CN114573004A - Production process of additive-free small-particle salt - Google Patents
Production process of additive-free small-particle salt Download PDFInfo
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- CN114573004A CN114573004A CN202210288400.1A CN202210288400A CN114573004A CN 114573004 A CN114573004 A CN 114573004A CN 202210288400 A CN202210288400 A CN 202210288400A CN 114573004 A CN114573004 A CN 114573004A
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- salt
- brine
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- evaporation
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- 150000003839 salts Chemical class 0.000 title claims abstract description 114
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 239000002245 particle Substances 0.000 title claims abstract description 10
- 239000012267 brine Substances 0.000 claims abstract description 70
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 69
- 238000004806 packaging method and process Methods 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000000746 purification Methods 0.000 claims abstract description 12
- 238000001035 drying Methods 0.000 claims abstract description 10
- 238000002425 crystallisation Methods 0.000 claims abstract description 9
- 230000008025 crystallization Effects 0.000 claims abstract description 9
- 230000018044 dehydration Effects 0.000 claims abstract description 7
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 7
- 238000003860 storage Methods 0.000 claims abstract description 7
- 235000002639 sodium chloride Nutrition 0.000 claims description 127
- 238000001704 evaporation Methods 0.000 claims description 41
- 239000002002 slurry Substances 0.000 claims description 35
- 230000008020 evaporation Effects 0.000 claims description 33
- 238000000034 method Methods 0.000 claims description 26
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 23
- 239000011780 sodium chloride Substances 0.000 claims description 20
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 12
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 12
- 239000004571 lime Substances 0.000 claims description 12
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 9
- 241001131796 Botaurus stellaris Species 0.000 claims description 8
- 239000003546 flue gas Substances 0.000 claims description 7
- 239000012452 mother liquor Substances 0.000 claims description 7
- 238000005086 pumping Methods 0.000 claims description 7
- 238000000605 extraction Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 235000017550 sodium carbonate Nutrition 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000002562 thickening agent Substances 0.000 claims description 3
- 238000003809 water extraction Methods 0.000 claims description 3
- 230000008719 thickening Effects 0.000 claims description 2
- 239000000654 additive Substances 0.000 claims 1
- 239000000276 potassium ferrocyanide Substances 0.000 abstract description 7
- XOGGUFAVLNCTRS-UHFFFAOYSA-N tetrapotassium;iron(2+);hexacyanide Chemical compound [K+].[K+].[K+].[K+].[Fe+2].N#[C-].N#[C-].N#[C-].N#[C-].N#[C-].N#[C-] XOGGUFAVLNCTRS-UHFFFAOYSA-N 0.000 abstract description 7
- 239000003795 chemical substances by application Substances 0.000 abstract description 6
- 238000002360 preparation method Methods 0.000 description 13
- 239000012535 impurity Substances 0.000 description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- 229910001424 calcium ion Inorganic materials 0.000 description 7
- 239000008267 milk Substances 0.000 description 6
- 235000013336 milk Nutrition 0.000 description 6
- 210000004080 milk Anatomy 0.000 description 6
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 5
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000010517 secondary reaction Methods 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 4
- 229910052925 anhydrite Inorganic materials 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 description 4
- 229910001425 magnesium ion Inorganic materials 0.000 description 4
- 239000001692 EU approved anti-caking agent Substances 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000008394 flocculating agent Substances 0.000 description 3
- 238000005065 mining Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000013535 sea water Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 239000007832 Na2SO4 Substances 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 241001122767 Theaceae Species 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 2
- 239000010931 gold Substances 0.000 description 2
- 229910052737 gold Inorganic materials 0.000 description 2
- 239000010442 halite Substances 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 2
- 239000000347 magnesium hydroxide Substances 0.000 description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 239000002455 scale inhibitor Substances 0.000 description 2
- 230000009291 secondary effect Effects 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 235000006694 eating habits Nutrition 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L magnesium chloride Substances [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
Classifications
-
- 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
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65B—MACHINES, APPARATUS OR DEVICES FOR, OR METHODS OF, PACKAGING ARTICLES OR MATERIALS; UNPACKING
- B65B1/00—Packaging fluent solid material, e.g. powders, granular or loose fibrous material, loose masses of small articles, in individual containers or receptacles, e.g. bags, sacks, boxes, cartons, cans, or jars
- B65B1/04—Methods of, or means for, filling the material into the containers or receptacles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65B—MACHINES, APPARATUS OR DEVICES FOR, OR METHODS OF, PACKAGING ARTICLES OR MATERIALS; UNPACKING
- B65B35/00—Supplying, feeding, arranging or orientating articles to be packaged
- B65B35/30—Arranging and feeding articles in groups
- B65B35/44—Arranging and feeding articles in groups by endless belts or chains
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D17/00—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces
- F25D17/02—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces for circulating liquids, e.g. brine
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/90—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in food processing or handling, e.g. food conservation
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Thermal Sciences (AREA)
- Materials Engineering (AREA)
- Physics & Mathematics (AREA)
- Combustion & Propulsion (AREA)
- Health & Medical Sciences (AREA)
- Nutrition Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to the field of salt production, in particular to a production process of additive-free small-particle salt, which comprises the steps of brine collection and transportation, purification, evaporative crystallization, centrifugal dehydration and drying (the salt temperature is 50℃)0C) Conveying by a belt, adjusting the pH value to be alkalescent, packaging by ton bags, temporarily storing, feeding by small packages, packaging by an automatic packaging machine and warehousing products. The invention ensures that the temperature of the drying salt is below 50 ℃ by increasing the flow of the circulating cold water in the drying process, and ensures that the food is eaten by adjusting the pH value before packagingThe salt is alkalescent, the salt is packaged by ton bags firstly during packaging, the ton bags are stored in a clean warehouse for temporary storage for 1 to 3 days, and the temporary ton bags of salt are lifted to a small conveying packaging belt line through a bucket elevator; the produced salt without the anticaking agent has high quality which is the level that sea and lake salt can not reach, and all quality indexes of the salt without the anticaking agent meet the GB/T5461 standard, and potassium ferrocyanide is not detected.
Description
Technical Field
The invention relates to the field of salt production, in particular to a production process of additive-free small-particle salt.
Background
Salt industry personnel know that salt is easy to cake, and most salt production enterprises adopt a mode of adding potassium ferrocyanide to ensure the looseness of the salt in order to prevent the salt from caking. Potassium ferrocyanide as one kind of food additive is completely available as specified in GB2760 standard if it is added in an allowable amount. However, it is considered that the addition of a substance such as cyanide is extremely harmful to the human body, and some people have a feeling of contradiction to the addition of the salt containing potassium ferrocyanide. Therefore, the present application intends to develop a common salt free of potassium ferrocyanide.
Domestic similar products mainly comprise naturally crystallized sea salt produced in coastal cities such as Shandong, Fujian, Guangdong and the like, and Qingqing salt with Qinghai characteristics and the like. The sea salt production in China generally adopts a solarization method, namely, coastal mudflats are utilized to build and open up a salt pan, the seawater is sucked into a pool by receiving tide and pumping up water, and brine is obtained by sunshine evaporation. When the brine concentration is evaporated to 25 Baume degrees, sodium chloride is separated out, namely the raw salt. Sea salt production is greatly influenced by sites and climates, and compared with refined salt, the sea salt has higher impurity content and the production amount is in a trend of shrinking year by year; the sea salt production process flow is as follows: moisture, brine preparation, crystallization and salt recovery.
Tibet halite is called Tibet halite because the origin is in Mongolia region and the salt turns green in white. The natural brine deposited in the tea card salt lake for thousands of years is taken as a raw material, and the tea card salt lake is prepared by natural sun-curing at the altitude of 3100 m under high-intensity ultraviolet rays, is uniform, white in grains, and is salty and fresh in taste. The salt is a special salt, accords with the eating habits of local people, is popularized all over the country at present, and the estimated sales volume of the salt variety can be increased.
Salt without anticaking agents on the market is generally prepared by natural crystallization, and raw materials are seawater and lake water, the components of the seawater and the lake water are complex, and the impurities are difficult to remove and are not thorough, so the salt with natural crystallization generally has higher impurity content and has certain requirements on sanitary conditions during crystallization.
At present, manufacturers which produce non-anticaking agents at home and abroad mainly concentrate on sea and lake salt production enterprises, are produced by natural evaporation crystallization, and are not easy to agglomerate due to large particles. But at the same time reveals the disadvantages of low main content, low throughput, etc. In the production of well mineral salt, some companies occasionally produce salt which is large in particle size and does not contain anticaking agents by adopting a recycling production process, but the total amount is small and the salt is rarely seen in the market.
Disclosure of Invention
In order to solve the technical problems, the invention provides a production process of additive-free small-particle table salt, which comprises the following steps:
a production process of additive-free small-particle table salt comprises the following steps:
s1, brine collection and transportation: adopting a double-well directional communication water extraction process for extraction, injecting clear water into a brine well by using a brine extraction pump to dissolve rock salt to form brine, and conveying the brine to a raw brine barrel of a purification workshop by using a brine conveying pump after the brine is collected;
s2, purifying: purifying by lime-flue gas method, mixing original bittern with mother liquor returned from salt-making workshop, adding lime for first-stage reaction, transferring qualified clear bittern into second-stage reaction, introducing flue gas, adding soda ash, reacting completely, and transferring into refined bittern barrel;
s3, evaporation and crystallization: heating by steam to continuously evaporate water, and evaporating to obtain semi-salt semi-water salt slurry; preheating refined brine in a purification workshop by using salt-making condensate water, then feeding the preheated brine into an evaporation tank, adding the preheated brine close to boiling into the evaporation tank, evaporating to obtain salt slurry, and transferring the salt slurry into another evaporation tank for evaporation;
S4, centrifugal dehydration: discharging salt slurry generated by salt legs of the two evaporation tanks into a salt slurry barrel, and pumping the salt slurry into a salt slurry thickener through a salt slurry pump; after the salt slurry in the salt slurry barrel is thickened, the salt slurry is sent into a centrifugal machine for dehydration and separation, and the throw-filtered mother liquor enters an evaporation system for evaporation again;
s5, drying, namely inputting the dried salt into a fluidized bed, and ensuring the temperature of the dried salt to be below 50 ℃;
s6, conveying to a packaging area through a belt;
s7, adjusting the pH value to be alkalescent, namely adjusting the pH value before packaging to ensure that the salt is alkalescent;
s8, packaging with a ton bag, wherein the ton bag is adopted for packaging;
s9, temporary storage: storing in clean warehouse for 1-3 days;
s10, small package feeding: the temporarily stored ton packaged salt is lifted to a small package conveying belt line through a bucket elevator;
and S11, packaging through an automatic vertical bag packaging machine, and warehousing products.
Further, the circulating cold water flow is increased in the step S5 to ensure that the temperature of the dried salt is below 50 ℃.
Further, in S3, the vapor for evaporation is from a heat pump, and the heat pump recompresses secondary vapor generated by the heat pump.
Further, the pH of common salt in S7 was adjusted to 7.5-8.5.
Furthermore, the moisture content after drying in the S5 is less than or equal to 0.40g/100 g.
Compared with the prior art, the invention has the beneficial effects that: according to the invention, the circulating cold water flow is increased in the drying process, the temperature of the dried salt is ensured to be below 50 ℃, the pH value is adjusted before packaging, the salt is ensured to be alkalescent, a ton bag is firstly adopted for packaging during packaging, the ton bag is stored in a clean warehouse for temporary storage for 1-3 days, and the temporary ton bag salt is lifted to a small conveying packaging belt line through a bucket elevator; the produced salt without the anticaking agent has high quality which is the level that sea and lake salt can not reach, and all quality indexes of the salt without the anticaking agent meet the GB/T5461 standard, and potassium ferrocyanide is not detected.
Detailed Description
In order that the invention may be more fully understood, reference will now be made to the following more detailed description. The present invention may be embodied in many different forms and is not limited to the embodiments described herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.
A production process of additive-free small-particle salt comprises the following steps:
1. collecting and transporting bittern: adopting a double-well directional communication water extraction process for extraction, injecting clear water into a brine well by using a brine extraction pump to dissolve rock salt to form brine, and conveying the brine to a raw brine barrel of a purification workshop by using a brine conveying pump after the brine is collected;
A brine collecting part: the vacuum salt-making waste water (or underground water mined on site) sent from a salt-making plant reaches 2 fresh water pools of a brine-mining station, the waste water is pumped from the fresh water pools by a brine-mining pump, is pressurized and sent to a brine-mining system main pipe, and is sent to a brine well control room by the system main pipe to be distributed to each brine well.
And a brine conveying part, wherein brine returned from each brine well enters a brine storage barrel, then enters a brine conveying pump, is pressurized by the brine conveying pump and then is conveyed to a salt plant.
2. Purifying: purifying by a lime-flue gas method, mixing raw brine with mother liquor returned from a salt manufacturing workshop, adding lime for primary reaction, transferring the qualified clear brine into secondary reaction, introducing flue gas, adding soda ash for complete reaction, and transferring into a refined brine barrel;
brine purification is a process of conveying raw brine conveyed from a mine to a salt making evaporation process after the raw brine is treated to reach a certain standard. The treatment method adopted by the invention is a lime-flue gas method, and the process is divided into three parts, namely preparation of the purification raw material, reaction process and salt mud treatment.
Brine purification refers to a process for removing impurities from brine by physical and chemical methods. Almost all brines contain impurities such as calcium, magnesium, sulfate and the like, and the effect of these impurities is manifested in the influence on the quality of the product and on the production process.
Due to CaSO4The composite material has the characteristic of inverse solubility, is separated out in the processes of brine conveying, preheating and evaporation, is attached to the wall of equipment of a pipeline to form scale, can seriously reduce the heat transfer coefficient, and the larger the scale layer is, the larger the heat transfer coefficient is reduced, so that the production capacity of the equipment is reduced. The elimination of the scale layer extends the effective working time.
CaSO in brine4、MgSO4、CaCl2、MgCl2The impurities can increase the boiling point and viscosity of the brine, thereby reducing the effective heat transferTemperature difference; the more impurities, the larger the discharge amount of the mother liquor for salt production, on one hand, the larger the heat quantity (namely, the higher the energy consumption); on the other hand, the recovery rate of NaCl is reduced, impurities in brine are effectively removed, and the product quality is obviously improved.
The process comprises the preparation process of lime milk, soda ash, flocculating agent, scale inhibitor and the like, the preparation of the lime milk and the soda ash are generally consistent, and the lime milk preparation is taken as an example for illustration. The quick lime is pumped into the lime tower through an air compression system, then is conveyed to the lime preparation barrel through a belt, and simultaneously, raw brine (refined brine is used during soda ash preparation) is injected into the barrel in proportion to control the concentration of lime milk to be between 100 and 150g/l, and the stirring of the lime preparation barrel can not be stopped all the time.
The preparation of the flocculant and the scale inhibitor is basically consistent, and the flocculant is taken as an example for illustration. The preparation solvent of the flocculant adopts low-temperature condensed water, and the amount of PAM to be added is calculated according to the preparation concentration. The preparation method comprises the following steps: firstly, a small amount of low-temperature condensed water is injected into a preparation barrel, then PAM is slowly added, and simultaneously PAM is added while water is injected until PAM is completely dissolved. (the concentration of the gold jar is 6kg at present, about 8 prescriptions in one barrel and about six ten-thousandths of the gold jar are prepared for standby application, and the concentration of PAM added into a brine reaction barrel is 1-3 ppm.
The main process of purification is the charging reaction process. Comprises a first-stage reaction and a second-stage reaction, and the reaction formula is as follows:
first-order reaction:
Ca(OH)2+ Mg2+== Mg(OH)2↓+ Ca2+
Ca(OH)2+ Na2SO4=== CaSO4↓+2 NaOH
Ca2++ SO4 2-==== CaSO4
and (3) secondary reaction:
2NaOH+ CO2== Na2CO3+H2O
CO2+ Ca(OH)2== CaCO3↓+ H2O
Na2CO3+ Ca2+=== CaCO3↓+2Na+
CaSO4+Na2CO3==CaCO3↓ +Na2SO4
in the first-stage reaction, the feeding time is determined according to the flow rate of the pump and the volume of the tank body, and the feeding time is about 2.5-3 hours. In the embodiment, the brine in the primary reaction tank mainly comprises two parts of raw brine and a salt making mother solution, and additionally, the brine from a raw brine barrel. Firstly, sampling and testing after the brine in the primary reaction barrel reaches a specified liquid level, measuring the concentrations of calcium ions, magnesium ions and sulfate ions, and calculating the amount of added lime milk according to a test result.
Adding lime milk, reacting for 5 hours, checking the content of calcium and magnesium ions and the value of over-alkali P, adding a flocculating agent after the calcium and magnesium ions are qualified, and settling for 2 hours to transfer the bittern to a secondary reaction tank. Discharging the salt mud after the first-stage refined brine is emptied.
In the secondary reaction, firstly, carbon dioxide is introduced for about 2 hours, then the pH value is repeatedly measured until the pH value reaches 10.2-10.6, the aeration is stopped, the excessive aeration is strictly prohibited, the sampling and assay are carried out, the calcium ions, the P value and the M value are measured, the amount of the added soda is calculated according to the inspection result, after the reaction is carried out for 2 hours, the contents of calcium, magnesium, sulfate radicals and P, M and sodium chloride are sampled and inspected, after the inspection is qualified, a flocculating agent is added, the mixture can be injected into a clear brine barrel after being settled for 2-4 hours, then the mixture enters an evaporation system through a multi-unit tubular filtration system FL-140, and simultaneously the filtered brine is injected into the evaporation system.
The main salt slurry magnesium hydroxide and calcium sulfate generated by brine purification primary reaction and the main salt slurry calcium carbonate generated by secondary reaction. Pumping the salt mud into a mud barrel through respective salt mud pumps, then pumping the salt mud into a mud settling barrel, enabling overflow clear liquid to enter, depositing the salt mud in a cone below the mud settling barrel, pumping the salt mud into a plate and frame filter, solidifying filter residues and then transporting the filter residues out of a workshop.
3. And (3) evaporation and crystallization: heating by steam to continuously evaporate water, and evaporating to obtain semi-salt semi-water salt slurry; the refined brine from a purification workshop is preheated by salt-making condensate water and then enters an evaporating pot, the preheated brine close to boiling is added into the evaporating pot to be evaporated into salt slurry, the salt slurry is transferred into another evaporating pot to be evaporated, the steam for evaporation comes from a heat pump, and secondary steam generated by the heat pump is recompressed to form the refined brine.
In the implementation, an MVR evaporator (MVR) is used, which is called MVR for short, and is a technology for reusing the energy of secondary steam generated by itself, thereby reducing the demand on external energy. The working process is that the low-temperature steam is compressed by a compressor, the temperature and the pressure are increased, the enthalpy is increased, and then the steam enters a heat exchanger for condensation, so that the latent heat of the steam is fully utilized. The principle is as follows: the initial steam is heated in the heating chamber by fresh steam, the solution is heated and boiled to generate secondary steam, the generated secondary steam is sucked by a turbine compressor, and after pressurization, the temperature and the pressure of the secondary steam are increased and enter the heating chamber as a heating heat source to be circularly evaporated. Thus, the circulating evaporation is continuously carried out, and the evaporated moisture is finally changed into condensed water to be discharged;
except for starting the MVR, no steam is needed in the whole evaporation process. In the multi-effect evaporation process, the secondary steam of a certain effect of the evaporator can not be directly used as a heat source of the effect, but can be used as a heat source of secondary effect or secondary effects. The MVR evaporator can compress secondary steam in the evaporator, and the secondary steam is used as a source of the effect, so that the original steam to be discarded is fully utilized, latent heat is recovered, the heat efficiency is improved, and the economical efficiency of the generated steam is equivalent to 30 effects of multi-effect evaporation.
4. And (3) centrifugal dehydration: discharging salt slurry generated by salt legs of an evaporation tank into a salt slurry barrel, and pumping the salt slurry into a salt slurry thickener through a salt slurry pump; thickening the salt slurry in the salt slurry barrel, sending the salt slurry into a centrifugal machine for dehydration and separation, and sending the filter-throwing mother liquor into an evaporation system for evaporation again;
5. drying, namely inputting the salt into a boiling bed, increasing the flow of circulating cold water, ensuring that the temperature of dried salt is below 50 ℃, and the water content after drying is less than or equal to 0.40g/100 g;
6. conveying the film to a packaging area through a belt;
7. adjusting pH to alkalescence, wherein the pH value is adjusted to 7.5-8.5 before packaging to ensure that the salt is alkalescent;
8. the ton bag is used for packaging, wherein a ton bag is used for packaging;
9. temporary storage: storing in clean warehouse for 1-3 days;
10. small package feeding: the temporarily stored ton packaged salt is lifted to a small package conveying belt line through a bucket elevator;
11. and packaging by an automatic bag erecting packaging machine, and warehousing the product.
According to the invention, the circulating cold water flow is increased in the drying process, the temperature of the dried salt is ensured to be below 50 ℃, the pH value is adjusted before packaging, the salt is ensured to be alkalescent, a ton bag is firstly adopted for packaging during packaging, the ton bag is stored in a clean warehouse for temporary storage for 1-3 days, and the temporary ton bag salt is lifted to a small conveying packaging belt line through a bucket elevator; the produced salt without the anticaking agent has high quality which is the level that sea and lake salt can not reach, and all quality indexes of the salt without the anticaking agent meet the GB/T5461 standard, and potassium ferrocyanide is not detected.
The industrial trial operation result shows that the process of the invention is relatively simple and convenient to operate, the investment limit of the fixed assets of the system is not large, the influence degree on the operation of the original salt making process is not large basically, and the implementation difficulty is small. The invention has excellent economic and technical indexes. The annual output can finally form the scale of 5 ten thousand tons, the output value is about 6500 ten thousand when the average 1300 yuan per ton is calculated, the tax is 585 ten thousand yuan, and the total profit is 2000 ten thousand when the profit is 400 yuan per ton.
The above description is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, several modifications and variations can be made without departing from the technical principle of the present invention, and these modifications and variations should also be regarded as the protection scope of the present invention.
Claims (5)
1. A production process of additive-free small-particle salt is characterized by comprising the following steps:
s1, brine collection and transportation: adopting a double-well directional communication water extraction process for extraction, injecting clear water into a brine well by using a brine extraction pump to dissolve rock salt to form brine, and conveying the brine to a raw brine barrel of a purification workshop by using a brine conveying pump after the brine is collected;
s2, purifying: purifying by lime-flue gas method, mixing original bittern with mother liquor returned from salt-making workshop, adding lime for first-stage reaction, transferring qualified clear bittern into second-stage reaction, introducing flue gas, adding soda ash, reacting completely, and transferring into refined bittern barrel;
S3, evaporation and crystallization: heating by steam to continuously evaporate water, and evaporating to obtain semi-salt semi-water salt slurry; preheating refined brine in a purification workshop by using salt-making condensate water, then feeding the preheated brine into an evaporation tank, adding the preheated brine close to boiling into the evaporation tank, evaporating to obtain salt slurry, and transferring the salt slurry into another evaporation tank for evaporation;
s4, centrifugal dehydration: discharging salt slurry generated by salt legs of the two evaporation tanks into a salt slurry barrel, and pumping the salt slurry into a salt slurry thickener through a salt slurry pump; thickening the salt slurry in the salt slurry barrel, sending the salt slurry into a centrifugal machine for dehydration and separation, and sending the filter-throwing mother liquor into an evaporation system for evaporation again;
s5, drying, namely inputting the salt into a fluidized bed to ensure that the temperature of the dried salt is below 50 ℃;
s6, conveying to a packaging area through a belt;
s7, adjusting the pH value to be alkalescent, namely adjusting the pH value before packaging to ensure that the salt is alkalescent;
s8, packaging with a ton bag, wherein the ton bag is adopted for packaging;
s9, temporary storage: storing in clean warehouse for 1-3 days;
s10, small package feeding: the temporarily stored ton packaged salt is lifted to a small package conveying belt line through a bucket elevator;
and S11, packaging through an automatic vertical bag packaging machine, and warehousing products.
2. The process for producing additive-free small table salt according to claim 1, wherein the temperature of the dried salt is 50 ℃ or lower by increasing the flow rate of the circulating cold water in the step S5.
3. The process for producing a small table salt without additives as claimed in claim 1, wherein the steam for evaporation in S3 is from a heat pump, and the heat pump recompresses the secondary steam generated by itself.
4. The process for producing additive-free small granulated common salt according to claim 1, wherein the pH of common salt is adjusted to 7.5 to 8.5 in S7.
5. The process for producing additive-free small granulated common salt according to claim 1, wherein the moisture content of dried S5 is not more than 0.40g/100 g.
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