KR101227157B1 - Manufacture equipment making salt from sea water - Google Patents

Abstract

PURPOSE: A salt manufacturing facility is provided to collect most of calcium components which is capable of being easily washed away, and to separate calcium sulfate crystals easily. CONSTITUTION: Enriched water, which is made of deep sea water by the reverse-osmosis treatment, is inputted and stored in an input tank. A concentration tank receiving the enriched water from the input tank evaporates and separates the moisture from the enriched water. A heater heats up the enriched water supplied to the concentration tank by the heat exchange. Calcium magma, which is obtained by evaporating and separating the moisture from the enriched water, is supplied and stored in a first buffer tank. The calcium magma is stored in crystal tanks(410, 420, 430). Calcium sulfate crystals are firstly separated by sedimentation from calcium magma, and classified to a first upper phase liquid and a first lower phase liquid. The moisture is evaporated and separated from the liquid. A calcium control tank(510) stores all or part of the first lower phase liquid which is drained from the crystal tank. A second buffer tank is supplied with and stores a first sodium chloride magma which is obtained by evaporating and separating the moisture from the calcium magma without the first lower phase liquid which is drained to the calcium control tank. A centrifuge(620) separates sodium chloride from the first sodium chloride magma which is supplied from the second buffer tank. Calcium sulfate crystals are secondly separated by sedimentation in sedimentation tanks(440, 450, 460), and classified to a second upper phase liquid and a second lower phase liquid. A mixer(630) mixes minerals with sodium chloride which is separated from the centrifuge. A rotary dryer(640) is supplied with sodium chloride mixed with mineral from the mixer, and transfers continuously while the moisture is dried.

Description

Continuous salt production facility by deep sea water {MANUFACTURE EQUIPMENT MAKING SALT FROM SEA WATER}

The present invention relates to a salt production facility, and more particularly, to a continuous salt production facility by the deep sea water that can process a large amount of deep sea water, can separate and extract minerals from the deep sea water and obtain salt. .

Deep sea water means seawater that is more than 200 meters deep without sunlight reaching it. Shallow sea water can cause photosynthesis or organic matter to propagate under the influence of sunlight, and air and land contaminants can easily enter, but these deep sea waters are not contaminated because these organics and contaminants do not descend to a depth of 200 m. It can keep nutrient rich minerals.

In addition, the deep ocean water is known to have properties such as an excellent scavenging effect on active oxygen by the action of dissolved metal ions because the essential trace elements and various mineral components are balanced.

Due to the useful effects of such deep sea water, various methods for obtaining salt or mineral water having high mineral content from deep sea water have been proposed.

Deep sea water is very salty and difficult to drink as it is, so in order to use it, the excess salts must be separated. However, since minerals, calcium and magnesium, which are useful minerals, may be lost in the process of separating salts, there is a need for a method for preventing the salts.

Conventionally, a method of preparing mineral salt or mineral water from deep ocean water by using electrolysis, electrodialysis or reverse osmosis membrane has been introduced, which is a beverage or salt from which excess salt (NaCl) has been removed to alleviate the salty taste of deep ocean water. The present invention relates to a method of preparing the present invention, or to a process of separating monovalent ions and divalent ions.

Korean Patent Publication No. 2010-0048613 discloses a method for producing mineral water and mineral salt from deep sea water, and selectively separates specific minerals such as magnesium, calcium or potassium from deep sea water to control the content of each mineral. In order to produce mineral water, a second evaporator is used to separate the precipitated sodium chloride by heating and concentrating deep ocean water, and monovalent and divalent cation selective exchange membranes and monovalent and divalent. Selectively separating the minerals using an electrodialysis apparatus combined with an anion selective exchange membrane, and to prepare mineral salts, by separating the sodium chloride precipitated by heating and concentrating the deep sea water using a secondary evaporator. Step, monovalent and divalent cation selective exchange membrane and monovalent and divalent anion selective exchange membrane Selectively separating the minerals using an electrodialysis apparatus, and in the mineral water tank, the weight ratio of potassium ions: magnesium ions: calcium ions is 1-100: 1-100: 1-100 The mixing step and the third evaporator, to evaporate the water of the mixture.

The present invention relates to a continuous salt production facility by the deep sea water that can process a large amount of deep sea water, and can extract and extract the minerals from the deep sea water, and to obtain the salt, especially energy waste during the treatment of deep sea water Minimizes, provides a recovery method of calcium that is likely to be lost during the process, and relates to a salt production facility where a continuous process can be achieved.

According to one preferred embodiment of the present invention, an input tank into which the deep sea water is subjected to reverse osmosis, and the concentrated water is injected and stored; A concentrated tank supplied with the concentrated water from the input tank and configured to evaporate and separate water in the concentrated water; A heater configured to heat the concentrated water supplied to the concentration tank by heat exchange; A first buffer tank configured to supply and store calcium magma obtained by evaporating and separating water from the concentrated water from the concentrated tank; The calcium magma is supplied and stored from the first buffer tank, and the primary sedimentation separation of the calcium sulfate crystal is performed from the calcium magma to be divided into a first supernatant and a first sublayer, and crystals are formed to evaporate and separate moisture. Tank; A calcium adjustment tank in which all or part of the first lower layer liquid discharged from the crystal tank is stored; A second buffer tank configured to supply and store a first sodium chloride magma obtained by evaporating and separating water from the crystal tank in a state excluding the first lower layer liquid discharged from the calcium magma to the calcium adjusting tank; And a centrifuge configured to separate sodium chloride from the first sodium chloride magma supplied from the second buffer tank. A continuous salt production facility is provided by deep ocean water.

In addition, the first lower layer liquid is supplied from the crystal tank, and the sedimentation tank is separated into a second supernatant liquid and a second lower layer liquid by the sedimentation sedimentation of the calcium sulfate crystals; The tank is characterized in that the second lower layer liquid is discharged to the calcium adjusting tank, and the second supernatant liquid is re-supplied to the crystal tank.

And from the centrifuge, a primary mother liquor formed by primary separation of sodium chloride from the first sodium chloride magma is resupplied to the crystal tank, and a second liquid from which the water is evaporated and separated from the primary mother liquor from the crystal tank. Sodium chloride magma is supplied to the second buffer tank, and in the centrifuge, sodium chloride is separated from the second sodium chloride magma.

Here, from the centrifugal separator, the mineral adjusting tank to which the secondary mother liquor is made by secondary separation of sodium chloride in the second sodium chloride magma; may be further included.

In accordance with a preferred embodiment of the present invention, a continuous salt production facility using deep sea water includes a mixer in which minerals are mixed with sodium chloride separated by the centrifuge; And a rotary dryer, which receives sodium chloride mixed with minerals from the mixer and continuously transports the mineral chloride, and is formed to dry moisture.

In addition, the mineral supplied to the mixer is made to be supplied from the mineral adjustment tank.

The crystal tank is divided into a first crystal tank, a second crystal tank, and a third crystal tank, and the first crystal tank, the second crystal tank, and the third crystal tank are sequentially used.

The concentrated tank may include: a first concentrated tank in which the concentrated water is supplied from the input tank, and a first concentrated water formed by evaporation and separation of water from the concentrated water is formed; A second enrichment tank configured to supply the first enrichment water from the first enrichment tank, and to form a second enrichment water formed by evaporation and separation of water in the first enrichment water; And the second concentrated water is supplied from the second concentrated tank, and water in the second concentrated water is evaporated and separated to form the calcium magma, and a third concentrate supplying the calcium magma to the first buffer tank. It is divided into tanks.

Here, each of the first concentration tank, the second concentration tank, and the third concentration tank includes a first circulation pipe, a second circulation pipe, and a third circulation pipe each configured to circulate the discharge and inflow of the solution supplied therein, respectively. The heater is divided into a first heater, a second heater, and a third heater, which are respectively formed on the first circulation tube, the second circulation tube, and the third circulation tube.

In addition, the heated water vapor for heat exchange is supplied to the heater, the water vapor is supplied so as to perform heat exchange while sequentially passing through the first heater, the second heater and the third heater.

Further, the water evaporated in the first concentration tank is connected to be supplied to the second heater, and the water evaporated in the second concentration tank is connected to be supplied to the third heater.

In addition, a supply pipe for supplying the concentrated water from the input tank to the first concentration tank is formed, on the supply pipe, an auxiliary heater is formed so that the concentrated water supplied to the first concentration tank is heated by heat exchange, Water evaporated in the third concentration tank is connected to be supplied to the auxiliary heater.

According to one embodiment of the present invention as described above, first, calcium magma is first formed by allowing water to evaporate through a concentration tank, and calcium sulfate crystals are separated by sedimentation separation in a crystal tank, In manufacturing, it is possible to collect crystals of calcium sulfate components having a very low solubility in a liquid state, thereby recovering most of the calcium components that are easily lost during the process. In addition, the present invention sequentially determines the crystal tank and the settling tank. By going through, the primary and secondary sedimentation separation can be made to facilitate the separation of calcium sulfate crystals.

In the present invention, the primary mother liquor from which sodium chloride is firstly separated from sodium chloride magma is re-supplied to the crystal tank, and the evaporation and centrifugation of water are performed again.

In addition, in the present invention, the crystal tank is composed of the first crystal tank, the second crystal tank and the third crystal tank, the enrichment tank is also composed of the first enrichment tank, the second enrichment tank and the third enrichment tank, In the process of preparing the salt, a continuous treatment process takes place, and a large amount of deep seawater can be processed quickly.

1 is a view showing a connection between some components of the continuous salt production facility by the deep sea water according to an embodiment of the present invention,
2 is a view showing a connection between some components of the continuous salt production facility by the deep sea water according to an embodiment of the present invention,
3 is a view showing the sedimentation separation process of calcium sulfate crystals in the treatment step by the continuous salt production facility by the deep sea water according to an embodiment of the present invention,
Figure 4 is a view showing the treatment process of the first sodium chloride magma in the treatment step by the continuous salt production facility by the deep sea water according to an embodiment of the present invention,
5 is a view showing the treatment process of the second sodium chloride magma in the treatment step by the continuous salt production facility by the deep sea water according to an embodiment of the present invention.

1 and 2, there is shown a connection relationship between some components of the continuous salt production facility by the deep sea water according to an embodiment of the present invention.

Continuous salt production facilities by the deep sea water according to a preferred embodiment of the present invention, as a facility for producing a salt using the deep sea water, it is basically made to use the deep sea water.

However, in the present invention, the deep ocean water is made using concentrated water concentrated by reverse osmosis (逆 浸透), the concentration process by reverse osmosis of the deep sea water can be made in a conventional manner, The description is omitted.

And in the description of the continuous salt production facility by the deep sea water according to the present invention, it will be divided into a facility for producing calcium magma, and a facility for producing salt while separating calcium sulfate and treating sodium chloride magma. The facility according to the former is shown in FIG. 1 and the facility according to the latter is shown in FIG. 2.

Here, the terms used in the present invention are simply defined as follows.

First, mother liquor means a saturated solution of solute. Accordingly, "primary mother liquor" and "secondary mother liquor" used in the present invention means a saturated solution of a solute such as mineral in the solvent. In particular, the primary mother liquor is a solution in which sodium chloride is first separated from the first sodium chloride magma described later, and the secondary mother liquor refers to a solution in which sodium chloride is secondarily separated from the second sodium magma.

Magma refers to a solution in which crystal is added to the mother liquor described above. Furthermore, 'calcium magma' used in the present invention is a solution containing calcium sulfate crystals or sodium chloride crystals in a saturated solution containing various minerals, and is a solution before separation of calcium sulfate crystals, and 'sodium chloride magma' is sulfuric acid. The solution after the separation of calcium crystals.

Here, 'separation of the calcium sulfate crystal' does not mean physically or chemically complete separation, but is used to mean that a significant portion of the calcium sulfate crystal is separated.

Hereinafter, first, a facility for producing calcium magma will be described with reference to FIG. 1.

In the continuous salt production facility by the deep sea water according to the present invention, the facilities for producing calcium magma are largely the input tank 100, the concentration tank (210, 220, 230), the heater (250, 260, 270) and It comprises a first buffer tank (300).

In addition, the concentration tank is made of a first concentration tank 210, the second concentration tank 220 and the third concentration tank 230 is separated for continuous processing, the heater is also the first heater 250, It is divided into a second heater 260 and a third heater 270.

The input tank 100 is supplied with the R / O (reverse osmosis) concentrated water (hereinafter, referred to as 'concentrated water') in which deep seawater is concentrated by reverse osmosis, and stored therein, and the first concentrated tank 210 is stored therein. ) To supply concentrated water.

A supply pipe 110 is formed in a line connected from the input tank 100 to the first concentration tank 210. In addition, a pump (not shown) and an auxiliary heater 240 are formed on the supply pipe 110 to supply concentrated water from the input tank 100, and the supply pipe 110 is formed by the auxiliary heater 240. Heat exchange is performed to increase the temperature of the concentrated water supplied to the first concentration tank 210 through. Thermal energy for heat exchange in the auxiliary heater 240 is supplied from steam discharged from the third concentration tank 230.

A first circulation tube 211 is formed in the first concentration tank 210, and the first circulation tube 211 circulates through the discharge and inflow of the concentrated water introduced into the first concentration tank 210. To be done. Accordingly, a pump (not shown) for circulation is formed on the first circulation pipe 211.

The first heater 250 is formed on the first circulation pipe 211, and supplies heat energy to increase the temperature of the concentrated water circulating through the first circulation pipe 211. Heated water vapor is used as a heat energy source supplied to the first heater 250, and the water vapor supplied to the first heater 250 sequentially drives the second heater 260 and the third heater 270. Through it, it is condensed and discharged. Accordingly, the condensed water discharged may be used as the reverse osmosis process or the washing water of the installation.

In the first heater 250, a heat exchange is performed between the heated water vapor supplied from the outside and the concentrated water passing through the first circulation pipe 211. This process is performed by the second heater 260 and the third heater ( The same is true for 270).

In the first concentration tank 210, the water is evaporated from the concentrated water heated through the first heater 250, the vaporized water vapor is discharged to the outside, the liquid concentrated water is the first The circulation pipe 211 is circulated.

Some of the concentrated water circulating in the first circulation pipe 211 flows into the second concentration tank 220, and water vapor evaporated in the first concentration tank 210 is transferred to the second heater 260. Supplied.

The second concentration tank 220, the second circulation tube 221, and the second heater 260 are the same as the first concentration tank 210, the first circulation tube 211, and the first heater 250. It is arranged in a structure, the third concentration tank 230, the third circulation pipe 231 and the third heater 270 is also the same.

In addition, the water vapor passed through the first heater 250 is supplied to the second heater 260, and is configured to continuously use waste heat for heating and to minimize energy waste.

The concentrated water flowing into the second concentration tank 220 and circulating through the second circulation pipe 221 is heated by the second heater 260, and the water of the second concentration tank 220 is concentrated in the second concentration tank 220. Evaporation takes place.

Some of the concentrated water circulating in the second circulation pipe 221 flows into the third concentration tank 230, and water vapor evaporated in the second concentration tank 220 flows to the third heater 270. Supplied.

The concentrated water introduced into the third concentration tank 230 is heated while circulating the third circulation pipe 231 in the same manner as described above to evaporate water and form the calcium magma. That is, the water is evaporated from the concentrated water in a continuous process, and calcium sulfate (CaSO ') crystals are included in the solution to form the calcium magma.

The calcium magma thus formed is supplied to and stored in the first buffer tank 300.

Hereinafter, with reference to Figure 2 will be described with respect to the facility for preparing the salt while separating the calcium sulfate from the calcium magma and treating sodium chloride magma.

In the continuous salt production facility by the deep sea water according to the present invention, the facilities for separating calcium sulfate from calcium magma and preparing the salt are largely divided into crystal tanks (410, 420, 430), calcium adjustment tank (510), and It consists of two buffer tank 610 and the centrifuge 620.

In addition, sedimentation tanks 440, 450, and 460 may be further formed on a path from the crystal tanks 410, 420, 430 to the calcium adjustment tank 510, respectively.

The crystal tanks 410, 420, and 430 are supplied with the calcium magma from the first buffer tank 300, and the first crystal tank 300, the first crystal tank for continuous supply and continuous processing of the calcium magma. It is divided into a two-crystal tank 420 and a third crystal tank 430.

The processing through the second crystal tank 420 and the third crystal tank 430 is performed in the same process as the processing through the first crystal tank 300, except that the time difference is different. For example, the input of the calcium magma from the first buffer tank 300 into the second crystal tank 420 may include the calcium magma from the first buffer tank 300 into the first crystal tank 300. Eight hours after the injection is made (based on the amount of 5108 kg input to each crystal tank), the third crystal tank 430 is also made at the same interval.

This time difference is that the first sodium chloride magma is the second sodium chloride from the first crystal tank 300 from the time when the calcium magma is introduced into the first crystal tank 300 from the first buffer tank 300. It is made to approximate the elapsed time until the time is supplied to the buffer tank 610.

Hereinafter, the description will be made based on the first determination tank 300.

The calcium magma supplied into the first crystal tank 300 includes calcium sulfate crystals, and primary sedimentation is performed after a predetermined time, and is divided into a first supernatant and a first sublayer by a density difference. Will be. That is, as the calcium sulfate crystal in the crystalline state sinks downward in the first crystal tank 300 by its own weight, a relatively large portion is placed below and a smaller density portion is positioned above.

The first lower layer liquid containing a substantial portion of the sulfurous calcium crystal is discharged from the first crystal tank 300, and is supplied to the sedimentation tank 440.

In the sedimentation tank 440, secondary sedimentation of calcium sulfate crystals is performed from the supplied first lower layer liquid, and is divided into a second upper layer liquid and a second lower layer liquid by a density difference. The calcium sulfate crystals in the second supernatant and the second sublayer liquid separated in this way are mostly included in the second sublayer liquid.

After the sedimentation tank 440 is divided into a second upper layer liquid and a second lower layer liquid, the second lower layer liquid containing most of the calcium sulfate crystal is discharged and stored in the calcium adjusting tank 510.

As described above, in the present invention, the crystals of the calcium sulfate component having a very low solubility are collected in a liquid state using the sedimentation separation method, whereby most of the calcium which is easily lost during the process can be recovered.

In the sedimentation tank 440, the second lower layer liquid is discharged into the calcium adjusting tank 510, but the second supernatant is supplied back into the first crystal tank 300 and mixed with the first supernatant. do.

After the first supernatant and the second supernatant are mixed in the first crystal tank 300, a process is performed in which the moisture is evaporated.

This heating is continued until water is sufficiently evaporated in the solution in which the first supernatant and the second supernatant are mixed to form first sodium chloride magma. In addition, the vapor to be evaporated is discharged to the outside to condense and can be used for the purpose, such as washing water.

The first sodium chloride magma is supplied to the second buffer tank 610, and as described above, calcium magma is supplied from the first buffer tank 300 to the second crystal tank 420. A series of processes are performed through the second crystal tank 420.

The first sodium chloride magma in the second buffer tank 610 is supplied into the centrifuge (620, centrifuge), and the components are separated by the density difference using centrifugal force.

Sodium chloride (NaCl) separated in the centrifuge 620 is moved to the mixer 630, and mixed with minerals of other components in the mixer 630. In this case, the mineral may be supplied from the mineral adjustment tank 520 to be described later.

Sodium chloride mixed with minerals in the mixer 630 is continuously transferred through the rotary dryer 640, the water is evaporated.

The solution in which sodium chloride is first separated from the first sodium chloride magma firstly supplied to the centrifuge 620 is the primary mother liquor, and the primary mother liquor is resupplied to the first crystal tank 300.

The primary mother liquor re-supplied into the first crystal tank 300 is in a saturation state of or near the solute including sodium chloride, and is heated again for precipitation of additional sodium chloride.

Accordingly, the primary mother liquid re-supplied into the first crystal tank 300 is heated, moisture is evaporated and discharged to form a second sodium chloride magma.

As the second sodium chloride magma is sequentially passed through the second buffer tank 610 and the centrifuge 620, sodium chloride is separated.

Sodium chloride firstly separated from the first sodium chloride magma and sodium chloride secondly separated from the second sodium chloride magma are packaged through a salt preparation process through the mixer 630, the rotary dryer 640, and the conveyor 650, and commercialized. .

The solution after the second separation of sodium chloride from the second sodium chloride magma becomes a secondary mother liquor, and the secondary mother liquor contains various minerals including calcium sulfate and sodium chloride, but most of calcium sulfate crystals and sodium chloride crystals are removed. It is done in a

The secondary mother liquor may be supplied to the mineral adjusting tank 520, and after extracting various minerals from the secondary mother liquor collected by the mineral adjusting tank 520, the secondary mother liquor may be supplied to the mixer 630.

Hereinafter, the mineral content of the solution for each process in the salt preparation process by the concentrated water made by the salt production facilities according to the present invention will be described.

3, the sedimentation separation process of calcium sulfate crystals is highlighted in the treatment step by the continuous salt production facility by the deep sea water according to an embodiment of the present invention.

As described above, the concentrated water treated by reverse osmosis flows into the input tank 100, and calcium magma is formed through the heater and the concentration tank, and the calcium magma passes through the first buffer tank 300. It is then introduced into the crystal tank.

The calcium magma is classified as the solution passes through the crystal tank, the sedimentation tank 440 and the calcium adjustment tank 510, and the mineral content of each step solution in this process is shown in Table 1 below.

The mineral content is based on a state where 5108 kg of calcium magma is introduced into the first crystal tank 300, and the concentration is 32.18% TS. (TS concentration: solids content / solution mass * 100)

division unit X1 X2 X3 X4 X5 X6 Driving time hr 3 One H2O Kg 3,464.00 3,177.60 346.40 346.40 226.40 120.00 CaSO4 (S) Kg 8.00 7.20 0.80 0.80 0.52 0.28 CaSO4 (C) Kg 58.24 - 58.24 58.24 58.24 MgSO4 Kg 100.08 90.72 10.08 10.08 6.59 3.49 MgBr2 Kg 3.84 3.46 0.38 0.38 0.25 0.13 MgCl2 Kg 157.44 141.70 15.74 15.74 10.29 5.45 KCl Kg 34.56 31.10 3.46 3.46 2.26 1.20 NaCl Kg 1,281.12 1,153.01 128.11 128.11 83.73 44.38 TS % 32.18 Sum 5,108.00 4,544.79 563.21 563.21 330.04 233.17

When 5108KG calcium magma is introduced into the first crystal tank 300 at a concentration of 32.18% TS, the mineral content at this time is as indicated in X1.

And the first sedimentation separation is made in the first crystal tank 300, when divided into the first supernatant and the second supernatant, the mineral component of the first supernatant is as shown in X2, the first lower layer The mineral component of the solution is as shown in X3.

The first lower layer liquid, which is the solution of the X2 component, moves to the sedimentation tank 440, and after the second sedimentation is separated in the sedimentation tank 440, the second supernatant is inside the first crystal tank 300. The second lower layer liquid is transferred to the calcium adjustment tank 510.

That is, the mineral component included in the second supernatant is as X5 in Table 1, and the mineral component included in the second lower layer is as X6.

As shown in Table 1, 58.24KG of calcium sulfate crystal contained in the total calcium magma is discharged to the calcium adjusting tank 510, and only 0.28KG of calcium sulfate is dissolved in the solution, and most of calcium is easily lost. It can be confirmed that this can be recovered.

4, the treatment process of the first sodium chloride magma is highlighted in the treatment step by the continuous salt production facility by the deep sea water according to an embodiment of the present invention.

division unit Y1 Y2 Y3 Y4 Driving time hr 5 H2O Kg 3,344.00 800 800 - CaSO4 (S) Kg 7.72 1.84 1.84 - CaSO4 (C) Kg - 5.88 5.88 - MgSO4 Kg 97.31 97.31 97.31 - MgBr2 Kg 3.71 3.71 3.71 - MgCl2 Kg 151.99 151.99 151.99 - KCl Kg 33.36 33.36 33.36 - NaCl (S) Kg 1,236.74 301.92 301.92 - NaCl (C) Kg - 934.82 - 934.82 TS % Sum 4,874.83 2,330.83 1,396.01 934.82

Mineral components in the case where the second supernatant is re-supplied into the first crystal tank 300 and mixed with the first supernatant are the same as Y1 of Table 2.

Thereafter, a first sodium chloride magma is formed through evaporation and discharge of moisture in the first crystal tank 300, and the mineral component of the first sodium chloride magma is equal to Y2. It can be seen in Table 2 that 934.82KG of crystalline sodium chloride is produced in this first sodium chloride magma, which is formed by evaporation and discharge of water.

Through the centrifugal separator 620, sodium chloride is firstly separated from the first sodium chloride magma, and the separated sodium chloride is salt-produced through the mixer 630, the rotary dryer 640, and the like, and sodium chloride is firstly separated. The primary mother liquor is resupplied to the first crystal tank 300.

At this time, the mineral component of the primary mother liquor is the same as Y3 in Table 2.

5, the treatment step of the second sodium chloride magma is highlighted in the treatment step by the continuous salt production facility by the deep sea water according to an embodiment of the present invention.

division unit Z1 Z2 Z3 Z4 Driving time hr H2O Kg 800.00 250.00 250.00 - CaSO4 (S) Kg 1.84 0.58 0.58 - CaSO4 (C) Kg 5.88 7.14 7.14 - MgSO4 Kg 97.31 97.31 97.31 - MgBr2 Kg 3.71 3.71 3.71 - MgCl2 Kg 151.99 151.99 151.99 - KCl Kg 33.36 33.36 33.36 - NaCl (S) Kg 301.92 94.35 94.35 - NaCl (C) Kg - 207.57 207.57 Sum 1,396.01 846.01 638.44 207.57

In the above-described Table 2, the primary mother liquor having a mineral content of Y3 (same as Z1 in Table 3) is re-supplied to the first crystal tank 300 and then heated to evaporate and discharge moisture. The mineral component of the second sodium chloride magma in the state after the evaporation is removed is shown in Table 3 above, and shows the same mineral content as Z2.

At this time, the sodium chloride crystals are precipitated as the water is evaporated and discharged, it can be seen that the sodium chloride crystals are formed 207.57KG.

The second sodium chloride magma is supplied to the centrifuge 620 via the second buffer tank 610, and through the centrifuge 620, sodium chloride is secondarily separated from the second sodium chloride magma, and the separated sodium chloride is separated. The salt is manufactured through the mixer 630, the rotary dryer 640, and the like, and the secondary mother liquor from which sodium chloride is separated secondary is supplied to the mineral control tank 520.

At this time, the mineral component of the secondary mother liquor is the same as Z3 in Table 3.

As described above, the continuous salt production facility using the deep sea water according to the present invention can collect the crystals of the calcium sulfate component having a very low solubility in the preparation of the salt in a liquid state, which is easy to be lost during the process. Most of the calcium component can be recovered, and the first and second sedimentation separation is performed while sequentially passing through the crystal tank and the sedimentation tank 440, so that calcium sulfate crystals can be easily separated.

In the present invention, it is possible to effectively supply salts and use of energy in the production of salts, such that the primary mother liquor from which sodium chloride is first separated from sodium chloride magma is re-supplied to the crystal tank, and the water is evaporated and centrifuged again. It can be made, a continuous treatment process in the process of preparing the salt from the concentrated water, it is possible to quickly process a large amount of deep sea water.

100: input tank 110: supply pipe
210: first concentration tank 211: first circulation pipe
220: second concentration tank 221: second circulation pipe
230: 3rd concentration tank 231: 3rd circulation pipe
240: auxiliary heater 250: first heater
260: second heater 270: third heater
300: the first buffer tank
410: the first crystal tank 420: the second crystal tank
430: the third crystal tank
440, 450, 460: sedimentation tank
510: calcium adjustment tank 520: mineral adjustment tank
610: second buffer tank 620: centrifuge
630: mixer 640: rotary dryer
650: Conveyor

Claims (12)

An input tank into which deep seawater is subjected to reverse osmosis and concentrated water is input and stored;
A concentrated tank supplied with the concentrated water from the input tank and configured to evaporate and separate water in the concentrated water;
A heater configured to heat the concentrated water supplied to the concentration tank by heat exchange;
A first buffer tank configured to supply and store calcium magma obtained by evaporating and separating water from the concentrated water from the concentrated tank;
The calcium magma is supplied and stored from the first buffer tank, and the primary sedimentation separation of the calcium sulfate crystal is performed from the calcium magma to be divided into a first supernatant and a first sublayer, and crystals are formed to evaporate and separate moisture. Tank;
A calcium adjustment tank in which all or part of the first lower layer liquid discharged from the crystal tank is stored;
A second buffer tank configured to supply and store a first sodium chloride magma obtained by evaporating and separating water from the crystal tank in a state excluding the first lower layer liquid discharged from the calcium magma to the calcium adjusting tank; And
And a centrifuge configured to separate sodium chloride from the first sodium chloride magma supplied from the second buffer tank.
The first lower layer liquid is supplied from the crystal tank, and the sedimentation tank is separated into a second supernatant and a second lower layer liquid by the secondary sedimentation of calcium sulfate crystals;
The sedimentation tank, the second lower layer liquid is discharged to the calcium adjustment tank, the second supernatant is re-supply to the crystal tank, continuous salt production equipment by the deep sea water.
delete The method of claim 1,
From the centrifuge, the primary mother liquor made by primary separation of sodium chloride from the first sodium chloride magma is fed back to the crystal tank,
From the crystal tank, a second sodium chloride magma formed by evaporation and separation of water from the primary mother liquor is supplied to the second buffer tank,
In the centrifuge, the continuous salt production facility by the deep sea water, characterized in that the sodium chloride is separated from the second sodium chloride magma.
The method of claim 3, wherein
And a mineral adjusting tank supplied with a secondary mother liquor from which the second chloride is separated from the second sodium chloride magma from the centrifugal separator.
The method of claim 4, wherein
A mixer in which minerals are mixed with sodium chloride separated by the centrifuge; And
A continuous salt-producing facility by deep sea water, further comprising; a rotary dryer which receives sodium chloride mixed with minerals from the mixer and continuously transports the same, and is configured to dry moisture.
The method of claim 5, wherein
The salt is supplied to the mixer, continuous salt production facility by the deep sea water, characterized in that from the mineral adjustment tank.
The method of claim 4, wherein
The crystal tank is divided into a first crystal tank, a second crystal tank and a third crystal tank,
The first salt tank, the second crystal tank and the third crystal tank is a continuous salt production facility by the deep sea water, characterized in that used sequentially.
The method of claim 1,
The concentration tank,
A first concentrated tank in which the concentrated water is supplied from the input tank, and a first concentrated water formed by evaporating and separating water from the concentrated water is formed;
A second enrichment tank configured to supply the first enrichment water from the first enrichment tank, and to form a second enrichment water formed by evaporation and separation of water in the first enrichment water; And
The second concentrated water is supplied from the second concentrated tank, and water is evaporated and separated from the second concentrated water to form the calcium magma, and a third concentrated tank for supplying the calcium magma to the first buffer tank. Continuous salt production equipment by deep sea water, characterized in that consisting of;
The method of claim 8,
Each of the first concentration tank, the second concentration tank, and the third concentration tank has a first circulation pipe, a second circulation pipe, and a third circulation pipe each configured to circulate discharge and inflow of the solution supplied therein, respectively. Become,
The heater is continuous salt production by deep sea water, characterized in that the first heater, the second circulation tube and the third circulation tube formed on the first heater, the second heater and the third heater, respectively, characterized in that equipment.
The method of claim 9,
The heated steam for heat exchange is supplied to the heater,
Water vapor is supplied to pass through the first heater, the second heater and the third heater in sequence so that the heat exchange is made to the continuous salt production facility by the deep sea water.
11. The method of claim 10,
Water evaporated in the first concentration tank is connected to be supplied to the second heater,
Water evaporated from the second concentration tank is a continuous salt production facility by the deep sea water, characterized in that connected to be supplied to the third heater.
The method of claim 11,
A supply pipe through which the concentrated water is supplied to the first concentration tank is formed from the input tank,
On the supply pipe, an auxiliary heater is formed so that the concentrated water supplied to the first concentration tank is heated by heat exchange,
Water evaporated from the third concentration tank is a continuous salt production facility by the deep sea water, characterized in that connected to be supplied to the auxiliary heater.

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