KR20180085610A - Hybrid system making fresh water and salt from sea water - Google Patents

Abstract

The present invention relates to a hybrid seawater desalination and salt production system. The system for desalination of seawater comprises: a reverse osmosis generation unit which applies a pressure to seawater to produce fresh water for a first time via reverse osmosis; a pressure booster which mixes concentrated seawater generated in the reverse osmosis generation unit with seawater to supply low-temperature concentrated seawater having appropriate pressure and flow rate; a first low-pressure evaporation production unit which comprises a first condensing chamber, a first heat exchanger, and a first evaporating chamber, to condense steam in the first condensing chamber to produce fresh water for a second time; a second low-pressure evaporation production unit which comprises a second condensing chamber, a second heat exchanger, and a second evaporating chamber, to condense steam in the second condensing chamber to produce fresh water for a third time; a fresh water collecting unit which collects fresh water produced in the reverse osmosis generation unit, the first low-pressure evaporation production unit, and the second low-pressure evaporation production unit; and a salt production unit which produces salt from concentrated seawater generated in the first low-pressure evaporation production unit and the low-pressure evaporation production unit. In particular, the first condensing room permits low-temperature concentrated seawater supplied from the pressure booster to pass through; the first heat exchanger performs heat-exchange between blue water heated in a first heater and concentrated seawater having passed through the first condensing chamber; and the first evaporating chamber receives high-temperature concentrated seawater heated in the first heat exchanger to generate steam, and delivers the generated steam to the first condensing chamber. In particular, the second condensing room permits low-temperature concentrated seawater supplied from the pressure booster to pass through; the second heat exchanger performs heat-exchange between blue water heated in a second heater and concentrated seawater having passed through the second condensing chamber; and the second evaporating chamber receives high-temperature concentrated seawater heated in the second heat exchanger to generate steam, and delivers the generated steam to the second condensing chamber.

Description

Hybrid system for desalination and salt production [

The present invention relates to a seawater desalination and salt production system, and more particularly, to a desalination and salt production system using a hybrid seawater desalination and salt production system capable of desalinating seawater by connecting a reverse osmosis system and a low pressure evaporation system in series, .

In areas where annual precipitation is very low or where there is a lack of fresh water available in coastal areas, islands, and deserts with long dry seasons, abundant seawater desalination is inevitable. In recent years, desertification has spread rapidly due to global warming and the like, and there are many regions where there is not enough fresh water available. In particular, shortage of dry water in the dry season lasting several months in the tropics is serious. Accordingly, a seawater desalination device capable of desalinating seawater has been developed and used.

As a method for producing fresh water from seawater, a high temperature evaporation method, a vacuum low temperature evaporation method, a reverse osmosis method, a freezing method, an electrolysis method and the like are used. In vacuum low pressure evaporation method, The reverse osmosis method is a method of producing fresh water by pressurizing the seawater at a high pressure of 50 to 70 bar at the reverse osmosis membrane. When the seawater is cooled below the freezing point (-1.8 ℃), the salinity in the seawater is excluded from the growth interface of the ice, and the crystals of the ice are precipitated and the salt in the concentrated seawater where the ice crystal is between the crystal surface and the crystal is separated And the electrolysis method is a method of separating and removing ions in seawater by flowing seawater through a cation exchange membrane and an anion exchange membrane alternately disposed between two electrodes.

There are a number of prior art techniques for desalinating seawater by the various desalination methods described above. However, each of the conventional seawater desalination methods has disadvantages.

Conventional high temperature evaporation method requires a large amount of energy to be evaporated by applying heat to seawater. In the low pressure evaporation method, maintenance of maintaining performance is generally difficult because seawater heating is performed inside the evaporator. In the reverse osmosis method Also, since the high-pressure pump is used, a lot of energy is consumed and there is a drawback that the pressure is high. Treatment of brines containing high concentrations of saline during the desalination process is accompanied by problems such as seawater pollution, soil contamination, and destruction of ecosystems in coastal areas, where fishermen live. It is difficult to operate seawater desalination facilities in difficult areas. In addition, in the case of salt production, current salt production can not be continuously produced throughout the year due to various environmental factors, it is difficult to obtain manpower, and it is necessary to produce manpower in a short period of time to produce salt. For example, if it does not rain or rain like summer roses, salt production is almost stopped and the quality of the salt is also a problem.

In addition to these basic problems, equipment and parts installed inside the actual seawater desalination plant were very inconvenient for maintenance and repair. Because the components contained in the seawater are in a scale state during the process of evaporation, they must be periodically exchanged or cleaned for scale removal. To solve this problem, there has been a problem that the entire facility must be disassembled or discontinued.

- Korean Patent Laid-Open No. 10-2001-0106805 (Dec. 7, 2001) " - Korean Registered Patent No. 10-0768334 (2007.10.11) "Concentration and desalination system of seawater using natural energy" - Korean Registered Patent No. 10-1541820 (Feb. 27, 201) "Non-discharge type fused composite sea water desalination device using unexploded energy" - Korean Registered Patent No. 10-1610596 (Apr. 1, 2014) "Seawater desalination device"

The object of the present invention is to provide a hybrid seawater capable of efficiently desalting a large amount of seawater and continuously producing a large amount of salt throughout the year, Desalination and salt production system.

And to provide a hybrid seawater desalination and salt production system that recycles energy that can not but be abandoned in the reverse osmosis system as cooling water required for vacuum and condensation in a low pressure low temperature evaporation system.

It is also intended to provide a hybrid seawater desalination and salt production system that can be easily replaced and repaired by continuously improving the structure and position of the demister and heat exchanger installed therein and difficult to maintain.

In addition, it provides an eco - friendly hybrid seawater desalination and salt production system that can generate solar electricity, supply electricity, and heat seawater with solar heat in areas where water is scarce.

In order to achieve the above object, there is provided a system for desalination of seawater, comprising: a reverse osmosis pressure producing unit for producing fresh water by reverse osmosis by applying pressure to seawater; A pressure booster for mixing the seawater into the concentrated seawater generated by the reverse osmosis pressure producing unit and supplying low temperature concentrated seawater having an appropriate pressure and flow rate; A first heat exchanger for exchanging heat between the concentrated condensed water supplied from the pressure booster and the concentrated condensed seawater heated by the first heater and the concentrated seawater passing through the first condenser chamber; And a first evaporation chamber for supplying heated high-temperature concentrated seawater to generate steam and deliver generated steam to the first condensation chamber, wherein the first low-pressure evaporation chamber for condensing water vapor in the first condensation chamber to produce fresh water secondarily, Production Department; A second heat exchanger for exchanging heat between the second condensing chamber through which the low temperature concentrated seawater supplied from the pressure booster passes and the concentrated seawater heated by the second heater and passing through the second condensing chamber; And a second evaporation chamber for supplying heated high-temperature concentrated seawater to generate steam and deliver generated steam to the second condensation chamber, wherein the second low-pressure evaporation chamber for condensing water vapor in the second condensation chamber to produce fresh water Production Department; A fresh water collection unit for collecting fresh water produced by the reverse osmosis production unit, the first low pressure evaporation production unit, and the second low pressure evaporation production unit; And a salt production unit for producing salt from the concentrated seawater generated in the first low pressure evaporation production unit and the second low pressure evaporation production unit.

Here, a first ejector or a second ejector, which has a venturi tube shape and through which mixed concentrated sea water supplied from the pressure booster passes, is provided at the inlet side of the first condensing chamber or the second condensing chamber, The branch pipe branching from the ejector is connected to the vacuum induction pipe in the first condensing chamber or the second condensing chamber so that the pressure inside the first condensing chamber or the second condensing chamber can be lowered.

A channel through which water vapor can pass is formed between the first condensing chamber and the first evaporation chamber or between the second condensing chamber and the second evaporation chamber, and a mesh is formed on the channel so as to pass water vapor, At least one plate-shaped demister may be provided.

In addition, the channel may be formed with a replacement opening that is open to the outside, and both sides of the replacement opening may be formed with a sliding groove for mounting the demister, or a locking protrusion that can be seated.

At this time, the demister may be composed of a multi-hole fingerboard having a plurality of holes and a stunnet attached to the multi-hole fingerboard.

According to the present invention having the above-described configuration, since a large amount of seawater is desalinated through various stages by a fusion method using reverse osmosis and low-pressure evaporation methods, the desalination efficiency is improved and productivity is improved. It is advantageous to continuously produce a large amount of salt without any restriction.

In addition, since energy dissipated in the reverse osmosis system can be recycled as low-pressure evaporation system and cooling water required for vacuum and condensation, energy is saved.

In addition, it has a demister structure that can be replaced from the outside, so it can be replaced and detached, washed and reused, which is advantageous for maintenance and repair.

Also, by separating the heat exchanger installed inside the evaporator chamber from the outside, the maintenance and repair of the heat exchanger can be easily performed, and continuous operation without interruption can be achieved, thereby increasing the production amount.

In addition, it is eco-friendly because it generates solar energy as natural energy in a region where water is scarce, supplies electricity, and seawater is heated by solar heat.

And it is industrially excellent because it is a technology that can be continuously installed in a conventional salt tank and continuously produce a large amount of salt.

BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic diagram illustrating a hybrid seawater desalination and salt production system in accordance with an embodiment of the present invention.
FIG. 2 is a structural view showing the main part of the first low-pressure evaporation production section of the present invention shown in FIG. 1; FIG.
3 is an exploded perspective view showing the internal structure of the channel and demister of the present invention shown in FIG. 2;

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.

For a better understanding of the present invention, the description with reference to the drawings is not intended to limit the scope of the present invention. In the following description, a detailed description of related arts will be omitted when it is determined that the gist of the present invention may be unnecessarily blurred.

In the present invention, 'concentrated water' refers to seawater whose relative salinity is increased as a by-product generated in the process of desalinating general seawater.

1 is a schematic diagram illustrating a hybrid seawater desalination and salt production system in accordance with an embodiment of the present invention.

The present invention relates to a system capable of producing fresh water (drinking water) from seawater and simultaneously producing a large amount of salt. Referring to the drawings, the reverse osmosis pressure producing unit 200, the pressure booster 300, A second low pressure evaporation production unit 500, a fountain collection unit 600, and a salt production unit 700. [

First, the reverse osmosis pressure producing unit 200 will be described.

The reverse osmosis pressure production unit 200 receives the seawater and performs a process of producing fresh water by the reverse osmosis method.

The seawater supply to the reverse osmosis pressure production unit 200 includes a seawater supply unit 100 consisting of an intake pump 110 for pumping seawater from the sea and a seawater storage tank 120 for storing seawater pumped by the intake pump 110 . At this time, it is preferable that the seawater storage tank 120 and the piping to which the seawater is conveyed in the present invention are made of a material resistant to corrosion or a corrosion-resistant coating is applied to the inside thereof, and heat insulation treatment may be performed to prevent heat exchange with the outside .

The seawater is supplied to the reverse osmosis pressure producing unit 200 through the pretreatment filter 220. The pretreatment filter 220 removes fine sand, microorganisms, solid substances and the like in advance to maintain the life and performance of the membrane filter 230. The pretreatment filter 220 uses a physical method and an electric sterilization method in parallel, Are also pre-processed in parallel.

The pretreated seawater drives the low pressure pump at the front end of the pretreatment facility and the high pressure pump at the downstream end to pass the high pressure seawater to the membrane filter 230 to produce about 20 to 30% And transmits it to the receiver (600). For reference, the discharge pressure of the high-pressure pump 240 is about 60 bar.

The remaining seawater that is not desalinated in the reverse osmosis pressure producing unit 200, that is, 70 to 75% of concentrated seawater is drained and sent to a pressure booster 300 to be described later. Since the concentrated seawater contains high-pressure energy, it is not discarded but is lowered to an appropriate pressure through a pressure booster 300 described later, and is then discharged to the first low-pressure evaporation production unit 400 and the second low- It can be saved without energy being thrown away.

Next, the pressure booster 300 lowers the pressure and mixes the high-pressure concentrated seawater generated and drained from the reverse osmosis pressure production part 200 and the seawater separately supplied from the seawater supply part 100 to increase the flow rate, 1 low-pressure evaporation production unit 400 and the second low-pressure evaporation production unit 500.

Specifically, the pressure of the seawater is reduced to about 6 to 9 bar while the flow rate of the seawater is increased through the pressure booster 300, and thus the low pressure is induced in the first low pressure evaporative production unit 400 and used to facilitate condensation.

Generally, the structure of the pressure booster is a known matter, so a detailed description thereof will be omitted.

Next, referring to FIG. 2, the first low-pressure evaporative production unit, which is a main core of the present invention, will be described in detail. FIG. 2 is a structural view showing the main part of the first low-pressure evaporation production section of the present invention shown in FIG. 1. FIG.

As described above, the concentrated seawater mixed with the high-pressure and low-temperature seawater supplied from the pressure booster 300 is secondarily produced in the first low-pressure evaporative production unit 400.

The first low pressure steam generator 400 includes a first condenser chamber 410, a first evaporator chamber 420, a first ejector 430, a first concentrated seawater tank 440, a first heat exchanger 450 ), And a first heater 460.

The first evaporation chamber 420 is a space for inducing the evaporation of the concentrated seawater and the first condensation chamber 410 is a space where water vapor evaporated in the first evaporation chamber 420 is condensed and desalinated. As shown in the figure, the first evaporation chamber 420 has a lower end and the first condensation chamber 410 is located on the upper side.

The first evaporation chamber 420 receives the heated high-temperature concentrated seawater from the first heat exchanger 450. At the lower end of the first evaporation chamber (420), the concentrated seawater which has not been evaporated through the concentrated seawater discharge port (422) is discharged. At this time, a heating band 470 heated by electric heating may be further attached to the outer surface of the first evaporation chamber 420 to further activate the evaporation by heating the first evaporation chamber 420.

The first condensing chamber 410 is disposed on the upper side of the first evaporating chamber 420 and is formed between the first evaporating chamber 420 and the first condensing chamber 410 in a passage- The channel C is formed. A partition 411 may be provided on one side of the channel C so that the channel C is formed.

A demister (412) may be installed on the channel (C). 3 is an exploded perspective view showing the internal structure of the channel and the demister of the present invention shown in FIG.

The demister 412 may have a plate shape in which a plurality of holes are formed in a structure that filters the salt contained in the water vapor. Or a net or a mesh having a plurality of stencils formed therein. Preferably, one or more demisters 412 are stacked to enhance the filtering function.

In the present invention, the demister 412 may have a structure that can be easily mounted and separated so as to be easily replaced. This is because, in the case of the demister 412, the scale is fixed on the surface for a long time. Calcium carbonate (CaCO ₃ ) is mainly used for the scale, because when the scale is accumulated, the evaporation efficiency is lowered and the desalination efficiency is lowered. Therefore, the demister must be replaced or detached to be cleanable.

For this purpose, as shown in the drawing, a replacement port 413 for inserting or removing the demister 412 in a direction blocking the channel C may be formed. The replacing tool 413 may be provided with fastening means for fixing a lid (not shown) having a shape with one side thereof being open and being hermetically sealed.

Here, a sliding groove may be formed on both sides of the interior of the replacement opening 413 to allow the demister 412 to be inserted or removed. Or a stopping jaw for seating the demister may be formed. However, the structure capable of replacing the demister is not limited to this, and can be variously implemented.

Referring to the enlarged portion of FIG. 3, the demister 412 may be composed of a porous substrate 412a and a stent 412b. The porous backing plate 412a has a flat plate shape in which a plurality of holes are formed to support the stainless steel net 412b. In addition, the stent 412b may be formed by densely woven wire, or alternatively may have a plurality of mesh holes. The water vapor passes through but can filter out the contained salts.

The salinity of the concentrated seawater may be adjusted by adjusting the number of the demisters 412 mounted.

Meanwhile, a first ejector 430 is provided at one side of the first condensing chamber 410.

The first ejector 430 has a venturi tube shape in which the flow path is narrowed to increase the flow velocity. The first ejector 430 is connected to the pressure booster 300, and the low-temperature concentrated seawater supplied from the pressure booster 300 flows at a high speed by the pressure. As the water passes through the first ejector 430, the seawater further flows into the first condensing chamber 410 and moves along the curved condensing pipe 433 provided in the first condensing chamber 410, And is discharged again to the outside of the first condensing chamber (410).

At this time, a branch pipe 431 branching outward is formed at a point where the flow path of the first ejector 430 is narrowed. The branch pipe 431 is connected to a vacuum induction pipe (not shown) provided in the first condenser chamber 410 432). Accordingly, since the pressure of the first ejector 430 is reduced at a point where the flow path of the first ejector 430 is narrowed, air in the first condenser chamber 410 is discharged through the vacuum induction pipe 432, The pressure in the first evaporator chamber 410 and the first evaporator chamber 420 is drastically lowered.

As the pressure is lowered, the evaporation of seawater in the first evaporation chamber 420 is further activated, thereby improving the desalination efficiency. The water condensed in the condensation pipe 433 is liquefied and condensed by the low-temperature concentrated seawater flowing through the condensation pipe 433.

The fresh water discharge port 414 is formed in the first condensing chamber 410 to discharge the fresh water produced by the condensation and the fresh water discharge port 414 is connected to the fresh water collection part 600 to collect the fresh water secondarily .

For reference, the first evaporation chamber 420 and the first condensation chamber 410 have a structure in which heat insulation is adhered to minimize heat loss.

Meanwhile, the seawater discharged from the first condensing chamber (410) is used to condense steam while passing through the condensing pipe (433), and is then sent to and stored in a separate first concentrated seawater tank (440).

The first heat exchanger 450 exchanges heat between the water heated to about 60-80 ° C. by the first heater 460 and the concentrated seawater (about 15 ° C.) supplied from the first concentrated seawater tank 440, The seawater is heated to about 45 ° C or higher and supplied through the concentrated seawater inlet 421 of the first evaporation chamber 420.

Also, the first heater 460 may use electric energy, but it is preferable to heat the first heater 460 using solar heat in the present invention. Most of the regions lacking actual water are lacking electricity, so solar heating is suitable. The solar heating method is well known in the art and will not be described in detail.

In the present invention, the first heat exchanger (450) is separately provided outside the first evaporation chamber (420), so that it is very easy to maintain and repair the heat exchanger itself, such as replacement and repair.

Next, the second low-pressure evaporation production unit 500 will be described.

The second low-pressure evaporation production unit 500 performs a process of generating fresh water from the seawater supplied from the pressure booster 300, and has a configuration that is substantially equivalent to the first low-pressure evaporation production unit 400 .

That is, the second low-pressure evaporation production unit 500 includes a second condensing chamber 510, a second evaporation chamber 520, a second ejector 530, a second concentrated seawater tank 540, a second heat exchanger 550 ), And a second heater 560.

The second condensing chamber 510 and the second evaporating chamber 520 may have the same or similar structure as the first condensing chamber 410 and the first evaporating chamber 420, respectively.

The second ejector 530 has a structure similar to that of the first ejector 430 and flows concentrated high-pressure and low-temperature concentrated seawater from the pressure booster 300 at a high speed, and the second ejector 530 The seawater further flows into the second condensing chamber 510 and moves along the curved condensing pipe 433 provided in the second condensing chamber 510 to be discharged to the outside of the second condensing chamber 510 Can be discharged.

The second concentrated seawater tank 540 is connected to the condensation pipe 433 in the second evaporation chamber 520 and stores the concentrated seawater discharged from the second condensation chamber 510 for use in steam liquefaction.

In addition, the seawater discharged from the concentrated seawater discharge port of the second evaporation chamber 520 is circulated by the seawater circulation pump and stored in the concentrated seawater collecting tank 710 automatically or manually when the concentration is set by the salinity sensor described later. In the concentrated seawater collecting tank 710, if necessary, highly concentrated seawater can be taken out and supplied to the salt tank 730 to produce salt daily.

In addition, the second heat exchanger 550 causes heat exchange between the fresh water heated to about 60-80 ° C. by the second heater 560 and the concentrated sea water supplied from the second concentrated seawater tank 540, Is heated to about 45 ° C or higher and supplied to the second evaporation chamber (520).

In addition, the second heater 560 may be a solar heat heater, which heats the circulating water circulating in the heat and heats the seawater using heat exchange by the hot plate of the titanium plate heat exchanger heated by the heated water.

A channel is formed between the second evaporation chamber (520) and the second condensation chamber (510), and a demister is replaceably mounted on the channel.

Next, the foul collection unit 600 will be described.

The dew collecting and collecting unit 600 collects and stores the fresh water produced in the reverse osmosis producing unit 200, the first low pressure evaporation producing unit 400 and the second low pressure evaporation producing unit 500, respectively.

To this end, the foul collecting and collecting unit 600 may include a first fresh water tank 610, a second fresh water tank 620, a third fresh water tank 630, and a fresh water collecting tank 640.

The first fresh water tank 610 is connected to a discharge pipe of the reverse osmosis pressure producing unit 200 to store fresh water produced primarily and sends it to the fountain collection water tank 640.

The second fresh water tank 620 is connected to a discharge pipe of the first low-pressure evaporation production unit 400 to store the secondarily produced fresh water and sends it to the fresh water collection tank 640.

The third fresh water tank 630 is connected to a discharge pipe of the second low pressure evaporation production unit 500 to store the fresh water produced in the third generation and sends it to the fountain collection water tank 640.

Here, the fresh water collecting water tank 640 is a tank for collecting and storing fresh water from the first, second and third fresh water tanks, and a sterilizing device may be provided therein, and fresh water can be supplied through the outlet.

And the fresh water of the first fresh water tank 610 is transferred to the seawater storage tank 120 by the pump to maintain the salt concentration of the seawater storage tank at a predetermined level or lower to adjust the inlet seawater pressure of the membrane filter to be 60 BAR or less .

Next, the salt production unit 700 will be described.

The salt production unit 700 may include a concentrated seawater collecting tank 710, a salinity sensor 720, and a salt tank 730.

The concentrated seawater collecting tank 710 is connected to the first concentrated seawater tank 440 and the second concentrated seawater tank 540 and collects the concentrated seawater discharged from each process. That is, it corresponds to preparation for producing salt by collecting concentrated seawater having different salinity in each step.

A salinity sensor 720 may be provided at the outlet of the concentrated seawater collecting tank 710 to measure the concentration of saline. Concentrated seawater with optimal salinity is needed to produce salt in the trough. Therefore, the concentrated saline can be delivered through the salt sensor 720 by controlling the concentration of the concentrated saline to have an appropriate salinity.

The salt trough 730 is a space where salt is produced by the evaporation of the actual concentrated sea water. Torsion 730 may be provided more than one, depending on the amount of salt required

In the present invention, as in the case where the first and second heaters heat water by the solar heat, it is preferable that the electric power generated by the solar power generator 800 is used to drive the system of the present invention. That is, all the electric-powered structures such as the opening and closing of various pumps and valves, and the like can be configured to use electricity produced by the solar power generation unit 800.

Hereinafter, the process of producing fresh water and salt from seawater according to the present invention will be described in detail.

Sea water is pumped by the intake pump 110 and stored in the seawater storage tank 120.

The seawater stored in the seawater storage tank 120 is passed through the membrane filter 230 by applying a high pressure to the high pressure pump 240 of the reverse osmosis pressure production unit 200. At this time, the fresh water produced by the reverse osmosis method is sent to the first fresh water tank 610, and the concentrated seawater as a by-product is drained and transferred to the pressure booster 300. For reference, the fresh water transferred to the first fresh water tank 610 is again sent to the fountain water tank 640 and collected.

The concentrated seawater transferred to the pressure booster 300 is mixed with the seawater supplied from the seawater storage tank 120 to be lowered to an appropriate pressure and to be concentrated into high-pressure and low-temperature concentrated seawater, And the second low-pressure evaporation production unit 500, respectively.

The concentrated high-pressure and low-temperature concentrated seawater supplied to the first low-pressure evaporation production section 400 passes through the first ejector 430 and lowers the pressure to be supplied to the first condenser 431 through the vacuum induction pipe 432 and the branch pipe 431 The pressure in the chamber 410 and the first evaporation chamber 420 is reduced to a vacuum of almost 90%.

And then passes through the condensing tube 433 to the first condensing chamber 410 and then to the first concentrated seawater tank 440. The low-temperature concentrated seawater (about 15 ° C) stored in the first concentrated seawater tank 440 is heat-exchanged with the fresh water (60 to 80 ° C) heated by the first heater and the first heat exchanger 450, (45 ° C or higher) and supplied to the first evaporation chamber 420.

The high-temperature concentrated seawater flowing into the first evaporation chamber 420 easily evaporates at a low temperature under a low-pressure environment, and evaporated water vapor moves to the first condensation chamber 410 through the channel. At this time, the salt is filtered while passing through the demister 412 mounted on the channel C, passes through only pure water vapor, and is condensed and desalinated while meeting with the condensation pipe 433 in the first condensation chamber 410.

The fresh water condensed in the first condensing chamber 410 is transferred to the second fresh water tank 620 through the fresh water discharge port 414 and then sent to the fountain water tank 640 to be collected. The concentrated seawater that has not evaporated in the first evaporation chamber (420) is circulated by the circulation pump, and then is sent to the second concentrated seawater tank (540) automatically or manually when the concentration of the concentrated seawater reaches a predetermined salt concentration or more.

Similarly, the high-pressure, low-temperature concentrated seawater supplied to the second low-pressure evaporation producing unit 500 lowers the pressure in the second condensing chamber 510 and the second evaporating chamber 520 through the second ejector 530.

And then passes through the second condensing chamber 510 through the condensing pipe 433 and is then sent to the second concentrated seawater tank 540. At this time, the concentrated seawater mixed with the concentrated seawater flowing in the first evaporation chamber (420) becomes more concentrated concentrated seawater.

The low-temperature concentrated seawater stored in the second concentrated seawater tank 540 is heat-exchanged in the second heat exchanger 550 with the fresh water (60 to 80 ° C) heated by the second heater 560, Deg.] C or more) and is supplied to the second evaporation chamber 520.

The high-temperature concentrated seawater flowing into the second evaporation chamber 520 evaporates in a low-pressure environment, and the evaporated water vapor moves to the second condensation chamber 510 through the channel C. At this time, the salt is filtered while passing through the demister 412 mounted on the channel C, passes through pure water vapor, and is condensed and desalinated while meeting the condensation pipe 433 in the second condensation chamber 510.

The fresh water condensed in the second condensing chamber 510 is transferred to the third fresh water tank 630 through the fresh water discharge port and then sent to the fountain water tank 640 to be collected. The concentrated seawater which has not evaporated in the second evaporation chamber (520) is circulated by the circulation pump, and when the concentration of the concentrated seawater reaches the predetermined salt concentration, it is automatically or manually sent to the concentrated seawater collecting tank (710) and collected.

On the other hand, the fresh water collected in the fresh water collecting tank 640 is used as drinking water, and the highly enriched seawater collected in the concentrated seawater collecting tank 710 is sent to the salt tank 730 to produce salt. At this time, it is possible to check the salinity sensor 720 and control it to become concentrated saline having necessary salinity, and to store it, and to take it out when necessary, so that it can be supplied to the salting, so that the salt can be continuously produced throughout the year.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention may be embodied in many other specific forms without departing from the spirit or essential characteristics thereof. Therefore, the scope of the present invention should not be limited to the described embodiments, but should be determined by the scope of the appended claims, as well as the appended claims.

100: Seawater supply unit
110: Intake pump 120: Seawater storage tank
200: Reverse osmosis product
210: Low pressure pump 220: Pretreatment filter
230: Membrane filter 240: High pressure pump
300: Pressure booster
400: first low pressure evaporation producing section
410: first condensing chamber 411: partition wall
412: Demister 412a: Multi-board Fingerboard
412b: stent network 413:
414: fresh water outlet
420: First evaporation chamber 421: Enriched seawater inlet
422: Concentrated seawater outlet
430: First ejector 431: Branch tube
432: vacuum induction pipe 433: condensation pipe
440: First concentrated seawater tank 450: First heat exchanger
460: first heater 470: heating band
500: second low pressure evaporation production section
510: second condensing chamber 520: second evaporation chamber
530: Second ejector 540: Second concentrated seawater tank
550: second heat exchanger 560: second heater
600: Fountain Collection
610: first fresh water tank 620: second fresh water tank
630: Third fresh water tank 640: Fountain water tank
700: Salt production unit 710: Concentrated seawater collecting tank
720: Salinity sensor 730: Torsion
800: Photovoltaic power generation part

Claims (5)

In a system for desalinating seawater,
A reverse osmosis production unit for producing fresh water by reverse osmotic pressure by applying pressure to seawater;
A pressure booster for mixing the seawater into the concentrated seawater generated by the reverse osmosis pressure producing unit and supplying low temperature concentrated seawater having an appropriate pressure and flow rate;
A first heat exchanger for exchanging heat between the concentrated condensed water supplied from the pressure booster and the concentrated condensed seawater heated by the first heater and the concentrated seawater passing through the first condenser chamber; And a first evaporation chamber for supplying heated high-temperature concentrated seawater to generate steam and deliver generated steam to the first condensation chamber, wherein the first low-pressure evaporation chamber for condensing water vapor in the first condensation chamber to produce fresh water secondarily, Production Department;
A second heat exchanger for exchanging heat between the second condensing chamber through which the low temperature concentrated seawater supplied from the pressure booster passes and the concentrated seawater heated by the second heater and passing through the second condensing chamber; And a second evaporation chamber for supplying heated high-temperature concentrated seawater to generate steam and deliver generated steam to the second condensation chamber, wherein the second low-pressure evaporation chamber for condensing water vapor in the second condensation chamber to produce fresh water Production Department;
A fresh water collection unit for collecting fresh water produced by the reverse osmosis production unit, the first low pressure evaporation production unit, and the second low pressure evaporation production unit;
And a salt production unit for producing salt from the concentrated seawater generated in the first low pressure evaporation production unit and the second low pressure evaporation production unit. The method according to claim 1,
A first ejector or a second ejector having a venturi tube shape and through which mixed concentrated sea water supplied from the pressure booster passes is provided in the first condenser chamber or the second condenser chamber, The branched branch pipe is connected to the vacuum induction pipe in the first condensation chamber or the second condensation chamber,
Wherein the pressure in the first condensing chamber or the second condensing chamber is lowered. 3. The method of claim 2,
A channel through which water vapor can pass is formed between the first condensing chamber and the first evaporation chamber or between the second condensation chamber and the second evaporation chamber, and a stainless mesh is formed on the channel so as to pass water vapor but not remove salt. Characterized in that at least one plate-shaped demister is provided for the desalination and salt production system of hybrid seawater. The method of claim 3,
Wherein the channel is provided with a replacement opening which is opened to the outside and both sides of the replacement opening are provided with a sliding groove for mounting the demister and a catching jaw which can be seated thereon. Salt production system. 5. The method of claim 4,
Wherein the demister comprises a multi-hole fingerboard on which a plurality of holes are formed, and a stainless steel net attached to the multi-hole fingerboard.

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