the underground brine contains 0.35% of calcium, 0.45% of magnesium, 2% of sodium, 0.1% of potassium, 2.0% of chloride ions and 0.8% of sulfate radicals; the concentration is 6 Baume degrees, the conductivity is 5500 mu s/cm, and the salt content is 11000mg/L.
Sedimentation and aeration: leading underground brine into a settling pond, and naturally settling the brine in an overflow mode; then introducing the settled brine into an aerator, wherein the brine treatment speed of the aerator is 14m 3 And h, deodorizing the brine in an aerator in a mode of air blast and activated carbon adsorption.
Sand filtration: guiding the seawater after sedimentation and aeration into a sand filter tank, wherein quartz sand with the granularity of 5-6 meshes is filled in the sand filter tank, and the sand filtering speed is 14m 3 H; the brine time is 8min.
Filtering with activated carbon: filtering the seawater after sand filtration by coconut shell activated carbon, wherein the granularity of the coconut shell activated carbon is 15-16 meshes, and the filtering speed is 14m 3 And h, the time for passing the brine through the coconut shell activated carbon is 8min.
Removing carbon dioxide: introducing the filtered brine into a decarbonizer, arranging a water distributor at the upper end of the decarbonizer for spraying brine, arranging an adsorption filler in the middle, blowing air from the lower end, blowing off the brine from the lower part of the decarbonizer, and discharging air from the top end. Removing carbon dioxide in the water to reduce the generation of precipitates such as calcium carbonate and the like in the brine, wherein the concentration of the carbon dioxide in the brine is 5ppm after carbon removal.
Secondary sedimentation: and (4) introducing the brine from which the carbon dioxide is removed into a settling tank, and settling for 2.5 days in the settling tank.
Fine filtering: allowing the brine after secondary sedimentation to enter a fine filter for fine filtration, wherein the filtration precision is 1 mu m; the pump head of the fine filter is 20 m, the flow is 15m 3 Pipeline DN50, ensuring brine to enter the fine filterThe pressure is 0.14MPa.
Preheating: the preheating is carried out by utilizing the steam hydrophobic temperature of 100 ℃, and the preheating temperature of the brine is 62 ℃.
And (3) evaporation: introducing the preheated brine into a bag filter, and further filtering with the filtering precision of 0.2 mu m; then leading to an evaporation platform, carrying out two-stage parallel evaporation, concentrating the brine to 18 Baume degrees, and carrying out evaporation for 4 hours; collecting the concentrated brine subjected to the two-stage evaporation into a third-stage evaporation tank, performing third-stage evaporation, and evaporating and concentrating the brine to 28 Baume degrees for 4 hours; the evaporation adopts steam heat tracing type evaporation, the steam pressure is 0.3Mpa, and the temperature is 200 ℃.
Cooling and crystallizing: transferring the salt water mixture obtained by evaporation to a cooling crystallization tank, standing for sedimentation, cooling for crystallization, cooling for 2 hours, pumping away supernatant after sedimentation is finished, and centrifuging the residual salt in a centrifuge to obtain crude low-sodium salt and mother liquor; removing impurities from the crude low-sodium salt to obtain refined low-sodium salt; condensing the steam in the evaporation process to obtain condensed water; the pH value of the obtained condensed water is 7.5, and the conductivity is 135us/cm.
Removing impurities: removing impurities from the crude low-sodium salt comprises selecting black slag from the crude low-sodium salt, and selecting impurities such as residue, calcium slag and the like to obtain refined low-sodium salt; the low sodium salt contains 85% of sodium chloride, 0.8% of calcium, 0.2% of potassium, 0.5% of magnesium and 3.5% of water.
Preparing primary target water: and (3) carrying out reverse osmosis on the condensed water to obtain primary target water, wherein the pH value of the primary target water is 7.5, and the conductivity of the primary target water is 8.5us/cm.
Electrolysis: adding mother liquor obtained by centrifugation into the primary target water, wherein the conductivity of mixed liquor is 28us/cm, and the total hardness is 50ppm; then the water is sent to a water ionizer to be electrolyzed to obtain alkaline ionized water with the pH value of 9.2 and the total hardness of 35 ppm.
Preparing alkaline water: and (3) sterilizing the alkaline ionized water by using filter bacteria (the filter precision is 0.2 um) and ultraviolet rays to obtain the product alkaline water with the pH value of 9.2 and the total hardness of 35 ppm.
The alkaline water prepared in examples 1-3 above was subjected to taste testing by blind testing.
Claims (8)
1. A production process for refining low-sodium salt and alkaline water by adopting brine is characterized by comprising the following steps: adopting underground brine, and performing sedimentation aeration, filtration and carbon dioxide removal, wherein the carbon dioxide removal is to introduce the filtered brine into a carbon remover, and the concentration of carbon dioxide in the brine after carbon removal is less than 5ppm; fine filtering, preheating and evaporating; firstly, further filtering the preheated brine, wherein the filtering precision is more than or equal to 0.2 mu m; then leading to an evaporation platform, and evaporating and concentrating brine to 20-30 Baume degrees; cooling and crystallizing the brine mixture obtained by evaporation, and centrifuging to obtain crude low-sodium salt and mother liquor; condensing the steam in the evaporation process to obtain condensed water; the pH value of condensed water obtained after the steam in the evaporation process is condensed is between 6.5 and 7.5, and the conductivity is less than or equal to 150us/cm;
removing impurities from the crude low-sodium salt to obtain refined low-sodium salt;
performing reverse osmosis on the condensed water to obtain primary target water, wherein the pH value of the primary target water is 6.5-7.5, and the conductivity is less than or equal to 10us/cm;
adding mother liquor obtained by centrifugation into the primary target water, wherein the conductivity of mixed liquor is 20-30 us/cm, and the total hardness is less than or equal to 50ppm; then obtaining alkaline ionized water with pH value of 8.0-9.5 and total hardness of 1-50 ppm through electrolysis;
and (3) filtering the alkaline ionized water, and sterilizing by ultraviolet rays to obtain the alkaline water product.
2. The process of claim 1, wherein the brine is used to refine low sodium salt and alkaline water, and the process comprises: the underground brine contains 0.1 to 0.4 percent of calcium, 0.1 to 0.5 percent of magnesium, 1 to 3 percent of sodium, 0.01 to 0.1 percent of potassium, 1 to 2.5 percent of chloride ion and 0.2 to 1 percent of sulfate radical; the concentration is 4-6 Baume degree, the conductivity is 4000-6000 mus/cm, and the salt content is 8000-12000 mg/L.
3. The process of claim 1, wherein the brine is used to refine low sodium salt and alkaline water, and the process comprises: the sedimentation aeration is to lead underground brine into a sedimentation tank to naturally settle the brine in an overflow mode; then leading the settled brine into an aerator, wherein the brine treatment speed of the aerator is 10-15 m 3 /h。
4. The process of claim 1, wherein the brine is used to refine low sodium salt and alkaline water, and the process comprises: the filtration comprises sand filtration and active carbon filtration; the sand filtration is to lead the seawater after sedimentation and aeration into a sand filter tank, quartz sand with the granularity of 2-8 meshes is filled in the sand filter tank, and the sand filtration speed is 10-15 m 3 H; the activated carbon filtration is to filter the seawater after sand filtration by coconut shell activated carbon, the granularity of the coconut shell activated carbon is 10-20 meshes, and the filtration speed is 10-15 m 3 /h。
5. The process of claim 1, wherein the brine is used to refine low sodium salt and alkaline water, and the process comprises: and a secondary sedimentation step is also included before fine filtration, wherein the secondary sedimentation is to guide the brine without carbon dioxide into a sedimentation tank, and the sedimentation tank is sedimentated for 1 to 3 days.
6. The process of claim 5, wherein the brine is used to refine low sodium salt and alkaline water, and the process comprises: and the fine filtration is to put the secondarily-settled brine into a fine filter for fine filtration, wherein the filtration precision is more than or equal to 1 mu m.
7. The process of claim 1, wherein the brine is used to refine low sodium salt and alkaline water, and the process comprises: the preheating is carried out by utilizing steam at the temperature of 80-100 ℃, and the preheating temperature of the brine is 55-65 ℃.
8. The process of claim 1, wherein the brine is used to refine low sodium salt and alkaline water, and the process comprises: the evaporation comprises three-stage evaporation, the preheated brine after further filtration is introduced to an evaporation platform for two-stage parallel evaporation, and then the concentrated brine after two-stage evaporation is subjected to third-stage evaporation for 2-4 hours; the evaporation is steam heat tracing type evaporation, the steam pressure is 0.3-0.6 Mpa, and the temperature is 150-200 ℃.
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