KR20140054901A - Electrolysis apparatus with salt water concentrating process - Google Patents

Abstract

The present invention relates to an electrolysis apparatus including a salt water concentrating process. An object of the present invention provides a salt water electrolysis apparatus without performing an anode water regeneration process based on a complex structure by arranging a vacuum evaporation concentrator in a diaphragm seal type electrolysis apparatus so that salt water, which is supplied from an anode water storage tank to an anode chamber, undergoes vacuum concentration and is supplied into an oversaturated salt water or saturated salt water. The present invention includes a diaphragm seal type electrolytic bath that is divided into an anode chamber and a cathode chamber with a diaphragm interposed therebetween so as to electrolyze supplied salt water and soft water; an anode water storage tank in which the saturated salt water that is supplied to the anode chamber of the electrolytic bath is stored; a vacuum evaporation concentrator that produces the oversaturated salt water through the vacuum evaporation concentration of the saturated salt water which is supplied from a salt water supply means or produces the saturated salt water through the vacuum evaporation concentration of the saturated salt water which is supplied from the salt water supply means and low-concentration salt water which reacts in an electrolytic bath anode chamber, and supplies the salt water to the anode water storage tank; and the salt water supply means that supplies the saturated salt water to at least one of the vacuum evaporation concentrator and the anode water storage tank.

Description

[0001] The present invention relates to an electrolysis apparatus with a salt water concentration process,

The present invention relates to an electrolytic apparatus having a brine concentration process, and more particularly, to an electrolytic apparatus having a salt water concentration process, and more particularly, to an electrolytic apparatus having a salt water concentration process, To an electrolytic apparatus including a concentrator.

Generally, in the case of an electrolytic apparatus using a diaphragm type electrolytic cell, an electrolysis reaction is performed in a galvanic cell electrolytic cell composed of an anode chamber and a cathode chamber in which an anode and a cathode are located, and a diaphragm partitioning the two anode chambers. At this time, the diaphragm generally uses a cation exchange membrane.

In the electrolytic reaction of salt water using the diaphragm type electrolytic cell, salt water of high concentration is supplied to the cathode chamber and soft water is supplied to the cathode and anode of the anode chamber, and chlorine ion (Cl ^- ) of salt water (NaCl) This is converted to chlorine gas (Cl ₂ ) through the anode electrode reaction and sodium ions (Na ⁺ ) to the cathode chamber through the diaphragm. The cathode chamber in the soft water (H ₂ O) through the electrode reaction in the cathode hydrogen gas (H ₂₎ and hydroxide ions (OH ^-) is converted to hydroxyl ions (OH ^-) is a sodium ion (Na ⁺⁾ passed from the anode chamber and It forms equilibrium to form caustic soda (NaOH).

(Anode chamber) Anode reaction 2Cl ^- → Cl ₂ + 2e ^-

(Cathode chamber) Mass transfer in the anode chamber (+) Na ⁺ + H ₂ O (-)

Cathode reaction 2H ₂ O + 2e ^- → H ₂ + 2OH ^-

2Na ⁺ + 2OH ^- ? 2NaOH

At this time, the brine of the anolyte discharged to the outlet of the anode chamber becomes lower in the concentration of the brine due to the electrode reaction at the anode and the mass transfer through the diaphragm. That is, when sodium ions move through the diaphragm, some of the water is also moved to the cathode chamber, and some of the water is decomposed through the anodic reaction. However, the water consumption is lower than the consumption of sodium chloride in the overall reaction.

In the brine electrolysis process using a membrane type electrolytic cell, chlorine gas (Cl ₂ ) produced in an anode chamber, caustic soda (NaOH) produced in a cathode chamber and sodium hypochlorite (NaOCl) produced through an external gas- (HCl) which is produced by reacting hydrogen in the cathode chamber with chlorine gas in the anode chamber.

In this case, as shown in FIG. 8, the anode and cathode are generally provided with a separate anode water reservoir and an anode water reservoir, respectively, to produce anode and cathode water in a circulating manner.

In this case, the anode water storage tank receives saturated brine to maintain the brine concentration after the reaction, and the anode water storage tank supplies the soft water.

As described above, the anode water storage tank has a larger amount of sodium chloride in the brine in terms of the material balance, so that the concentration of the brine in the anode water storage tank is continuously diluted. As a result, the ion conductivity of the anode chamber is lowered, And the lifetime of the anode is lowered.

Accordingly, it is general that some of the anode water is regenerated through the anode water regeneration process and reused as the anode water reservoir through the saturated brine supply unit.

However, in this anode water regeneration step, hydrochloric acid (HCl) is added in a first step to keep the pH below 2 to recover and recover the chlorine remaining in the anode water, and the step of adding the neutralizing agent to the residual chlorine (Cl ₂ ) and comprises a step, the step of maintaining a weak alkaline naejineun again to neutral pH by injecting sodium hydroxide (NaOH) in three steps to 7 to 10 with the step of ^reducing-the chloride ion (Cl). The neutralizing agent used here is a chlorine reducing agent such as NaHSO ₃ .

However, the conventional structure having the above-described anode water regeneration process has a problem in that the apparatus becomes complicated. That is, each of the chemical tank, the infusion pump, and the reaction tank is required as the three chemicals are used in the third step. (HCl), neutralizing agent, and caustic soda (NaOH) are used, which makes it difficult to maintain and maintain the equipment and increase the maintenance cost. And a problem due to the concentration of chemicals in the supply of saturated brine due to the use of a neutralizing agent and the like.

Korean Patent Registration Registration No. 10-1079470 (Oct. 27, 2011)

SUMMARY OF THE INVENTION In order to solve the above problems, an object of the present invention is to provide a membrane-type electrolytic apparatus having a reduced-pressure evaporator, a concentrated anode water recovery process by concentrating the salt water supplied to the anode water reservoir under reduced pressure, And to provide a brine electrolysis apparatus that does not require the use of the apparatus.

Another object of the present invention is to provide a membrane-type electrolytic apparatus which comprises a reduced-pressure evaporator, and electrolytic reaction is performed in an electrolytic bath, followed by concentrating the anode water of the anode water storage tank in which the cathode water having a diluted concentration is circulated, And which does not require a regeneration process for the anode water of the structure.

It is a further object of the present invention to provide a membrane-type electrolytic apparatus in which a decompression evaporator and an anode water storage tank are integrally provided, electrolyzed in an electrolytic cell, and a cathode water in a cathode water storage tank, And supplying a saturated brine to the brine electrolysis apparatus.

According to an aspect of the present invention, there is provided a membrane-type electrolytic cell for electrolyzing brine and soft water;

A cathode water storage tank storing saturated brine supplied to the anode chamber of the electrolytic bath;

A reduced pressure evaporator concentrator for concentrating the saturated brine supplied from the brine supply means by evaporation under reduced pressure and supplying the saturated brine to the anode water storage tank in a supersaturated brine state;

And a brine supply means for supplying the brine to at least one of the decompression evaporator, the decompression evaporator, and the anode water storage tank.

In a preferred embodiment of the present invention, the reduced-

A concentrating tank for supplying and storing the saturated brine from the brine supplying means and supplying the concentrated supersaturated brine to the anode water storing tank;

A vacuum pump for concentrating the brine of the thickening tank under reduced pressure and supplying the vaporized water vapor to the salt storage tank of the salt supply means through the steam discharge pipe;

A brine circulation pump for supplying the brine in the concentration tank to the spray nozzle in the concentration tank through the saturated brine circulation pipe and circulating the brine;

A spray nozzle for spraying the brine from the brine circulation pump at an upper portion of the water level to increase the specific surface area of the brine to increase the evaporation amount;

And a demister disposed on an upper portion of the spray nozzle installed in the concentration tank so that moisture does not flow into the vacuum pump.

In a preferred embodiment of the present invention, the concentration tank is located above the anode water storage tank, and the supersaturated brine stored by the gravity is supplied to the anode water storage tank through opening and closing of the supersaturated brine discharge valve on the discharge pipe located below, And supply supersaturated brine to the anode water reservoir through the pump.

The present invention is a preferred embodiment, and the lower portion of the thickener may be cone-shaped.

According to a preferred embodiment of the present invention, the branch circulation pipe is branched at one point of the saturated brine circulation pipe and circulated to the concentrating tank directly in accordance with the opening of the saturated brine circulation valve.

In one preferred embodiment of the present invention, the anode water heat exchanger is installed at one point of the saturated brine circulation pipe, and can be configured to exchange heat with the high temperature anode water circulating from the anode chamber of the electrolytic cell through the low concentration brine circulation pipe to the anode water reservoir have.

The present invention is a preferred embodiment of the present invention in which the steam discharge pipe is provided with a salt reservoir of the brine supplying means after the heat pipe condensed at the front end or the rear end of the vacuum pump passes through the inside of the thickener so that the heat of the steam condensate is exchanged with saturated brine in the concentration tank .

In a preferred embodiment of the present invention, the reduced-

A saturated salt water is supplied from the brine supply means and stored, and the concentrated supersaturated brine is supplied to the anode water storage tank, the lower portion is formed into a cone-shaped double jacket shape, A condensing tank in which condensed water supplied through the steam discharge pipe of the condensing water heat exchanger is stored;

A vacuum pump for concentrating the brine of the thickening tank under reduced pressure and supplying the vaporized water vapor to the salt storage tank of the salt supply means through the steam discharge pipe;

A brine circulation pump for supplying the brine in the concentration tank to the spray nozzle in the concentration tank through the saturated brine circulation pipe and circulating the brine;

A spray nozzle for spraying the brine from the brine circulation pump at an upper portion of the water level to increase the specific surface area of the brine to increase the evaporation amount;

And a demister disposed on an upper portion of the spray nozzle installed in the concentration tank so that moisture does not flow into the vacuum pump.

In a preferred embodiment of the present invention, the supersaturated brine stored in the thickening tank may be configured to supply a brine supply pump installed on the supersaturated brine discharge pipe connected to the positive electrode water reservoir according to the opening of the supersaturated brine discharge valve.

In a preferred embodiment of the present invention, the branch circulation pipe is branched at one point of the saturated brine circulation pipe to supply supersaturated brine to the cone-shaped inner thickening tank when the supersaturated brine is supplied to the spray nozzle, The brine branch pipe may be branched to supply saturated brine to the anode water reservoir upon opening of the saturated brine branch valve.

In a preferred embodiment of the present invention, when the branched circulation pipe is branched to supply supersaturated brine to the cone-shaped inner thickening tank, the crystal salt which flows in the tangential direction of the thickening tank is circulated so as to be easily gathered to the center can do.

The present invention is a preferred embodiment of the present invention in which the steam discharge pipe is stored in an external condensate heat exchanger in the form of a double jacket in the lower part of the condenser so that the heat of the steam condensed at the front end or the rear end of the vacuum pump is exchanged with saturated brine in the condenser, To the salt storage tank of the brine supply means.

In a preferred embodiment of the present invention, a cathode water heat exchanger is installed at one point of the saturated brine circulation pipe, and is heat-exchanged with a high temperature anode water circulated from the anode chamber of the electrolytic cell through the low concentration brine circulation pipe to the anode water reservoir, The temperature of the supersaturated brine can be increased.

The present invention also provides, in another embodiment,

A membrane type electrolytic cell for electrolyzing brine and soft water;

A cathode water storage tank for storing anode water supplied to the anode chamber of the electrolyzer;

A saturated brine supplied from the brine supply means and a low pressure brine concentrated in the electrolytic bath anion chamber by evaporating the low concentration brine under reduced pressure to obtain a saturated brine and supplying the brine to the bipolar water storage tank;

And a brine supply means for supplying a saturated brine to the decompression evaporator. The electrolytic apparatus includes a brine concentration step.

In a preferred embodiment of the present invention, the reduced-

A concentrating tank for storing the saturated brine supplied from the brine supplying means and the low concentration brine reacted in the electrolysis tank anode chamber and supplying the concentrated brine to the anode water storage tank through the brine circulation pump;

A vacuum pump for concentrating the brine of the concentration tank under reduced pressure and discharging the vaporized water vapor through a steam discharge pipe;

A brine circulation pump for circulating the salt water in the thickener tank through a saturated brine circulation pipe and supplying the saturated brine to the anode water storage tank through a saturated brine branch pipe;

A cathode water transfer pump for supplying a low-concentration brine stored in the anode water storage tank to a spray nozzle of the thickener through an anode water circulation pipe;

A spray nozzle for spraying the low concentration brine transferred from the anode water transfer pump at the upper portion of the brine in the concentration tank to increase the specific surface area of the brine to increase the evaporation amount;

And a demister disposed on an upper portion of the spray nozzle installed in the concentration tank so that moisture does not flow into the vacuum pump.

The present invention is a preferred embodiment of the present invention in which the steam discharge pipe is provided with a salt reservoir of the brine supplying means after the heat pipe condensed at the front end or the rear end of the vacuum pump passes through the inside of the thickener so that the heat of the steam condensate is exchanged with saturated brine in the concentration tank .

According to a preferred embodiment of the present invention, the condensed water discharged through the steam discharge pipe may be discharged to the outside through a water separator or may be supplied to the salt storage tank of the brine supplying means, and the dry air may be discharged into the atmosphere, To be transferred.

According to another aspect of the present invention, there is provided a membrane-type electrolytic cell comprising: a membrane-type electrolytic cell which is divided into an anode chamber and a cathode chamber via a diaphragm and electrolyzes the supplied brine and soft water;

A cathode water storage tank storing saturated brine supplied to the anode chamber of the electrolytic bath;

The saturated salt water supplied from the brine supplying means and the low-concentration brine reacted in the electrolysis tank anode chamber are concentrated by evaporation under reduced pressure to obtain saturated brine and supplied to the anode water storage tank integrally formed at the lower portion. A concentrator;

And a brine supply means for supplying a saturated brine to the decompression evaporation concentrator.

According to a preferred embodiment of the present invention, the reduced-pressure evaporator concentrator integrally coupled to the upper portion of the anode water storage tank comprises: an upper concentrator for storing saturated brine supplied from brine supply means and low-concentration brine reacted in the electrolysis cell anode chamber;

A vacuum pump for concentrating and concentrating the brine of the thickening tank under reduced pressure and discharging the evaporated water vapor through a steam discharge pipe;

A spray nozzle for spraying the low concentration brine supplied from the anode chamber of the electrolytic cell at the upper portion of the brine in the upper concentration tank to increase the specific surface area of the brine to increase the evaporation amount;

And a demister disposed on an upper portion of the spray nozzle installed in the concentration tank so that moisture does not flow into the vacuum pump.

The present invention is a preferred embodiment of the present invention, in which the steam discharge pipe is constructed such that a heat pipe for heat exchange with the saturated brine in the anode water storage tank in which the heat of steam condensed at the front end or the rear end of the vacuum pump is integrally combined with the bottom of the thickener, As shown in Fig.

In a preferred embodiment of the present invention, the water vapor discharged through the steam discharge pipe is condensed and then discharged to the outside through a water separator or supplied to the salt storage tank of the brine supplying means, and the dry air containing Cl ₂ gas is supplied to the gas- It can be configured to be supplied to a separate processing apparatus according to the chemical product to be produced.

According to a preferred embodiment of the present invention, a vacuum release valve is provided at the upper end of the thickener to adjust the vacuum depressurization state of the thickener as necessary.

As described above, according to the present invention, the membrane-type electrolytic apparatus is provided with the decompression evaporator, and the brine supplied to the anode water storage tank is concentrated by evaporation under reduced pressure to supply the brine in the supersaturated brine state, However,

The electrolytic reaction is carried out in the electrolytic cell, and the anode water of the anode water storage tank in which the cathode water having the diluted concentration is circulated is evaporated under reduced pressure to be supplied in the saturated salt water state by providing the decompression evaporation concentrator in the membrane- The balance of material balance between sodium chloride and water at the same time,

In addition, the membrane-type electrolytic apparatus is provided with a decompression evaporator and an anode water electrolytic cell integrally, thereby simplifying the apparatus. After the electrolytic reaction in the electrolytic cell, the anode water of the anode water storage tank, In addition, it is possible to adjust the material balance of sodium chloride and water in the electrolytic reaction at any time,

In order to increase the salt concentration of the anode water stored in the anode water storage tank after electrolysis in the anode chamber according to the supply of supersaturated brine or saturated brine as described above, the conventional HCl injection apparatus, NaHSO ₃ injection apparatus, NaOH injection apparatus, PH adjustment tank, and desalting tank, so that a complicated anode water recovery process is not required. Therefore, the device is simple in structure, safe and safe to use because it does not use hazardous chemicals,

In addition, it is a useful invention having an advantage that heat exchange of waste heat generated in a reduced pressure evaporation and concentration process is performed to increase the efficiency of evaporation of reduced pressure, and energy consumption is reduced.

1 is a schematic view showing an electrolytic apparatus provided with a reduced-pressure evaporator for producing a supersaturated brine according to an embodiment of the present invention,
FIG. 2 is a schematic view showing an electrolytic apparatus having a reduced-pressure evaporator for producing a saturated brine according to another embodiment of the present invention,
FIG. 3A is a general view showing an electrolytic apparatus having a reduced-pressure evaporator according to a first embodiment of the present invention for producing supersaturated brine,
FIG. 3B is an enlarged schematic view of the main part of FIG. 3A,
FIG. 4A is an overall view showing an electrolytic apparatus having a reduced-pressure evaporator according to a second embodiment of the present invention for producing supersaturated brine,
FIG. 4B is an enlarged schematic view of the main part of FIG. 4A,
FIG. 5A is an overall view showing an electrolytic apparatus having a reduced-pressure evaporator according to a third embodiment of the present invention for producing supersaturated brine,
FIG. 5B is an enlarged schematic view of the main part of FIG. 5A,
6A is an overall view showing an electrolytic apparatus having a reduced pressure evaporator according to a fourth embodiment of the present invention for producing saturated brine,
FIG. 6B is an enlarged schematic view of the main part of FIG. 6A,
FIG. 7A is an overall view showing an electrolytic apparatus having a reduced-pressure evaporator according to a fifth embodiment of the present invention for producing saturated brine,
FIG. 7B is an enlarged schematic view of the main part of FIG. 7A,
FIG. 8 is a view showing an example of an electrolytic apparatus having a cathode water regeneration process using a conventional chemical agent.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the following description of the present invention, a detailed description of known functions and configurations incorporated herein will be omitted when it may make the subject matter of the present invention rather unclear.

FIG. 1 is a schematic view showing an electrolytic apparatus having a reduced-pressure evaporator for producing a supersaturated brine according to an embodiment of the present invention, and FIG. 2 is a schematic view of a decompression evaporator for producing a saturated brine according to another embodiment of the present invention. FIG. 2 is a schematic view showing an electrolytic apparatus provided therein.

The constitution of the present invention mainly includes a diaphragm type electrolytic cell which is divided into an anode chamber and a cathode chamber with a diaphragm interposed therebetween and electrolyzes the supplied brine and soft water; A cathode water storage tank storing saturated brine supplied to the anode chamber of the electrolytic bath; The saturated brine supplied from the brine supply means is concentrated by evaporation under reduced pressure to produce supersaturated brine, or the saturated brine supplied from the brine supply means and the low concentration brine reacted in the electrolysis chamber are evaporated under reduced pressure to be saturated brine, A pressure reducing evaporator for supplying the reduced pressure; And a brine supply means for supplying saturated brine to at least one of the decompression evaporator, the decompression evaporator, and the anode water storage tank.

The reason why the decompression evaporator is constructed is that when the electrolytic reaction is continuously performed in the diaphragm type electrolytic cell, the concentration of the anode water, that is, the brine, supplied to the anode chamber is lowered. When the concentration of the diluted salt water is lowered to the supersaturated concentration or the brine Supply and replenishment. Such a configuration is a device for increasing the concentration of salt by evaporating water vapor, and it does not require the steps of desalting, neutralizing, and pH adjusting the chlorine discharged from the anode water storage tank as in the prior art, The electrolytic apparatus can be constructed simply and safely.

As shown in the drawing, a cathode water storage tank for supplying soft water, which is the cathode water, is connected to the cathode chamber of the diaphragm type electrolytic cell, and chlorine generated in the anode chamber and caustic soda (NaOH) generated in the cathode chamber are supplied And a gas-liquid contact reaction tank for producing sodium hypochlorite (NaOCl) by a gas-liquid contact reaction can be provided.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

In the above, the saturated brine is about 25 to 30 wt% of brine, and the supersaturated brine is about 40 to 65 wt% of brine.

The principle of the vacuum evaporation concentrator is that according to the general thermodynamic law, 1.67 m ³ is converted into water vapor when a heat of 540 kcal is applied to pure water of 1 kg and 100 ° C. under 1 atm, and 1 kg and 32 ° C. When the amount of heat of 580 kcal is applied to pure water, 28.7 m ³ is converted into water vapor, so that even at a lower temperature and a lower calorific value, it can be converted into more water vapor. The device is used to concentrate the saturated brine or anode water under reduced pressure, Means a device for increasing the concentration of salt water.

It is also preferred that the reduced pressure evaporator includes means for increasing the surface area of the solution to increase the amount of evaporation.

The present invention as described above is divided into two types of embodiments according to whether the reduced pressure evaporator is made of supersaturated brine or saturated brine, and the basic structure thereof will be described below.

First, referring to FIG. 1, the present invention includes a diaphragm type electrolytic cell 1 for electrolyzing salt water and soft water, which are divided into an anode chamber and a cathode chamber with a diaphragm interposed therebetween; A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath; A decompression evaporator 3 for concentrating the saturated brine supplied from the brine supply means by evaporation under reduced pressure and supplying the saturated brine to the anode water storage tank in a supersaturated brine state; And a brine supply means (4) for supplying saturated brine to at least one of the decompression evaporator, the decompression evaporator, and the anode water storage tank.

As shown in the drawing, a cathode water storage tank for supplying soft water, which is the cathode water, is connected to the cathode chamber of the diaphragm type electrolytic cell, and chlorine generated in the anode chamber and caustic soda (NaOH) generated in the cathode chamber are supplied And a gas-liquid contact reaction tank for producing sodium hypochlorite (NaOCl) by a gas-liquid contact reaction can be provided.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

In the above, the saturated brine is about 25 to 30 wt% of brine, and the supersaturated brine is about 40 to 65 wt% of brine.

The brine supply means 4 is provided with a salt storage tank 41 in which raw water is supplied to and stored in the stored salt and a first brine supply pump 43 which supplies water stored in the salt storage tank to remove impurities in brine, And a brine purifier 42 for supplying the brine purifier 42 to the water storage tank 2.

Referring to FIG. 2, the present invention includes a diaphragm electrolytic cell 1 for electrolyzing salt water and soft water separated into an anode chamber and a cathode chamber with a diaphragm interposed therebetween; A cathode water storage tank (2) storing anode water supplied to an anode chamber of the electrolytic bath; (3) for concentrating the saturated brine supplied from the brine supply means and the low-concentration brine reacted in the electrolysis tank anode chamber into a saturated brine to be supplied to the bipolar water storage tank; And brine supply means (4) for supplying saturated brine to the reduced pressure evaporation concentrator.

As shown in the drawing, a cathode water storage tank 5 for supplying soft water, which is the cathode water, is connected to the cathode chamber of the diaphragm type electrolytic cell, and chlorine generated in the anode chamber and caustic soda generated in the cathode chamber And a gas-liquid contact reaction tank 6 for producing sodium hypochlorite (NaOCl) by gas-liquid contact reaction.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

The brine supply means 4 is provided with a salt storage tank 41 in which raw water is supplied to and stored in the stored salt and a first brine supply pump 43 which supplies water stored in the salt storage tank to remove impurities in brine, And a brine purifier 42 for supplying the brine purifier 42 to the water storage tank 2.

The reduced-pressure evaporator 3 is installed inside or outside of the anode water storage tank 2 to evaporate water vapor in the low-concentration anode water and is re-injected into the anode water storage tank 2 to be maintained as a saturated brine, .

The low-concentration anode water circulated in the above refers to a brine having a concentration of brine lower than 25% after electrolysis.

Further, the salt water consumed in the anode chamber is configured to be additionally supplied through the brine supply means.

The evaporated water vapor may be separately drained or configured to be reused in brine supply means for producing brine.

The specific configurations of the above-described two embodiments of the present invention will be described below with reference to the respective embodiments.

FIG. 3A is an overall configuration diagram showing an electrolytic apparatus having a reduced-pressure evaporator according to a first embodiment of the present invention for producing supersaturated brine, and FIG. 3B is an enlarged view of a main portion of FIG.

As shown in FIG. 1, the entire structure according to the first embodiment of the present invention basically comprises a diaphragm type electrolytic cell 1 for electrolyzing salt water and soft water, which are divided into an anode chamber and a cathode chamber with a diaphragm interposed therebetween, Wow; A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath; A decompression evaporator 3 for concentrating the saturated brine supplied from the brine supply means by evaporation under reduced pressure and supplying the saturated brine to the anode water storage tank in a supersaturated brine state; And a brine supply means (4) for supplying saturated brine to at least one of the decompression evaporator, the decompression evaporator, and the anode water storage tank.

As shown in the figure, the cathode chamber of the diaphragm type electrolytic cell is provided with a cathode water reservoir 5 for supplying cathode water, and chlorine generated in the anode chamber and caustic soda (NaOH) generated in the cathode chamber, And a gas-liquid contact reaction tank 6 for producing sodium hypochlorite (NaOCl) by gas-liquid contact reaction.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

Hereinafter, the present embodiment will be described in detail with reference to a reduced-pressure evaporator 3 for concentrating the salt water supplied to the anode compartment of the electrolytic cell.

The reduced-pressure evaporation concentrator 3 receives saturated brine from the brine supply means 4 and stores the concentrated brine into the supernatant brine discharge pipe P8 through the opening and closing of the supersaturated brine discharge valve V1, A condensing tank (31) for supplying the water to the storage tank (2);

A vacuum pump 32 for concentrating the brine of the thickening tank under reduced pressure and for supplying the vaporized water vapor to the salt storage tank 41 of the salt supply means 4 through the steam discharge pipe P1;

A brine circulation pump 33 for supplying the brine in the thickening tank 31 to the spray nozzle in the concentration tank through the saturated brine circulation pipe P2 and circulating the same;

A spray nozzle 35 for spraying the brine from the brine circulation pump at an upper portion of the water level to increase the specific surface area of the brine to increase the evaporation amount;

And a demister (36) provided on an upper portion of the spray nozzle (35) provided in the concentration tank so as to prevent moisture from flowing into the vacuum pump (32).

The concentration tank 31 is located at the upper part of the anode water storage tank and is connected to the anode water storage tank 2 through the opening and closing of the supersaturated brine discharge valve V1 on the supersaturated brine discharge pipe P8 located below the supersaturated brine stored by gravity .

A vacuum release valve V4 is formed at the upper end of the thickening tank 31 to release the vacuum decompression state of the thickening tank if necessary.

The lower part of the thickening tank is cone-shaped and smoothly discharged to the anode water storage tank 2 through the saturated brine discharge valve V1, and the salt is well accumulated on the lower side.

A branch circulation pipe P3 is branched at one point of the saturated brine circulation pipe P2. The branch circulation pipe P3 is configured to circulate directly to the concentration tank 31 without passing through the spray nozzle 35 as the saturated brine circulation valve V2 installed on the pipe is opened.

The anode water heat exchanger 37 is installed at one point of the saturated brine circulation pipe P2 and is connected to the anode water reservoir 2 through the low concentration brine circulation pipe P4 in the anode chamber of the electrolyzer, (About 18 wt% of low-concentration brine) of about 80 DEG C). As a result, the temperature of the supersaturated brine supplied to the spray nozzle increases, thereby increasing the evaporation amount of the water vapor.

In addition, the water vapor discharge pipe (P1) is installed such that the heat of the steam condensed at the front end or the rear end of the vacuum pump (32) exchanges heat with the saturated brine in the concentration tank so that one pipe passes through the pipe into the concentration tank (31) (NaCl) of the solid crystal by supplying the condensed water downward to the salt storage tank 41 of the brine supply means 4. [

The saturated brine supplied to the anode water storage tank 2 and the concentration tank 31 supplies the saturated brine supplied from the brine purifier 42 of the brine supply means 4 through the brine supply pipe P5. For this, a saturated brine supply valve V3 is provided on the piping supplied to the anode water storage tank 2 so that the supply can be controlled.

The saturated brine stored in the anode water storage tank 2 is supplied to the anode chamber 11 of the diaphragm type electrolytic cell 1 through the anode water supply pipe P6.

The operation according to the above-described embodiment will be described below.

The water level of the anode water storage tank 2 is set to L to H. When the water level drops to L, the saturated brine supply valve (V3) is opened and saturated brine is introduced until the water level reaches the H position.

When the brine concentration of the inflow of the anode chamber 11 of the diaphragm type electrolytic cell 1 falls below the lower limit set value, the supersaturated brine discharge valve V1 and the supersaturated brine circulation valve V2 are opened and concentrated, And when the concentration reaches the upper limit value, the supersaturated brine discharge valve V1 and the supersaturated brine circulation valve V2 are closed. For reference, the lower and upper limits of the concentration are used by the ion conductivity sensor (sensor indicated as CON in the figure) before entering the anode chamber of the electrolysis cell.

When the supersaturated brine discharge valve V1 and the supersaturated brine circulation valve V2 are opened, the vacuum pump 32 is stopped and the vacuum release valve V4 is opened to release the vacuum in the concentration tank 31, To prevent backflow of dilute brine.

Conversely, when the supersaturated brine discharge valve V1 and the supersaturated brine circulation valve V2 are closed, the vacuum pump 32 is activated simultaneously with the vacuum release valve V4 being closed and the constant concentration of salt water in the concentrate tank 31 The concentration process is continued until the supersaturated state is reached.

The water level of the thickening tank (31) is adjusted by using a water level valve or an automatic valve which can be controlled constantly.

The brine in the thickening tank 31 is circulated using the brine circulation pump 33 and the spray nozzle 35 is used at the upper part of the water level to raise the specific surface area of the liquid (brine) to increase the evaporation amount. At this time, the demister (36) prevents moisture from flowing into the vacuum pump (32) through the upper part of the thickener (31).

The anode water heat exchanger 37 is installed in the saturated brine circulation pipe P2 provided with the brine circulation pump 33 so that the anode chamber 11 of the diaphragm type electrolyzer 1 is filled with the brine, Which is a low-concentration brine, entering the anode water storage tank 2 from the anode water.

The steam pump 31 discharges the heat while condensing the steam at the front end or the rear end of the vacuum pump 32. In order to recover the heat to the condenser 31, The condensed water whose temperature has dropped after the heat exchange enters the salt (NaCl) storage tank 41 of the brine supply means 4 and is configured to be reused to dissolve the salt (NaCl) of the solid crystal.

FIG. 4A is an overall configuration diagram showing an electrolytic apparatus having a reduced pressure evaporator according to a second embodiment of the present invention for producing supersaturated brine, and FIG. 4B is an enlarged schematic view of the main part of FIG. 4A.

As shown in FIG. 1, the overall structure of the electrolytic cell 1 according to the second embodiment of the present invention is basically divided into an anode chamber and a cathode chamber with a diaphragm interposed therebetween, Wow; A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath; A decompression evaporator 3 for concentrating the saturated brine supplied from the brine supply means by evaporation under reduced pressure and supplying the saturated brine to the anode water storage tank in a supersaturated brine state; And a brine supply means (4) for supplying saturated brine to at least one of the decompression evaporator, the decompression evaporator, and the anode water storage tank.

As shown in the figure, the cathode chamber of the diaphragm type electrolytic cell is provided with a cathode water reservoir 5 for supplying cathode water, and chlorine generated in the anode chamber and caustic soda (NaOH) generated in the cathode chamber, And a gas-liquid contact reaction tank 6 for producing sodium hypochlorite (NaOCl) by gas-liquid contact reaction.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

Hereinafter, the present embodiment will be described in detail with reference to a reduced-pressure evaporator 3 for concentrating the salt water supplied to the anode compartment of the electrolytic cell.

The reduced-pressure evaporation concentrator 3 receives and stores saturated brine from the brine supply means 4 and supplies the concentrated brine to the anode water reservoir (not shown) through the supersaturated brine discharge pipe P8 and the supersaturated brine discharge valve V1 2, and the lower part of the jacket is constructed in the form of a double jacket, the concentration of the saturated brine in the cone-shaped double jacket is concentrated, and the external condensate water heat exchange tank 38 of the double jacket is supplied with water vapor A condensing tank (31) connected to the discharge pipe (P1) and configured to recover the condensation heat and then discharge through the discharge steam discharge pipe (P1) for discharge again;

A vacuum pump 32 for concentrating the brine of the thickening tank under reduced pressure and for supplying the vaporized water vapor to the salt storage tank 41 of the salt supply means 4 through the steam discharge pipe P1;

A brine circulation pump 33 for supplying the brine in the thickening tank 31 to the spray nozzle in the concentration tank through the saturated brine circulation pipe P2 and circulating the same;

A spray nozzle 35 for spraying the brine from the brine circulation pump at an upper portion of the water level to increase the specific surface area of the brine to increase the evaporation amount;

A demister (36) provided at an upper portion of the spray nozzle (35) provided in the concentration tank so that moisture does not flow into the vacuum pump (32);

And a brine supply pump 34 installed between the supersaturated brine discharge pipe P8 and the supersaturated brine discharge valve V1 to supply supersaturated brine to the bipolar reservoir.

A vacuum release valve V4 is formed at the upper end of the thickening tank 31 to release the vacuum decompression state of the thickening tank if necessary.

The brine circulation pipe P3 is branched at one point of the saturated brine circulation pipe P2 to supply supersaturated brine to the cone-shaped inner thickening tank portion formed at the lower portion of the thickening tank when supersaturated brine is supplied to the spray nozzle, The branch is configured to supply a saturated brine to the anode water reservoir (2) if the saturated brine branch pipe (P7) is branched and the anode water reservoir level is low.

The steam discharge pipe P1 is connected to an external condensate heat exchanger 38 in the form of a double jacket at the bottom of the condenser 31 so that the heat of the steam condensed at the front end or the rear end of the vacuum pump 32 can be exchanged with saturated brine in the condenser And then the condensed water whose temperature has been lowered is supplied to the salt storage tank 41 of the brine supply means 4 to be reused for dissolving the salt (NaCl) of the solid crystal.

The saturated brine supplied to the thickening tank 31 supplies the saturated brine supplied from the brine purifier 42 of the brine supply means 4 through the brine supply pipe P5.

The saturated brine stored in the anode water storage tank 2 is supplied to the anode chamber 11 of the diaphragm type electrolytic cell 1 through the anode water supply pipe P6.

The operation according to the above-described embodiment will be described below.

The water level of the anode water storage tank 2 is set to L to H. When the water level drops to L, the saturated brine branch valve (V5) is opened and saturated brine is introduced until it becomes H.

The supernatant brine discharge valve V1 is opened and the brine supply pump 34 is activated when the brine concentration of the inflow of the anode chamber 11 of the diaphragm type electrolytic cell 1 falls below the lower limit set value, And when the upper limit is reached, the brine supply pump 34 is stopped and the supersaturated brine discharge valve V1 is closed.

A brine circulation pump 33 and a brine supply pump 34 are attached to the concentrating tank 31 having a double jacket-shaped lower structure having a conical bottom portion and a condensate water heat exchange tank 38, The brine supply pump 34 is used to supply supersaturated brine to the positive electrode water storage tank 2 as described above and the brine circulation pump 33 is used to control the water level of the positive electrode water reservoir 2 and the circulation of the brine in the concentration tank 31 To be sprayed through a spray nozzle at the top.

The reason for spraying through the spray nozzle is to widen the specific surface area of the liquid to increase the evaporation efficiency. The circulation (P3) of the concentrated liquid flows in the tangential direction of the thickening tank (31), so that the brine circulates in the circulating flow and precipitates in a supersaturated state The salt (NaCl) of crystals plays a role in centering by the difference in specific gravity. The centralized salt (NaCl) is transferred to the anode water storage tank 2 through the brine supply pump 34 in a supersaturated state when the brine concentration of the influent flowing into the anode chamber 11 of the diaphragm electrolytic cell 1 drops .

The reason why the thickener 31 is manufactured in the form of a double jacket to recover the condensation heat of the steam condensed at the front end or the rear end of the vacuum pump 32 is that the inside is concentrated and the outside is connected to the front end or the rear end of the vacuum pump 32 And serves as a heat exchanger for recovering the heat of condensation. If the thickener 31 is not a double jacket, the heat exchanger may be inserted into the thickener 31.

The condensed water enters the salt reservoir 41 of the brine supply means 4 and is reused to dissolve the salt of solid crystals (NaCl).

FIG. 5A is an overall configuration diagram showing an electrolytic apparatus having a reduced-pressure evaporator according to a third embodiment of the present invention for producing supersaturated brine, and FIG. 5B is an enlarged schematic view of the main part of FIG. 5A.

As shown in FIG. 1, the entire structure of the electrolytic cell 1 according to the third embodiment of the present invention is basically divided into an anode chamber and a cathode chamber with a diaphragm interposed therebetween, Wow; A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath; A decompression evaporator 3 for concentrating the saturated brine supplied from the brine supply means by evaporation under reduced pressure and supplying the saturated brine to the anode water storage tank in a supersaturated brine state; And a brine supply means (4) for supplying saturated brine to at least one of the decompression evaporator, the decompression evaporator, and the anode water storage tank.

As shown in the figure, the cathode chamber of the diaphragm type electrolytic cell is provided with a cathode water reservoir 5 for supplying cathode water, and chlorine generated in the anode chamber and caustic soda (NaOH) generated in the cathode chamber, And a gas-liquid contact reaction tank 6 for producing sodium hypochlorite (NaOCl) by gas-liquid contact reaction.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

Hereinafter, the present embodiment will be described in detail with reference to a reduced-pressure evaporator 3 for concentrating the salt water supplied to the anode compartment of the electrolytic cell.

The reduced-pressure evaporation concentrator 3 receives and stores saturated brine from the brine supply means 4 and supplies the concentrated brine to the anode water reservoir (not shown) through the supersaturated brine discharge pipe P8 and the supersaturated brine discharge valve V1 2, and the lower part of the jacket is constructed in the form of a double jacket, the concentration of the saturated brine in the cone-shaped double jacket is concentrated, and the external condensate water heat exchange tank 38 of the double jacket is supplied with water vapor A condensing tank (31) connected to the discharge pipe (P1) and configured to recover the condensation heat and then discharge through the discharge steam discharge pipe (P1) for discharge again;

A vacuum pump 32 for concentrating the brine of the thickening tank under reduced pressure and for supplying the vaporized water vapor to the salt storage tank 41 of the salt supply means 4 through the steam discharge pipe P1;

A brine circulation pump 33 for supplying the brine in the thickening tank 31 to the spray nozzle in the concentration tank through the saturated brine circulation pipe P2 and circulating the same;

A spray nozzle 35 for spraying the brine from the brine circulation pump at an upper portion of the water level to increase the specific surface area of the brine to increase the evaporation amount;

A demister (36) provided at an upper portion of the spray nozzle (35) provided in the concentration tank so that moisture does not flow into the vacuum pump (32);

And a brine supply pump 34 installed between the supersaturated brine discharge pipe P8 and the supersaturated brine discharge valve V1 to supply supersaturated brine or saturated brine to the bipolar water storage tank.

A vacuum release valve V4 is formed at the upper end of the thickening tank 31 to release the vacuum decompression state of the thickening tank if necessary.

The brine circulation pipe P3 is branched at one point of the saturated brine circulation pipe P2 to supply supersaturated brine to the cone-shaped inner thickening tank portion formed at the lower portion of the thickening tank when supersaturated brine is supplied to the spray nozzle, A branch of saturated brine branch P7 is branched to supply a saturated brine to the anode water reservoir 2 for regulating the level of the anode water reservoir 2.

The anode water heat exchanger 37 is installed at one point of the saturated brine circulation pipe P 2 and is connected to the anode water reservoir 2 through the low concentration brine circulation pipe P 4 in the anode chamber of the electrolyzer, (About 18 wt% of low-concentration brine) of a predetermined temperature (e.g. As a result, the temperature of the supersaturated brine supplied to the spray nozzle increases, thereby increasing the evaporation amount of the water vapor.

The steam discharge pipe P1 is connected to an external condensate heat exchanger 38 in the form of a double jacket at the bottom of the condenser 31 so that the heat of the steam condensed at the front end or the rear end of the vacuum pump 32 can be exchanged with saturated brine in the condenser And then the condensed water whose temperature has been lowered is supplied to the salt storage tank 41 of the brine supply means 4 to be reused for dissolving the salt (NaCl) of the solid crystal.

The saturated brine supplied to the thickening tank 31 supplies the saturated brine supplied from the brine purifier 42 of the brine supply means 4 through the brine supply pipe P5.

The saturated brine stored in the anode water storage tank 2 is supplied to the anode chamber 11 of the diaphragm type electrolytic cell 1 through the anode water supply pipe P6.

The operation according to the above-described embodiment will be described below.

The water level of the anode water storage tank 2 is set to L to H. When the water level drops to L, the saturated brine branch valve (V5) is opened and saturated brine is introduced until it becomes H.

The supernatant brine discharge valve V1 is opened and the brine supply pump 34 is activated when the brine concentration of the inflow of the anode chamber 11 of the diaphragm type electrolytic cell 1 falls below the lower limit set value, And when the upper limit is reached, the brine supply pump 34 is stopped and the supersaturated brine discharge valve V1 is closed.

A brine circulation pump 33 and a brine supply pump 34 are attached to the concentrating tank 31 having a double jacket-shaped lower structure having a conical bottom portion and a condensate water heat exchange tank 38, The brine supply pump 34 is used to supply supersaturated brine to the positive electrode water storage tank 2 as described above and the brine circulation pump 33 is used to control the water level of the positive electrode water reservoir 2 and the circulation of the brine in the concentration tank 31 To be sprayed through a spray nozzle at the top.

The reason for spraying through the spray nozzle is to widen the specific surface area of the liquid to increase the evaporation efficiency. The circulation of the concentrated liquid flows in the tangential direction of the thickening tank 31, so that the salt water circulates in the inside, (NaCl) is centered by the difference in specific gravity. The centralized salt (NaCl) is transferred to the anode water storage tank 2 through the brine supply pump 34 in a supersaturated state when the brine concentration of the influent flowing into the anode chamber 11 of the diaphragm electrolytic cell 1 drops .

The reason why the thickener 31 is manufactured in the form of a double jacket to recover the condensation heat of the steam condensed at the front end or the rear end of the vacuum pump 32 is that the inside is concentrated and the outside is connected to the rear end of the vacuum pump 32, As a heat exchanger. If the thickener 31 is not a double jacket, the heat exchanger may be inserted into the thickener 31.

The condensed water enters the salt reservoir 41 of the brine supply means 4 and is reused to dissolve the salt of solid crystals (NaCl).

A positive electrode water heat exchanger 37 is provided at one point of the saturated brine circulation pipe P2 at the rear end of the brine circulation pump 33 so that the positive electrode chamber 11 of the diaphragm type electrolytic cell 1 is connected to the positive electrode water reservoir 2 Recover the high-temperature heat before entering.

FIG. 6A is an overall configuration diagram showing an electrolytic apparatus having a reduced-pressure evaporator according to a fourth embodiment of the present invention for producing saturated brine, and FIG. 6B is an enlarged schematic view of the main part of FIG. 6A.

As shown in the figure, the overall structure according to the fourth embodiment of the present invention is basically the same as that shown in FIG. 2 except that the separator is divided into the anode chamber 11 and the cathode chamber with the diaphragm interposed therebetween, An electrolytic bath (1); A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath; (3) for concentrating the saturated brine supplied from the brine supply means and the low-concentration brine reacted in the electrolysis tank anode chamber into a saturated brine to be supplied to the bipolar water storage tank; And brine supply means (4) for supplying saturated brine to the reduced pressure evaporator.

As shown in the figure, the cathode chamber of the diaphragm type electrolytic cell is provided with a cathode water reservoir 5 for supplying cathode water, and chlorine generated in the anode chamber and caustic soda (NaOH) generated in the cathode chamber, And a gas-liquid contact reaction tank 6 for producing sodium hypochlorite (NaOCl) by gas-liquid contact reaction.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

Hereinafter, the present embodiment will be described in detail with reference to a reduced-pressure evaporator 3 for concentrating the salt water supplied to the anode compartment of the electrolytic cell.

The reduced-pressure evaporation concentrator 3 stores the saturated brine supplied from the brine supply means 4 and the low-concentration brine reacted in the electrolysis tank anode chamber and supplies the concentrated brine to the anode water storage tank 33 via the brine circulation pump 33, A condensing tank 31 for supplying the condensed water to the evaporator;

A vacuum pump 32 for concentrating the brine of the thickening tank under reduced pressure, and discharging the vaporized water vapor through the steam discharge pipe P1;

The brine in the thickening tank 31 is supplied into the thickening tank through the saturated brine circulation pipe P2 and is circulated. At the same time, saturated brine is supplied to the anode water storage tank through the saturated brine branch pipe P7 provided with the check valve V6 A brine circulation pump 33 for circulating the water;

A positive electrode water transfer pump 39 for supplying low-concentration brine stored in the positive electrode water storage tank 2 to the spray nozzle 35 of the concentration tank through the positive water circulation pipe P9;

A spray nozzle 35 for spraying the low concentration brine transferred by the anode water transfer pump 39 at an upper portion of the brine in the concentration tank to increase the specific surface area of the brine to increase the evaporation amount;

And a demister (36) provided on an upper portion of the spray nozzle (35) provided in the concentration tank so as to prevent moisture from flowing into the vacuum pump (32).

Further, the steam discharge pipe (P1) is provided with a pipeline to the inside of the concentrating tank (31) so that the heat of the steam condensed at the front end or the rear end of the vacuum pump (32) exchanges heat with the saturated brine in the concentration tank, Is supplied to the salt storage tank (41) of the tank (4) to be reused to dissolve the salt (NaCl) of the solid crystal.

The condensed water discharged through the steam discharge pipe P1 may be discharged to the outside through the water separator 7 or may be supplied to the salt storage tank of the brine supply means and the dry air may be discharged to the atmosphere or transferred to a separate treatment device Can be configured.

The saturated brine supplied to the thickening tank 31 supplies the saturated brine supplied from the brine purifier 42 of the brine supply means 4 through the brine supply pipe P5.

The saturated brine stored in the anode water storage tank 2 is supplied to the anode chamber 11 of the diaphragm type electrolytic cell 1 through the anode water supply pipe P6.

The operation according to the above-described embodiment will be described below.

The saline solution can be supplied to the anode water storage tank 2 through the brine circulation pump 33 while maintaining a constant level of salted water and the predetermined amount can be recirculated to the concentration tank 31.

And the brine stored in the anode water storage tank 2 by the anode water transfer pump 39 is sprayed through the spray nozzle 35 at the top of the thickener tank via the anode water circulation pipe P9.

A demister 36 is attached to the upper portion of the condenser 31 so that moisture does not flow into the vacuum pump 32. The vacuum pump 32 sucks the supersaturated moisturizer at the uppermost portion of the condenser 31, And the heat exchanged with the concentrate at the subsequent stage. The condensed liquid after the heat exchange can be discharged to the outside through the water separator (7) or supplied to the salt storage tank of the brine supply means, and the dry air can be discharged to the atmosphere or transferred to a separate treatment device.

The water level of the thickening tank 31 is controlled to a certain level using a four-level valve or an automatic valve, and the saturated brine purified through the brine purifier 42 is introduced into the concentration tank 31.

FIG. 7A is an overall configuration diagram showing an electrolytic apparatus having a reduced-pressure evaporator according to a fifth embodiment of the present invention for producing saturated brine, and FIG. 7B is an enlarged view of a main portion of FIG. 7A.

As shown in the figure, the entire structure according to the fifth embodiment of the present invention is a modified embodiment of FIG. 2, in which the saltwater is divided into an anode chamber 11 and a cathode chamber with a diaphragm interposed therebetween, An electrolytic bath (1); A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath; The saturated salt water supplied from the brine supplying means and the low concentration brine reacted in the electrolytic bath anion chamber are concentrated by evaporation under reduced pressure to be made into a saturated brine so as to be supplied to the anode water storage tank integrally formed at the lower part, (3); And brine supply means (4) for supplying saturated brine to the reduced pressure evaporator.

As shown in the figure, the cathode chamber of the diaphragm type electrolytic cell is provided with a cathode water reservoir 5 for supplying cathode water, and chlorine generated in the anode chamber and caustic soda (NaOH) generated in the cathode chamber, And a gas-liquid contact reaction tank 6 for producing sodium hypochlorite (NaOCl) by gas-liquid contact reaction.

The equipment at the downstream end of the electrolytic cell may be separately configured for the purpose of producing chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl), which are chemical products produced by other electrolytic devices.

Hereinafter, the present embodiment will be described in detail with reference to a reduced-pressure evaporator 3 for concentrating the salt water supplied to the anode compartment of the electrolytic cell.

The reduced-pressure evaporator 3 integrally coupled to the upper portion of the anode water storage tank 2 is connected to a saturated brine supplied from the brine supply means 4 and an upper concentrated tank 31 for storing the low- )Wow;

And concentrated under reduced pressure to evaporate the salt water in the concentration tank, the evaporated water vapor is water vapor discharge pipe via a water separator (7) is installed on (P1) discharged from or fed into the salt reservoir in the salt water supply means, and Articles containing Cl ₂ gas A vacuum pump 32 for supplying air to a separate treatment device according to the chemical product to be produced, such as the gas-liquid contact tank 6 illustrated in the drawing;

A spray nozzle 35 for spraying the low concentration brine supplied from the anode chamber of the electrolytic cell at an upper portion of the brine in the upper concentration tank to raise the specific surface area of the brine to increase the evaporation amount;

And a demister (36) provided on an upper portion of the spray nozzle (35) provided in the concentration tank so as to prevent moisture from flowing into the vacuum pump (32).

The water vapor discharge pipe P1 is connected to a cathode water storage tank (not shown) so that heat of steam condensed at the front end or the rear end of the vacuum pump 32 is heat-exchanged with saturated brine in the anode water storage tank 2, 2) Install piping inside.

The saturated brine supplied to the thickening tank 31 supplies the saturated brine supplied from the brine purifier 42 of the brine supply means 4 through the brine supply pipe P5.

The saturated brine stored in the anode water storage tank 2 is supplied to the anode chamber 11 of the diaphragm type electrolytic cell 1 through the anode water supply pipe P6.

The operation according to the above-described embodiment will be described below.

Thereby integrating the evaporation-concentrating tank 31 and the anode water storage tank 2 together. A demister 36 is attached to the upper part of the anode water storage tank 2 so as to prevent water from flowing into the vacuum pump 32. The vacuum pump 32 sucks the supersaturated humidifier and Cl ₂ gas from the upper part of the concentration tank 31, Exchanged with the saturated brine of the anode water storage tank 2 integrally connected to the lower portion of the thickening tank 31 at the front end or the rear end of the pumping pump 32 through the water vapor discharge pipe P1 connected to the pump 32. [

The condensed water after the heat exchange is discharged to the outside through the water separator (7) or supplied to the salt storage tank of the brine supply means, and the dry air including the Cl ₂ gas is supplied to the chemical And is supplied to a separate processing apparatus according to the product.

The water level of the integrated anode water storage tank 2 is controlled to a certain water level by using a four-level valve or an automatic valve, and is introduced into the anode water storage tank 2 in which the purified brine is integrated through the brine purifier 42.

It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined in the appended claims and their equivalents. Of course, such modifications are within the scope of the claims.

Description of the Related Art
(1): diaphragm type electrolytic cell (2): anode water storage tank
(3): vacuum evaporation concentrator (4): brine supply means
(5): cathode water storage tank (6): gas-liquid contact tank
(7): water separator (11): anode chamber
(31): Enrichment tank (32): Vacuum pump
(33): Saltwater circulation pump (34): Brine supply pump
(35): Spray nozzle (36): Demister
(37): anode water heat exchanger (38): condensate water heat exchanger
(39): anode water transfer pump (41): salt storage tank
(42): brine purifier (43): first brine supply pump
(P1): steam discharge pipe (P2): saturated brine circulation pipe
(P3): Branch circulation piping (P4): Low concentration brine circulation piping
(P5): saturated brine supply pipe (P6): anode water supply pipe
(P7): saturated brine branch piping (P8): supersaturated brine discharge piping
(P9): anode water circulation pipe (V1): supersaturated brine discharge valve
(V2): Supersaturated brine circulation valve (V3): Saturated brine supply valve
(V4): vacuum release valve (V5): saturated brine branch valve
(V6): Check valve

Claims (22)

A membrane type electrolyzer (1) for electrolyzing brine and soft water;
A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath;
A decompression evaporator 3 for concentrating the saturated brine supplied from the brine supply means by evaporation under reduced pressure and supplying the saturated brine to the anode water storage tank in a supersaturated brine state;
And a brine supply means (4) for supplying saturated brine to at least one of the decompression evaporator, the decompression evaporator, and the anode water storage tank.
The method according to claim 1,
The reduced-pressure evaporator (3)
A concentrating tank 31 for receiving and storing the saturated brine from the brine supplying means 4 and supplying the concentrated supernatant brine to the anode water storage tank 2;
A vacuum pump 32 for concentrating the brine of the thickening tank under reduced pressure and for supplying the vaporized water vapor to the salt storage tank 41 of the salt supply means 4 through the steam discharge pipe P1;
A brine circulation pump 33 for supplying the brine in the thickening tank 31 to the spray nozzle in the concentration tank through the saturated brine circulation pipe P2 and circulating the same;
A spray nozzle 35 for spraying the brine from the brine circulation pump at an upper portion of the water level to increase the specific surface area of the brine to increase the evaporation amount;
And a demister (36) installed at an upper portion of the spray nozzle (35) installed in the concentration tank so as to prevent water from flowing into the vacuum pump (32).
The method of claim 2,
The concentration tank 31 is located at the upper part of the anode water storage tank and supplies supersaturated brine stored by gravity to the anode water storage tank 2 through opening and closing of the supersaturated brine discharge valve V1 on the discharge pipe P8 located below And a supercritical brine is supplied to the anode water storage tank (2) through a pump.
The method of claim 2,
Wherein the lower part of the thickening tank is formed in a cone shape.
The method of claim 2,
Wherein the brine circulation pipe P3 is branched at one point of the saturated brine circulation pipe P2 and is circulated and supplied directly to the concentration tank 31 in accordance with the opening of the saturated brine circulation valve V2 And an electrolytic device.
The method of claim 2,
A positive electrode water heat exchanger 37 is provided at one point of the saturated brine circulation pipe P 2 and a high temperature anode water circulating from the anode chamber of the electrolyzer to the anode water reservoir 2 through the low concentration brine circulation pipe P 4 Wherein the electrolytic water is subjected to heat exchange.
The method of claim 2,
The water vapor discharge pipe P1 passes through the inside of the thickener 31 so that the heat of the steam condensed at the front end or the rear end of the vacuum pump 32 can be heat-exchanged with the saturated brine in the concentration tank. And the salt water is supplied to the salt storage tank (41).
The method according to claim 1,
The reduced-pressure evaporator (3)
The saturated salt water is supplied from the brine supply means 4 and stored, and the concentrated supernatant brine is supplied to the anode water storage tank 2, A condensing tank 31 in which a condensed water heat exchanging tank 38 in which heat is exchanged to store the condensed water supplied through the steam discharging pipe P1 at the upstream or downstream of the vacuum pump 32 is formed;
A vacuum pump 32 for concentrating the brine of the thickening tank under reduced pressure and for supplying the vaporized water vapor to the salt storage tank 41 of the salt supply means 4 through the steam discharge pipe P1;
A brine circulation pump 33 for supplying the brine in the thickening tank 31 to the spray nozzle in the concentration tank through the saturated brine circulation pipe P2 and circulating the same;
A spray nozzle 35 for spraying the brine from the brine circulation pump at an upper portion of the water level to increase the specific surface area of the brine to increase the evaporation amount;
And a demister (36) installed at an upper portion of the spray nozzle (35) provided in the concentration tank so as to prevent water from flowing into the vacuum pump (32).
The method of claim 8,
Wherein the supersaturated brine stored in the thickening tank is supplied with a brine supply pump 34 installed on a supersaturated brine discharge pipe P8 connected to the positive electrode water storage tank according to the opening of the supersaturated brine discharge valve V1 .
The method of claim 8,
The brine circulation pipe P3 is branched at one point of the saturated brine circulation pipe P2 to supply supersaturated brine to the cone-shaped inner thickening tank when the supersaturated brine is supplied to the spray nozzle, Wherein the piping (P7) is branched to supply saturated brine to the anode water storage tank (2) in accordance with the opening of the saturated brine branch valve (V5).
Claim 10
The branch circulation pipe P3 is branched to supply the supersaturated brine to the cone-shaped inner thickening tank portion, the crystal salt which flows in the tangential direction of the thickening tank 31 is swirled so as to be easily collected into the central portion And a brine concentration step of electrolyzing the brine.
The method of claim 8,
The water vapor discharge pipe P1 is stored in an external condensate water heat exchanger 38 formed in the form of a double jacket below the thickener 31 so that the heat of steam condensed at the front end or the rear end of the vacuum pump 32 can be exchanged with saturated brine in the thickener And the condensed water whose temperature has been lowered after the heat exchange is supplied to the salt storage tank (41) of the brine supply means (4).
The method of claim 8,
A positive electrode water heat exchanger 37 is provided at one point of the saturated brine circulation pipe P 2 and a high temperature anode water circulating from the anode chamber of the electrolyzer to the anode water reservoir 2 through the low concentration brine circulation pipe P 4 And the temperature of the supersaturated brine supplied to the spray nozzle is increased by heat exchange.
A membrane type electrolyzer (1) for electrolyzing brine and soft water;
A cathode water storage tank (2) storing anode water supplied to an anode chamber of the electrolytic bath;
(3) for concentrating the saturated brine supplied from the brine supply means and the low-concentration brine reacted in the electrolysis tank anode chamber into a saturated brine to be supplied to the bipolar water storage tank;
And a brine supply means (4) for supplying a saturated brine to the reduced pressure evaporator.
15. The method of claim 14,
The reduced-pressure evaporator (3)
A concentrating tank 31 for storing the saturated brine supplied from the brine supplying means 4 and the low concentration brine reacted in the electrolysis tank anode chamber and supplying the concentrated brine to the anode water storage tank through the brine circulation pump 33;
A vacuum pump 32 for concentrating the brine of the thickening tank under reduced pressure, and discharging the vaporized water vapor through the steam discharge pipe P1;
A brine circulation pump 33 for circulating brine in the thickening tank 31 through a saturated brine circulation pipe P 2 and circulating the same and supplying saturated brine to the brine storage tank P 7 through a saturated brine branch pipe P 7, Wow;
A positive electrode water transfer pump 39 for supplying low-concentration brine stored in the positive electrode water storage tank 2 to the spray nozzle 35 of the concentration tank through the positive water circulation pipe P9;
A spray nozzle 35 for spraying the low concentration brine transferred by the anode water transfer pump 39 at an upper portion of the brine in the concentration tank to increase the specific surface area of the brine to increase the evaporation amount;
And a demister (36) installed at an upper portion of the spray nozzle (35) installed in the concentration tank so as to prevent water from flowing into the vacuum pump (32).
16. The method of claim 15,
The water vapor discharge pipe P1 passes through the inside of the thickener 31 so that the heat of the steam condensed at the front end or the rear end of the vacuum pump 32 can be heat-exchanged with the saturated brine in the concentration tank. And the salt water is supplied to the salt storage tank (41).
16. The method of claim 15,
The condensed water discharged through the steam discharge pipe P1 may be discharged to the outside through the water separator 7 or may be supplied to the salt storage tank of the brine supply means and the dry air may be discharged to the atmosphere or transferred to a separate treatment device And the electrolytic water is supplied to the electrolytic cell.
A diaphragm type electrolytic cell (1) which is divided into an anode chamber (11) and a cathode chamber via a diaphragm and electrolyzes the supplied brine and soft water;
A cathode water storage tank (2) storing saturated brine supplied to the anode chamber of the electrolytic bath;
The saturated salt water supplied from the brine supplying means and the low concentration brine reacted in the electrolytic bath anion chamber are concentrated by evaporation under reduced pressure to be made into a saturated brine so as to be supplied to the anode water storage tank integrally formed at the lower part, (3);
And a brine supply means (4) for supplying a saturated brine to the reduced pressure evaporator.
19. The method of claim 18,
The reduced-pressure evaporator 3 integrally coupled to the upper part of the anode water storage tank 2 is connected to a saturated brine supplied from the brine supply unit 4 and an upper concentrated tank 31 )Wow;
A vacuum pump 32 for concentrating and concentrating the brine of the concentration tank under reduced pressure, and discharging the vaporized water through a steam discharge pipe P1;
A spray nozzle 35 for spraying the low concentration brine supplied from the anode chamber of the electrolytic cell at an upper portion of the brine in the upper concentration tank to raise the specific surface area of the brine to increase the evaporation amount;
And a demister (36) installed at an upper portion of the spray nozzle (35) provided in the concentration tank so as to prevent water from flowing into the vacuum pump (32).
The method of claim 19,
The water vapor discharge pipe P1 is provided so that the heat of the steam condensed at the front end or the rear end of the vacuum pump 32 is heat-exchanged with the saturated brine in the anode water storage tank 2 integrally bonded to the lower portion of the thickening tank 31, Wherein the electrolytic water is passed through the inside of the anode water storage tank (2).
The method of claim 19,
The vapor discharge pipe (P1) of water vapor is then condensed and through the water separator 7 is discharged to the outside or supplied to the salt reservoir of salt water feed means, dry air is the gas-liquid contact reactor 6 containing the Cl ₂ gas discharged through the And the electrolytic water is supplied to a separate treatment device according to a chemical product to be produced.
The method of any one of claims 2, 8, 15, and 19,
Wherein a vacuum release valve (V4) is provided at an upper end of the thickening tank (31) so as to adjust a vacuum depressurization state of the concentration tank if necessary.

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