KR100887517B1 - A method to produce salt using concentration salt water which is drained a process to produce ice from deep sea water - Google Patents

Abstract

The present invention relates to a method of making salt from concentrated brine while producing ice from low temperature deep sea water, and more particularly, by collecting low temperature deep sea water at a depth of more than 200 m from the sea surface. It relates to a method of preparing salt from concentrated brine during preparation.

To this end, the present invention, by taking the low-temperature deep sea water deeper than 200m from the sea surface and sends it to the anode chamber (4) of the electrolysis device (3) Oxidation reduction potential (ORP) value of +1,000 ~ + Treated with 1,200 ㎷ electrolytic oxidized water to the ice making process to produce sherbet ice at -2-12 ° C, and the concentrated brine is transferred to the cathode chamber (5) of the electrolysis device (3). Send the redox potential treated with -100 ~ -800-electrolytic reduced water to the salt manufacturing process to produce reducing salt.

Deep sea water, ice, salt, electrolysis, redox potential, electrolytic oxidation water, electrolytic reduction water

Description

A method to produce salt using concentration salt water which is drained a process to produce ice from deep sea water}

1 is a process chart for preparing ice and salt from deep sea water

2 is an electrolysis process chart

3 is a process chart of making ice

4 is a process for preparing salt by evaporation by atmospheric air

5 is a process for preparing salt by evaporation by heating evaporation

6 is a phase diagram of an H ₂ O—NaCl system.

7 is a state diagram when cooling sea water

Figure 8 is the precipitation rate of various salts according to the specific gravity change in the concentration of seawater at 35 ℃

9 is a precipitation rate of various salts according to specific gravity change in the concentration of seawater at 80 ℃

10 is a change in the concentration of various salts according to the specific gravity of the concentrated brine by the concentration of sea water

<Explanation of symbols for main parts of drawing>

1: Filtration Sump 2: Filtrate Transfer Pump

3: electrolysis device 4: anode chamber

5: cathode chamber 6: diaphragm

7: positive electrode 8: negative electrode

9: rectifier 10: ice maker

10a: cooling pipe 10b: sprinkling platter

10c: Sprinkler plate 10d: Scraper blade

10e: Scraper 11: Compressor

12: condenser 13: refrigerant storage tank

14: refrigerant circulation pump 15: expansion valve (Expansion valve)

16: Rotary valve 17: Screw conveyer

18: Trommel screen 19: Hopper

20: belt conveyer 21: concentrated brine reservoir

22: concentrated brine transfer pump 23: salt extraction tank

24: salt bath tank 25: evaporation tower by atmospheric air

26: spray nozzle 27: exhaust fan

28: return concentrated brine storage tank 29: concentrated brine return pump

30: precipitation salt conveying screw conveyer 31: dehydrated filtrate reservoir

32: dewatered filtrate transfer pump 33: evaporation tower by hot air

34: Demister 35: Blower

36: burner 37: heat exchanger

Ⓢ: Solenoid valve M: Motor

pHI: pH indicator

ORPIS: Oxidation reduction potential indicating switch

BI: Baume indicator

BIS: Baume indicating switch

TI: Temperature indicator

TIC: Temperature indicating controller

The present invention relates to a method for producing salt with concentrated brine while producing ice from low temperature deep sea water, and more particularly, to collect low temperature deep sea water at a depth of more than 200 m from the sea surface. It is sent to the anode chamber of the decomposition apparatus and treated with Oxidation Reduction Potential (ORP) value of + 1,000 ~ + 1,200㎷ electrolytic oxidation water to de-ice process and sherbet ice at -2 ~ -12 ℃. The brine concentrated during the production of ice) is sent to the cathode chamber of the electrolysis device, and the redox potential is treated with -100 to -800 kPa electrolytic reduced water to a salt manufacturing process to produce reducing salt.

Deep sea water is generally called deep sea water, which is deeper than 200m above sea level. Unlike surface waters, plankton and life cannot grow because sunlight does not reach, so the concentration of nutrients is high, There is no contaminant present in surface seawater because it is not mixed with surface seawater due to the difference in density, so it is low temperature stability, cleanliness, eutrophicity, minerals compared with surface seawater. There are characteristics such as balance characteristics and maturation, and the details are shown in Table 1.

                      Table 1 Characteristics of deep sea water

 Low temperature stability While the surface water temperature fluctuates greatly with the seasons, deep ocean waters are stable at low temperatures with little fluctuations in the water temperature.   Cleanliness Deep ocean water is deep and difficult to be polluted by terrestrial river water and air, and there are very few chemicals, bacteria, organisms and suspensions.   Eutrophication Deep sea water is deep in the sunlight and does not have photosynthesis. Compared with surface sea water, it contains many inorganic nutrients such as nitrogen, phosphorus, and silicic acid, which are necessary for the growth of living organisms.   Mineral properties Deep sea water contains a variety of essential minerals and is characterized by low impurities.    Aging Deep sea water matures over a long period of time under high pressure, and the clusters of water molecules are small grouped, so that the surface tension is low, and the permeability is high, and the thermal conductivity is high.

The deep sea water contains about 5 to 10 times more inorganic nutrients than the surface water, and contains various major elements necessary for the growth of animals and plants. The analysis of the major components of deep sea and surface seawater is shown in Table 2 below.

           Table 2 Depth analysis of deep sea and surface seawater

       division           Ulleungdo Hyunpo   Toyama Nyuzen, Japan    650m deep sea water  Surface waters  384m deep ocean water   Surface waters  Water temperature (℃)       0.5     23      1 to 2    8-30  Salinity (wt%)       3.41      3.45      3.41  3.3 to 3.4  Magnesium (wt%)   1,320  1,280  1,300   1,278  Calcium (mg / L)     393    403    390     402  Potassium (mg / L)     380    356    380     356  Nitric Acid Nitrogen (mg / L)       0.28      0.04      0.35       0.04  Total phosphorus (mg / ℓ)       0.06      0.012      0.055       0.012  Silicon (mg / l)       2.8      0.44      2.8       0.44  Number of live bacteria (dog / ml)       0    520      0   10 to 1,000  E. coli count (pcs / ml)      voice     voice     voice      voice

In terms of ice production, deep sea water deeper than 200 m from the sea level has lower temperatures compared to surface waters and can produce hygienically safe ice at low cost, and salt production is also hygienic. It is safe and can produce salts containing various minerals.

In particular, deep sea waters in the East Sea of Korea settled by dense differences in cold seawater that melted drift ice in the Sea of Okhotsk, off the coast of Vladivostok between Ostrov Sakhalin and Hokkaido. Deep inflow of water leads to a blockage of the Japanese archipelago, which slows the flow, and the water temperature is 1 to 2 ° C throughout the year at a depth deeper than 300m above sea level. Compared with deep water etc., it has a characteristic low about 8-11 degreeC.

In the case of ice production using seawater or deep ocean water of Japanese Patent Application Laid-Open No. 2006-189227, Japanese Patent Application Laid-Open No. 2006-10129, and Japanese Patent Application Laid-Open No. 2005-300002, a method of preparing sorbet ice by simply cooling seawater is proposed. However, there is a problem that the sterilization power is lowered during the cold storage of the fish and shellfish.

In the case of Japanese Patent Laid-Open Publication No. 2004-77105, a method of preparing sherbet ice having bactericidal power by injecting ozone (O ₃ ) into seawater has been proposed, but there is a high manufacturing cost problem.

In the present invention, the Bomedo (° Be) of the Baume's hydrometer showing the specific gravity of the seawater is expressed as a numerical value of the scale when the Bomedo hydrometer is floated in the liquid to measure the specific gravity of the liquid, rather than the specific gravity of the water. Heavy bomedoes for heavy liquids and light bomedoes for light liquids that are lighter than the specific gravity of water. Among them, pure liquids are pure water. 0 ° Be, 15% saline solution to 15 ° Be, with 15 divisions between them. For liquid solution, 10% saline solution to 0 ° Be and pure water to 10 ° Be. The scale is divided into 15 equal parts between them, and BOME (° Be) is widely used as a measure of concentration because seawater approximates salt concentration (wt%).

The relationship between the Bume (° Be) and the specific gravity (d) of the liquid is

For heavy media that has a specific gravity of liquid greater than that of water

d = 144.3 / (144.3-Be). … … … … … … … … … … … … … … … … … ⑴

In the case of an alarm field where the specific gravity of the liquid is lower than the specific gravity of the water

d = 144.3 / (134.3 + Be)... … … … … … … … … … … … … … … … … … ⑵

The present invention is to provide a method for producing salt by evaporating concentrated brine while making the sherbet ice with high sterilizing power by taking deep sea water of low temperature deeper than 200m from the sea surface to solve the above problems. It is an object of the invention.

In order to achieve the above object, the present invention is to take the deep sea water deeper than 200m from the sea surface, pretreatment step, producing electrolytic oxidation water in the electrolysis process, manufacturing sherbet ice, electrolyzed concentrated brine In the step of producing electrolytic reduced water, it is characterized by consisting of the step of preparing salt.

Hereinafter, described in detail by the accompanying drawings as follows.

I. Pretreatment stage

1. Intake process

In FIG. 1, the deep sea water is taken from the seabed deeper than 200m deep from the sea surface, and the intake method is to take down the pipe from the ship's surface to a depth of 200m deep from the sea surface, or deeper than 200m deep from the sea surface. The pipe is installed until the water intake by the pump, or the pipe is installed up to the depth of 200m from the sea level, and the intake well is installed below the sea level to take the water according to the siphon principle.

2. Pretreatment Filtration Process

Pretreatment filtration process uses sand filter, micro filter, ultra filtration alone or a combination of two or more to filter suspended solids (SS). Remove

At this time, the filtration pressure is determined in consideration of the pressure loss of the filter and the pressure loss of the pipe according to the operating conditions.The filtration speed of sand filtration is 6-10 m / hour, and the effective diameter of the filter sand is 0.3-0.45 mm, the uniformity coefficient shall be 2.0 or less, and the thickness of the filtrate layer shall be 0.5-1.0 m.

At this time, when the turbidity of the deep ocean water withdrawn is 2 mg / l or less, the pretreatment filtration process does not need to be performed.

Micro-filter and ultra-filter are not limited to the type of filtration membrane, and the supply pressure of the pump is decided by considering the filtration speed and the pressure loss according to the vendor's specifications. do.

In microfiltration or ultrafiltration, filtration treats the water's fouling index (FI) in the range of 2-4.

The FI value is a numerical value representing the fine turbidity concentration in the target water and is expressed by the following equation.

FI = (1-T ₀ / T ₁₅ ) x 100/15... … … … … … … … … … ⑶

T ₀ is the time required for filtration of the first 500 mL of sample water when the sample water was filtered under pressure of 0.2 MPa using a 0.45 μm microfiltration membrane, and T ₁₅ was filtered for 15 minutes in the same state as T _0. It is the time required for the filtration of 500 ml of sample water later.

II. Step of producing electrolytic oxidation water in the electrolysis process

When pre-filtered filtered water flows into the filtered water collecting tank (1) in the pre-filtering process, it is supplied to the anode chamber (4) of the electrolysis device (3) by the filtration water transfer pump (2), and the trommel to the cathode chamber (5). 3-15 volts of direct current electricity is supplied from the rectifier 9 to the positive electrode 7 of the positive electrode chamber 4 and the negative electrode 8 of the negative electrode chamber 5 while supplying concentrated brine filtered on the screen 18. Electrolytic oxidation water is generated by applying the redox potential value of the oxidation reduction potential indicating switch (ORPIS) installed in the anode chamber 4 to be in the range of +1,000 to +1,200 kV. When it is sent to the watering platter (10b) portion of the upper ice maker 10.

At this time, the electrochemical reaction occurring in the anode chamber 4 is as follows.

Water and electrolyte salts undergo a hydrolysis reaction.

^{_{H 2 O ⇔ 2H + + OH}} - ... … … … … … … … … … … … … … … … ⑷

NaCl ⇔ Na ^{+ +} Cl ^- ... … … … … … … … … … … … … … … … ⑸

Electrode reaction at the anode (7)

^{_{H 2 O → 2H + + 1}} / 2O 2 + 2e - ... … … … … … … … … … … … … … … … ⑹

2Cl ⁻ → Cl _{2 ( aq )} + 2e ⁻ . … … … … … … … … … … … … … … … ⑺

Solution reaction in the anode chamber (4)

_{Cl 2 (aq) + 2H 2} O → H + + Cl - + HClO ... … … … … … … … … … … … … ⑻

The electrolysis device (3) is made of polyvinyl chlorite (PVC), polyethylene (PE), polypropylene (PP), acrylic resin (Acrylonitrile butadiene styrene copolymer), butadiene resin (Butelite) ), Ebonite and Acrylic resin can be used.

The anode 7 of the anode chamber 4 is a corrosion resistant material and is subjected to baking coating of RuO ₂ -TiO ₂ on a titanium plate having a high chlorine and oxygen generation overvoltage. One dimensionally stable anode (DSA) electrode or a platinum plated electrode is used.

The diaphragm 6 is an exchange membrane that selectively permeates only a monovalent cation while suppressing the permeation of divalent or higher polyvalent cations. The main chain of the polystyrene-divinylbenzene system is main. Grafts such as polyethyleneimine or polyvinylpyridine have side chains on the negatively charged membranes that hold the negatively charged R-SO ₃ ⁻ in the chain An ion exchange membrane synthesized from a graft polymer or a graft polymer whose main chain is polyethyleneimine or polyvinyl pyridine and a side chain of polystyrene. It may be used without limitation, and preferably, polyethylene, polypropylene, polyvinyl chloride, polystyrene, or the like. Polyvinylpyridine, polyvinyl, which is a molecular structure having only a monovalent cation permeable to the main chain or side chain having the same molecular structure as that of a polymer composed of a cation exchange membrane fixed with a negatively charged R-SO ₃ ⁻ A membrane modified with a cationic resin such as amine (Polyethyleneamine) or polyethyleneimine (Polyethyleneimine) can be used, and in particular, polystyrene-graft-ethylene imine of polystyrene-divinylbenzene can be most preferably used.

In the case of using the diaphragm 8 that simultaneously transmits a bivalent or higher polyvalent cation, multivalent ions such as Ca, Sr, Mg, Fe, and Fe move to the cathode chamber 5 to form a cathode 8 plate. The use of the diaphragm 6 which permeates polyvalent ions should be avoided because scale is generated and electrical resistance is increased to reduce processing efficiency.

 III. Steps to Make Sherbet Ice

First, when reviewing the "phase equilibrium diagram of H ₂ O-NaCl" of FIG. 6, pure water freezes at 0 DEG C, but salt water such as seawater and deep sea water is salt (as shown in FIG. 6). As the concentration of NaCl) solution increases, it shows a freezing point drop, and it exists as a salt solution above this freezing line, but below this line, ice and a salt solution coexist.

At 40 ℃, the saturated concentration of salt is 26.71wt%, and if the temperature is cooled to 0.15 ℃, the saturated concentration of salt becomes 26.285wt%, and 0.425wt% of salt precipitates and if cooled to a temperature lower than 0.15 ℃, It is present as NaCl ₂ H ₂ O (2 water salt) crystal and saturated brine solution, where the salt concentration of 0.15 ℃ is 26.285wt%.

At this inflection point, the salt crystal becomes a transition point that transitions from a cubic system to a monoclinic system.

If it rapidly cools below this transition point, it proceeds like a dashed line and reaches -22.40 ℃. It exists only as ice and dihydrate salt (NaCl 2H ₂ O) crystals, but no solution exists. This is called.

This process point is metastable, and the temperature rises to a stable process point of 21.12 ° C., which is a process point for anhydrous salt, and the dihydrate salt is dissolved into a saturated solution having a concentration of 23.31 wt%.

Therefore, at 0.15 ° C or lower, it becomes a region where crystals of dihydrate salt (NaCl ₂ H ₂ O) and a saturated solution coexist, but when the salt concentration is higher than 61.863 wt% (calculated from NaCl / NaCl ₂ H ₂ O). Ice does not exist, and all the water of ice becomes crystal crystalline water of salt, and anhydrous salt and dihydrate salt coexist.

And as shown in "Phase diagram of H ₂ O-NaCl" of FIG. 6 and "State diagram when cooling seawater" of FIG. As the ice of (Sherbet) starts to form, semi-solid ice is produced when the temperature is -11-12 ° C, and solid ice is produced when the temperature is -22.40 ° C.

Refrigerants include ammonia, fluorohydrocarbon (HCFC) Freon, azeotropic mixed refrigerants, azeotropic mixed refrigerants, One kind of methyl chloride can be selected and used.

The deep seawater treated with the redox potential in the anode chamber 4 of the electrolysis device 3 in the range of +1,000 to +1,200 kW is supplied to the upper watering platter 10b of the ice maker 10. When the coolant is supplied to the cooling tube 10a to maintain the temperature in the ice maker 10 in the range of -5 to -11 ° C, when the sherbet-like ice is generated at the wall of the ice maker 10, the scraper blade 10d is used. When the scrape falls into the lower cone portion, the concentrated brine filtered by sending the scraper 10e to the rotary valve 16 through the screw conveyor 17 to the Trommel screen 18 is filtered. B) is sent to the concentrated brine reservoir (21) and conveyed to the sprinkling platter (10b) of the top of the ice maker (10) to the concentrated brine transfer pump (22) while the specific ratio of the Baume indicating switch (BIS) Baume indicating switch (BIS) Solenoid valve (ⓢ: 10 to 15 ° Be) It is sent to the cathode chamber (5) of the electrolysis device (3), Sherbet ice (concentrated brine) is separated by a belt conveyor (Belt conveyer) 20 to be sent to the storage and packaging process to prepare the ice. .

At this time, the concentrated brine filtered by supplying to the Trommel screen (Trommel screen 18) is concentrated in the concentration of 10 ~ 15wt% salt concentration of the brine sent to the concentrated brine reservoir 21 through the hopper (19).

The refrigerant gas heated in the ice maker (10) is sent to the compressor (11) to perform adiabatic compression, then to the condenser (12), cooled with cooling water, converted to a liquid refrigerant, and sent to the refrigerant storage tank (13). An expansion valve (15) is sent to the circulation pump (14) for isotropic entropy expansion and the temperature drop is sent to the cooling tube (10a) of the ice maker (10) and the fluid in the ice maker (10). To cool.

Ⅳ. Producing electrolytic reduced water from concentrated brine in the electrolysis process

The concentrated brine in the concentrated brine reservoir 21 is sent to the cathode chamber 5 of the electrolysis device 3 from the rectifier 9 to the anode 7 of the anode chamber 4 and the cathode 8 of the cathode chamber 5. DC red electric power of 3 to 15 volts is applied in the negative electrode chamber 5 so that the redox potential of the ORPIS is within the range of -100 to -850 ㎷. The water is converted into electrolytic reduced water and sent to the salt manufacturing process.

At this time, the electrochemical reaction occurring in the anode chamber 4 is as follows.

^{_{2H 2 O + 2e - → H}} 2 + 2OH - ... … … … … … … … … … … … … … … … ⑼

2Na ⁺⁺ 2OH → 2NaOH... … … … … … … … … … … … … … … … ⑽

The cathode 8 of the cathode chamber 5 is made of Ranney nickel or stainless steel sheet with high hydrogen generation overvoltage.

Ⅴ. Step to prepare salt

The brine concentrated while making the ice is subjected to a process of evaporating water by atmospheric air in summer, as shown in FIG. 4, and by heated air in winter or rainy season. The process as shown in Figure 5 to evaporate.

1. A process of preparing salt by dehydrating and drying the precipitated salt by the evaporative concentration process to evaporate moisture by atmospheric air and drying it.

In the case of evaporating moisture by atmospheric air, the precipitation of salt is sent to the cathode chamber 5 of the electrolysis apparatus 3 by sending the brine concentrated in the concentration range of 10 to 15 wt% in the ice making process, thereby reducing the redox potential. The concentrated brine treated in the range of -100 to -850 kPa with the concentrated brine returned to the concentrated brine conveying pump 29 through the spray nozzle 26 to the upper part of the evaporation tower 25 by atmospheric air. While spraying, air is sucked from the lower part of the evaporation tower 25 by atmospheric air by the exhaust fan 27, and the water in the concentrated brine is evaporated while countercurrently contacting the concentrated brine. Water flows to the upper portion of the evaporation tower 25 by atmospheric air by the concentrated brine return pump 29, and then flows into the upper portion of the evaporation tower 25 by the concentrated brine return pump 29. 8, the temperature of the hydrous water is 35 ° C. When the specific gravity of Bomedo reaches 25.8 ° Be, NaCl starts to precipitate, and when the precipitated salt (NaCl) is precipitated to the bottom of the salt extraction tank 23, the cone of the bottom center of the salt precipitation tank 23 is formed by the salt precipitation tank lake 24. (Cone) is collected and supplied to the dehydration process by the precipitation salt feed screw conveyor (30), and the dehydration filtrate is sent to the dehydration filtrate storage tank (31), and then by the dewatering filtrate transfer pump (32) salt extraction tank (23) center well Return to the center well, and when the depletion filtrate reservoir 31 has a specific gravity of 30 to 32 ° Be, the solenoid valve (ⓢ) is operated by the BME's specific gravity indication controller (BIS). The product is discharged, and the dehydrated salt is sent to a drying process to make salt.

The structure of the evaporation tower 25 by atmospheric air is the same as that of the cooling tower of an industrial plant. The material is made of preservative wood, fiber glass reinforced plastic (FRP), slate, and the like. Specifications, operation and design conditions are the same as the process of the evaporation tower 33 by hot air air described later.

2. A process of producing salt by dehydrating and drying the precipitated salt by the evaporative concentration process of evaporating water by heating air and drying it.

During the winter season, when the temperature is low, or during the rainy season, when the humidity is high, the brine concentrated in the salt concentration range of 10 to 15 wt% is sent to the cathode chamber 5 of the electrolysis device 3 so that the redox potential is increased. The concentrated brine treated in the range of -100 to -850 kPa is sent to the upper portion of the evaporation tower 33 by hot air air together with the conveyed concentrated brine and compressed air conveyed by the concentrated brine conveying pump 29 to spray the nozzle 26. When the air supplied from the blower 35 is sprayed through the heat exchanger 37 heated by the burner 36 while being sprayed through the air, the water vaporized while countercurrently contacting the hot air air is demister ( 34) is discharged to the atmosphere through the evaporation, and the concentrated brine is sent to the center well of the salt extraction tank 24, and as shown in FIG. (NaCl) starts to precipitate and when the precipitated salt precipitates, (24) collected by the lower center cone portion and sent to the dehydration process by the precipitation salt feed screw conveyor 30, the dehydrated filtrate is sent to the dewatered filtrate storage tank 31 by the dewatered filtrate transfer pump (32) While returning to the center well, the solenoid valve (ⓢ) is operated by the BME when the Bomedo specific gravity of the dewatered filtrate of the dewatered filtrate reservoir 31 is in the range of 30 to 32 ° Be. It is discharged as a product of water, and the dehydrated salt is sent to a drying process, dried to prepare salt, and then packaged, inspected, and commercialized.

The material of the evaporation tower 33 by hot air is preferably flame retardant titanium or SUS-316L. However, in consideration of economical efficiency, FRP (Fiber reinforced plastics) resin or epoxy resin is used on steel sheet. Lining or coating (Coating).

In order to improve the spraying efficiency of the injection nozzle 26, the compressed air is supplied at a pressure of 1 to 6 atm on the upstream side, and a mass ratio of air and liquid is supplied at a ratio of 1.1 to 1.2. .

The heating of the hot air air supplied from the blower 35 may use heavy oil or light oil in the burner 36, but may use natural gas (LNG) or liquid petroleum gas (LPG). The temperature of the wet air discharged to the atmosphere through the demister 34 is set to 60 to 80 ° C, and the dry evaporation in the evaporation tower 33 by hot air is only the constant drying. The evaporation tower 33 is designed such that the temperature of the evaporated brine discharged to the salt-precipitation tank 23 from the lower portion is 80 ° C. or less so that the weak components of heat are not thermally decomposed.

The overflowed brine in the salt-precipitation tank 23 flows into the conveyed concentrated brine storage tank 28, and the flow rate of the conveyed concentrated brine of the concentrated brine conveying pump 29 is 2 to 4 times the flow rate of the inflow.

The flow rate of the hot air air supplied from the blower 36 required for drying evaporation is determined in consideration of 5 to 10% of the heat loss in the value obtained from the enthalpy and the material balance of the device entrance.

When the flow rate of the hot air air supplied from the blower 35 is determined, the top diameter of the evaporation tower 33 by the hot air air shall have a flow velocity of the hot air air of 3 to 5 m / sec.

The angle α of the lower cone of the evaporation tower 33 by hot air is designed to be 10 ° ≤α≤60 °, and the ratio of the diameter of the outlet (D _o ) to the diameter of the tower (D) ) it is designed in the range of 0.3≤D _o /D≤0.7.

The salt-precipitation tank 23, the return concentrated brine storage tank 28, and the dehydration filtrate storage tank 31 may be made of epoxy coated on reinforced concrete or titanium, SUS-316L, or steel plate with FRP resin or epoxy resin. Use lining or coating.

The diameter of the salt-precipitation tank 23 has a solid load of 60-90 kg / m 2 · day of precipitation salt, a depth of 3-4 m, and a slope of the bottom of the bottom in the range of 1.5 / 10 to 2.5 / 10. To be designed).

The salt-precipitation tank rake 24 also uses the above-described flame-retardant material or coated with an epoxy resin on a steel sheet, and the rotation speed is 0.02 to 0.05 rpm, and the power of the speed reducer is equal to the diameter of the salt-precipitation tank 23. The torque is determined by taking into account the state of the precipitated salt.

The concentrated brine conveying pump (29), the precipitation salt conveying screw conveyor (30), the dehydration filtrate conveying pump (32) and the dehydrator are made of titanium or SUS-316L, all the brine piping is titanium, SUS-316L or PE ( Polyethylene) and PVC (Poly vinyl chloride) resin tubes are used.

Concentrated brine is evaporated and concentrated as shown in FIGS. 8, 9 and 10 while the concentrated brine evaporated from the evaporation towers 25 and 33 to the salt-precipitation tank 23. At 26 ° Be, NaCl begins to precipitate.

Continued evaporation, MgCl ₂ will be precipitated when the concentration of Bumedo concentration in the brine is 30-32 ° Be, followed by precipitation of MgBr ₂ .

Therefore, in the present invention, the filtrate dehydrated at a specific gravity of 30-32 ° Be is discharged to the liver water product so that the bromine (Br: :) low salt is produced.

As described above, the present invention is an alkaline reducing salt from concentrated brine produced as a by-product while producing ice with excellent sterilizing power in the range of +1,000 to +1,200 kW while being hygienically safe from low temperature deep sea water. It is expected to have a widely used effect in the ice and salt manufacturing field because it can be produced.

Claims (2)

Concentrated brine discharged from manufacturing sherbet ice during the pretreatment stage, electrolytic oxidation water production in the electrolysis process, and sherbet ice production in the stage of taking deep sea water deeper than 200m from sea level When supplied to the reservoir 21, concentrated brine is sent to the cathode chamber 5 of the electrolysis device 3, from the rectifier 9 to the anode 7 of the anode chamber 4 and the cathode 8 of the cathode chamber 5. 3 to 15 volts of direct current is applied so that the redox potential of the redox battery switch (ORPIS) installed in the cathode chamber 5 is in the range of -100 to -850 ㎷. The exhaust fan 27 is sprayed through the spray nozzle 26 onto the evaporation tower 25 by atmospheric air together with the concentrated brine returned to the concentrated brine return pump 29 by converting the electrolytic reduced water into the electrolytic reduced water. Dry air in the atmosphere is sucked from the bottom of the evaporation tower 25 by the atmospheric air After the water in the concentrated brine is evaporated while countercurrently contacting the brine, the overflowed water, which flows into the salt-precipitation tank 23 and overflows to the upper part, is sent to the concentrated brine storage tank 28, and then the concentrated brine is returned. Moisture evaporates while the pump 29 conveys the upper part of the evaporation tower 25 by atmospheric air. At a temperature of 35 ° C., NaCl starts to precipitate when the specific gravity of the Bumedo reaches 25.8 ° Be. When the salt (NaCl) is precipitated to the lower portion of the salt extraction tank 23, the salt is collected by the salt extraction tank rake 24 into the cone portion of the lower center of the salt extraction tank 23, and dehydrated by the precipitation salt feed screw conveyor 30. The dehydrated filtrate is fed to the dehydrated filtrate storage tank 31, and then returned to the center well of the saltwater extraction tank 23 by the dehydrated filtrate transfer pump 32. When the specific gravity of the province reaches 30 to 32 ° Be The controller operates the solenoid valve (ⓢ) by (BIS) to discharge the guard (苦 汁) product, and dehydrating the salt method for preparing the salt by drying sent to the drying process. The method according to claim 1, wherein instead of spraying the converted electrolyzed water with the concentrated brine returned to the concentrated brine return pump 29, the spray nozzle 26 is sprayed onto the evaporation tower 25 by atmospheric air. The converted concentrated electrolyzed water was sent to the upper part of the evaporation tower 33 by hot air air by the conveyed concentrated brine and the compressed air conveyed by the concentrated brine conveying pump 29 in the blower 35 while spraying through the spray nozzle 26. When the supplied air is supplied downward through the heat exchanger 37 heated by the burner 36, the evaporated water is released to the atmosphere through the demister 34 while being countercurrently contacted with the hot air air. , The evaporated brine is sent to the center well of the salt extraction tank 24, and when the temperature of the water is 80 ° C, the salt (NaCl) starts to precipitate when the specific gravity of Bumedo reaches 26 ° Be. Is precipitated by the salt bath tank 24 Collected into parts and sent to the dehydration process by the precipitated salt feed screw conveyor 30, the dehydrated filtrate is sent to the dewatered filtrate storage tank 31 and returned to the center wells by the dewatered filtrate transfer pump (32) When the specific gravity of the dehydrated filtrate in the dehydrated filtrate reservoir 31 is in the range of 30 to 32 ° Be, the solenoid valve (ⓢ) is operated by the BME to discharge the water into the product. , The dehydrated salt is sent to a drying process to dry to prepare a salt.

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