KR20160003350A - Electrolysis apparatus with evaporation concentrating process of salt water - Google Patents

Abstract

The present invention relates to an electrolysis apparatus having an evaporation concentration process of salt water and, more specifically, to an electrolysis apparatus which always maintains anode water, stored in an anode water circulation tank, at a set concentration of salt water by receiving the diluted anode water of the anode water circulation tank, which is stored by being circulated after an anodic reaction in an electrolyzer in order to make conductivity of the anode water supplied to the electrolyzer maintained without using a chemical drug, evaporating and concentrating the diluted anode water, and resupplying the same. The electrolysis apparatus of the present invention comprises: a membrane type electrolyzer (1) composed of an anode chamber, which electrolyzes saturated salt water circulated and supplied from the anode water circulation tank (2) between membranes, and a cathode chamber, which electrolyzes soft water circulated and supplied from a cathode water circulation tank (3); and an evaporation concentration apparatus (4) which supplies low temperature and humid air through an external air supply line into an evaporation concentration tank which receives the diluted anode water stored in the anode water circulation tank after the anodic reaction in the anode chamber, heats the same, changes the same into air in high temperature and humid steam condition, discharges the same through an air transfer line, and resupplies the concentrated anode water to the anode water circulation tank.

Description

[0001] The present invention relates to an electrolysis apparatus having an evaporation concentrate process,

More particularly, the present invention relates to an electrolytic apparatus having a brine evaporation concentration process, in detail, in order to balance the brine in the anode water circulating tank circulated to the anode chamber of the diaphragm electrolytic cell, the diluted anode water is evaporated and concentrated, To an apparatus for electrolyzing brine.

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 anode and cathode electrodes are located, and a diaphragm partitioning the anode chamber and the cathode chamber. The diaphragm used in this case generally uses a cation exchange membrane.

In the electrolytic reaction of salt water using the diaphragm type electrolytic cell, when a high concentration of saturated brine is supplied to the anode chamber and soft water is supplied to the cathode chamber and DC power is supplied to each anode and cathode, the chlorine ion (Cl ^- ) is converted to chlorine gas (Cl ₂ ) through the anode electrode reaction and sodium ions (Na ⁺ ) are transferred to the cathode chamber through the diaphragm. The cathode chamber in the soft water (H ₂ O), hydrogen gas (H ₂₎ and hydroxide ions (OH ^-) via the negative electrode reaction is converted to hydroxide ion (OH ^-) is a sodium ion (Na ⁺⁾ passed from the anode chamber and the 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

In the brine electrolysis process using the diaphragm type electrolytic cell, chlorine gas (Cl ₂ ) produced in the anode chamber, caustic soda (NaOH) produced in the cathode chamber, and sodium hypochlorite (NaOCl ), Hydrochloric acid (HCl) produced by reacting hydrogen in the cathode chamber and chlorine gas in the anode chamber, respectively.

In this case, the salt water discharged to the outlet of the anode chamber after the electrolysis reaction is lowered in the concentration of salt water due to the electrode reaction at the anode and the mass transfer through the diaphragm. In other words, when sodium ions move through the diaphragm, some of the water is also moved to the cathode chamber, and some water is decomposed through the anodic reaction. However, since the water consumption is lower than the consumption amount of sodium chloride in the overall reaction, .

More specifically, referring to FIG. 8, an anode water number and an anode water number are separately provided, and a cathode water number and an anode water number are produced by circulating the anode water circulating tank and the cathode water circulating tank.

In this case, saturated salt water is supplied to the anode water circulation tank to maintain the brine concentration after the reaction, and the anode water circulation tank supplies the soft water.

As described above, the anode water circulation tank has a larger amount of sodium chloride in the brine in terms of the material balance, so that the brine concentration in the anode water circulating tank is continuously diluted, thereby lowering the ion conductivity of the anode chamber, There is a structural problem that the lifetime of the anode is also lowered.

In order to solve such a problem, it is general that some of the anode water is regenerated through a brine recovery device, supplied to the saturated brine supply tank, and then supplied to the anode water circulation tank to be reused.

For this purpose, hydrochloric acid (HCl) stored in a separate chemical tank is charged into a brine recovery device using an injection pump to maintain the pH below 2, thereby recovering and recovering the chlorine remaining in the anode water.

In addition, caustic soda (NaOH) stored in a separate chemical tank is injected into a brine regenerating apparatus by using an injection pump to adjust the pH to 7 to 10 to maintain neutral or alkaline again.

And a step of adding a neutralizing agent such as a chlorine reducing agent (NaHSO ₃ ) stored in a separate chemical tank to an apparatus for recovering salt water using an injection pump to reduce residual chlorine (Cl ₂ ) to chlorine ions (Cl ^- ). The reason for this process is that in order to remove the hardness (Ca / Mg) in the saturated brine stored in the salt tank, a saturated brine water softener (using chelating resin) is installed in the previous stage of the anode circulation bath, In order to increase the removal efficiency, it is necessary to increase the pH, and since the chelate resin is vulnerable to chlorine, it is necessary to remove residual chlorine.

When the above steps are performed, the anode water can be regenerated and reused.

However, in the conventional regeneration process by injecting the above-mentioned medicines, each chemical tank for storing and injecting the three medicines, a salt water regeneration device for reacting with the injection pump, and various other devices Sensor, and a separate piping for moving the material. Therefore, there is a problem in that the apparatus is complicated and the safety hazards due to the use of chemicals such as hydrochloric acid (HCl), neutralizing agent and caustic soda (NaOH) There are various problems such as an increase in maintenance cost.

Meanwhile, in another method, there is a method of injecting salt water into the anode tank in a supersaturated state, which uses a special pump such as a hose pump or a piston pump, and ultimately removes the hard substance in the salt itself There is a limitation that the hardness of the salt can not be removed to the level required in the process.

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

In order to solve the above-mentioned problems, an object of the present invention is to provide an electrolytic cell which is circulated after an anode reaction in an electrolytic bath so as to maintain the conductivity of the anode water supplied to the electrolytic cell without using a chemical, And a concentrated salt solution evaporating step of concentrating the water and re-supplying the concentrated water to maintain a high concentration of the anode water stored in the anode water circulation tank at a constant concentration of saturated brine.

It is another object of the present invention to provide an electrolytic cell having an electrolytic cell having an efficient brine evaporation concentration process by supplying the diluted anode water through the upper part of the evaporation condensing tank to increase the efficiency of converting low temperature and low humidity air supplied from outside into hot, And a decomposition apparatus.

Another object of the present invention is to provide an electrolytic apparatus having an evaporation concentrator for concentrating the diluted anode water in an inclined manner and connecting the anode water circulation tank and the anode water circulation tank by a single connection line, .

Another object of the present invention is to provide an electrolytic apparatus having a brine evaporation concentration process with means for safely removing or recycling the chlorine gas generated when the diluted anode water is evaporated and concentrated.

According to the present invention, there is provided an electrolytic apparatus including a cathode chamber for electrolyzing a high-concentration salt water circulated and supplied from a cathode water circulating tank through a diaphragm, And a cathode chamber for electrolyzing the soft water circulated and supplied from the cathode chamber;

After the cathode reaction in the anode chamber, the low-temperature and low-humidity air is introduced into the evaporation tank through which the diluted anode water stored in the anode water circulation tank is supplied to the evaporation tank, and then the air is converted into hot and humid water vapor. And an evaporation concentrator for discharging the concentrated anode water and re-supplying the concentrated anode water to the anode water circulation tank.

In a preferred embodiment, a concentrating heater for heating the diluted anode water may be installed in the evaporation tank.

In a preferred embodiment, the evaporation and concentration tank is supplied with the diluted anode water of the anode water circulating tank through the dilute anode water supply line, and the concentrated brine is supplied again to the anode water circulating tank through the anode water supply line .

In a preferred embodiment, the dilute anode water supply line of the evaporation concentrator is connected to the lower end of the anode water circulation tank and the lower end of the evaporation condenser so that the pressure of the anode water circulation tank can be transferred to the evaporation tank through the anode water circulation tank. Can be configured.

In a preferred embodiment, the dilute anode water supply line of the evaporation concentrator may be branched on the anode water supply line at the downstream end of the anode water circulation tank circulation pump and transferred to the evaporation tank.

In a preferred embodiment, the evaporation tank is constructed such that the lower portion thereof is inclined and the anode water circulation tank is connected to the anode water circulation tank through a single material exchange line so that the anode water level between the anode water level and the salt water concentration is automatically adjusted.

In a preferred embodiment, the outside air supply line may be configured to supply low-temperature and low-humidity air into the diluted anode water of the evaporation condenser, thereby increasing the contact area with the anode water diluted by bubbling.

In a preferred embodiment, an air diffusing pipe is connected to the distal end of the outside air supply line so that fine bubbling occurs.

 In a preferred embodiment, the evaporation condenser may further comprise a dilute anode water injection nozzle for injecting the diluted anode water supplied through the dilute anode water supply line at an upper end thereof.

In a preferred embodiment, the dilute anode water supply line may be branched on the anode water supply line at the downstream end of the anode water circulation tank circulation pump and transferred to the evaporation / concentration tank.

In a preferred embodiment, a diaphragm may be installed inside the evaporator to increase the residence time of the diluted anode water on the evaporator.

In a preferred embodiment, the diaphragm may be configured as a top and bottom multi-stage.

In a preferred embodiment, the air supplied to the evaporation and concentration tank may be configured such that the outside air supply means provided at the upstream side of the outside air supply line pressurizes and supplies air to bubble into the diluted anode water stored in the evaporation tank.

In a preferred embodiment of the present invention, the air supplied to the evaporation and concentration tank is decompressed in the evaporation / condensation tank by the outside air supply means provided at the rear end of the evaporation / concentration tank, so that outside air flows into the diluted anode water stored in the evaporation / So as to be injected.

In a preferred embodiment, the evaporation and concentration apparatus may further include an adsorption tank in which activated carbon is contained to remove chlorine components contained in hot and humid air discharged through an air transfer line.

In a preferred embodiment, the evaporation and concentration apparatus includes an absorption tank for receiving and storing cathode water containing caustic soda from the cathode water circulation tank to remove chlorine components contained in hot and humid air discharged through an air transfer line; And the like.

In a preferred embodiment, the chlorine component in the hot and humid air may be bubbled or scrubbed so that the absorption reaction may occur in the cathode water containing caustic soda stored in the absorption tank.

In a preferred embodiment, the absorption liquid heated by the exothermic reaction in the formation of sodium hypochlorite in the absorption tank is introduced into a heat exchanger provided on a transfer line for supplying saturated brine from the salt storage tank to the anode water circulation tank through a heat exchange line installed in the absorption tank And the saturated brine is heat-exchanged with the saturated brine being conveyed to raise the temperature of the brine.

In a preferred embodiment, the absorption liquid, which is a caustic soda solution containing a part of sodium hypochlorite discharged from the absorption tank, is supplied to the reaction apparatus together with the chlorine gas discharged through the chlorine gas supply line connected to the upper part of the anode water circulation tank, To produce sodium hypochlorite.

In a preferred embodiment of the present invention, a conductivity measurement sensor is provided at any point of the anode water supply line or the anode water recovery line connecting the anode water circulation tank and the anode chamber of the electrolytic cell, and a level sensor for level measurement installed in the anode water circulation tank When the conductivity is less than the set value, the evaporation concentration apparatus is operated. When the water level of the anode water circulation tank is less than the set value, the saturated salt water in the salt storage tank is supplied to the anode water circulation tank through the saturated salt water transfer line.

The present invention having such characteristics as described above is characterized in that an evaporative concentration tank for supplying cold air to the diaphragm type electrolytic apparatus and heating the diluted anode water is heated so that the amount of water vapor per unit volume of exhausted air is saturated, The amount of water in the anode water is reduced so that the diluted anode water supplied from the anode water circulating tank can be re-supplied to the anode water circulating tank at a high concentration close to that of saturated brine, It is possible to supply the anode water at a high concentration close to that of saturated brine,

Also, since the diluted anode water is supplied through the upper part of the evaporation tank, the efficiency of converting the low temperature and low humidity air supplied from the outside into the hot,

In addition, the lower part of the evaporation condenser for evaporating and concentrating the diluted anode water is inclined so that it is connected to the anode water circulation line through one line, so that the material balance of sodium chloride and water is naturally reduced by the level of the anode water and the concentration difference The advantage of being able to simplify the entire device configuration is that it can be adjusted,

In addition, since the chlorine gas generated when the diluted anode water is concentrated by evaporation can be adsorbed through activated carbon or reacted with sodium hydroxide to produce sodium hypochlorite, it can be supplied to the reaction apparatus, It is a highly anticipated invention.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a first embodiment of the present invention,
FIG. 2 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a second embodiment of the present invention,
FIG. 3 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a third embodiment of the present invention,
FIG. 4 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a fourth embodiment of the present invention,
5 is an exemplary view showing the structure of an evaporation and concentration tank according to a fifth embodiment of the present invention,
6 is an exemplary view showing a dilute anode water supply configuration supplied to an evaporation and concentration tank according to a sixth embodiment of the present invention,
7 is an exemplary view showing a dilute anode water supply configuration supplied to an evaporation and concentration tank according to a seventh embodiment of the present invention,
FIG. 8 is an exemplary view showing an electrolytic apparatus having an anode water regeneration process by conventional drug injection.

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.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a first embodiment of the present invention; FIG.

As shown in the figure, the present invention has a diaphragm type electrolytic cell 1 for electrolyzing saturated water and soft water, which are divided into an anode chamber 102 and a cathode chamber 103 with a diaphragm 101 therebetween.

When the anode water is supplied to the cathode chamber 103 and the DC power is supplied to the anode and the cathode, the cathode chamber 102 constitutes the anode chamber. (Cl ^- ) in the saturated salt water (NaCl) is converted into the chlorine gas (Cl ₂ ) through the anode electrode reaction and the sodium ion (Na ⁺ ) is transferred to the cathode chamber through the diaphragm. In the cathode chamber, soft water (H ₂ O) constituting the cathode water is supplied and is converted into hydrogen gas (H ₂ ) and hydroxide ion (OH ^- ) through the cathode electrode reaction, so that the hydroxide ion (OH ^- It forms equilibrium with ions (Na ⁺ ) to form caustic soda (NaOH).

The saturated brine supplied to the anode chamber 102 of the electrolyzer 1 is supplied to the anode water circulation tank 2 through the anode water supply line 202 by the anode water circulation tank circulation pump 201 do.

Further, the chlorine gas generated after the anode reaction in the anode chamber and the diluted anode water are supplied to the anode water circulating tank through the anode water collecting line 203, and the chlorine gas recovered into the anode water circulating tank is supplied again to the anode water circulating tank Is supplied to the reaction apparatus 7 through the chlorine gas supply line 204 connected to the sodium hypochlorite to be used for producing sodium hypochlorite.

Soft water supplied to the cathode chamber of the electrolytic cell cathode water circulation (3) hydroxide ions (OH ^-) generated stored soft water is supplied through the training supply line 301, and also after a negative electrode reaction in the cathode chamber in the NaOH is formed in equilibrium with the sodium ions (Na ⁺ ) supplied from the anode chamber and supplied to the cathode water circulating tank through the cathode water recovery line 302 together with the soft water, and the caustic soda recovered into the cathode water circulating tank The caustic soda solution mixed with the aqueous softener water is supplied to the reactor 7 through the caustic soda feed line 303 connected to the cathode water circulation tank and the metering pump 304 to produce sodium hypochlorite .

After being subjected to a positive electrode reaction in the anode chamber of the membrane-type electrolytic cell, the dilute anode water circulated through the anode water recovery line 203 to the anode water circulation bath is supplied to the evaporation concentrator 4, And is supplied to the circulation tank.

Concretely, the evaporation concentrator 4 supplies the diluted anode water of the anode water circulation tank 2 through the diluted anode water supply line 401 to the evaporation and concentration tank 402 and stores it. At this time, it is preferable that the dilute anode water supply line 401 is connected to the lower part of the evaporation and concentration tank 402. This is because the diluted anode can be moved naturally in the anode water circulating tank by using the pressure difference due to the water level of the anode water circulating tank without any separate transporting means.

Air supply means 403 such as a ring blower type blower is connected to the lower portion of the evaporation and concentration tank 402 through the outside air supply line 404 to blow low temperature and low humidity air into the diluted anode water stored in the evaporation concentration tank, So that the air is brought into contact with the diluted anode water. In order to prevent the reverse flow of the anode water stored in the evaporation tank through the outside air supply line, it is preferable to set the position of the outside air supply means or the outside air supply line higher than the water level of the anode water stored in the evaporation tank, or install a check valve on the outside air supply line Do.

At this time, the concentrated water heater 405, which is installed through the inside of the evaporation and concentration tank, heats the diluted anode water. The low temperature and low humidity air supplied through the outside air supply means is heated by the difference of the saturated steam according to the temperature difference, State to evaporate.

In addition, an air diffuser 412 is installed at the distal end of the outside air supply line to reduce the bubble size of the low-temperature and low-humidity air supplied from the outside, thereby increasing the contact area with the diluted anode water, It is preferable to further increase it.

When the low-temperature, low-humidity air supplied through the outside air supply means is in contact with the diluted anode water in the bubbling state, it is converted into hot and humid air so that the amount of water in the diluted anode water stored in the evaporation- do. The reason for introducing the low-temperature and low-humidity air is that the enrichment efficiency of the anode water is drastically increased because a much larger amount of the anolyte in the humid evaporation tank is evaporated and discharged.

For reference, the evaporation concentration principle is explained in detail. The absolute humidity (water vapor amount per unit volume, kg_water / kg_air) when the relative humidity is 100% at 1 at 25 ° C and 80 ° C is different and the values are 0.02007 and 0.545498 . That is, when the air temperature rises from 25 ° C to 80 ° C, the amount of water vapor (water) that can be contained in the same volume of air is increased by about 27 times. Therefore, when the diluted anode water is kept at a high temperature in the evaporation tank filled with the appropriate water level, and when the cold air flows out from the outside of the evaporator, the air and the anode water contact through the anode water in the evaporation tank and the bubbling or scrubbing process (Heat transfer) and discharged as hot and humid air, the diluted anode water in the evaporator is concentrated.

The water vapor in the high temperature and high humidity state evaporated by the heating of the condensing heater is included together with a part of chlorine gas which can be introduced together with the dilution water from the anode water circulation tank to the evaporation tank through the diluted anode water supply line 401 And then discharged through the air transfer line 406. The discharged water vapor and the chlorine gas are supplied to the adsorption tank 407a in which the activated carbon is present and pass through the activated carbon to remove the chlorine gas. The air from which the chlorine gas has been removed is discharged to the atmosphere through the air discharge line 408 .

At this time, the air discharge line 408 for supplying the high temperature and high-humidity steam supplied to the activated carbon adsorption tank 407a to the upper portion of the activated carbon tank and discharging the air through which the chlorine gas has been removed through the activated carbon, And a waste liquid discharge port (not shown) capable of discharging a part of condensed high-temperature and high-humidity water vapor to the waste liquid can be disposed under the adsorption tank 407a.

However, the present invention is not limited to the structure of the adsorption tank 207a. In the present invention, a structure capable of reducing differential pressure, minimizing the condensation of water vapor and removing the discharged chlorine gas when treating the incoming hot, Any of the above can be applied.

The evaporated and concentrated anode water is recycled to the anode water circulating tank 2 through the anode water supply line 409. At this time, the anode water supply line 409 starts to flow from the upper side of the anode water circulating tank and is piped so as to be discharged after passing through the lower side, so that the concentrated anode water overflows due to the water level and is naturally transported to the anode water circulating tank 2 .

Further, the evaporation concentration apparatus 4 operates when the conductivity of the anode water circulating in the anode water circulating tank 2 and the electrolytic bath is below the set control value, increases the conductivity, and stops when the conductivity becomes higher than the target control value desirable. To this end, a sensor 205 for measuring the conductivity is provided at any point in the anode water supply line 202 or the anode water recovery line 203, and a level sensor for measuring the water level is installed in the anode water circulation tank 2 And controls the concentration heater 405 and the outside air supply means 403 when the conductivity is lower than the set value and controls the supply of saturated brine through the saturated brine transfer line 502 when the water level falls below the lower limit . The sensor 205 for measuring the conductivity may be installed at the rear end of the anode water circulation tank circulation pump.

The saturated brine supplied to the anode water circulation tank is supplied through the salt reservoir 5. At this time, the saturated brine discharged to the salt storage tank is supplied to the anode water circulating tank through the transfer line 502 by the transfer force of the transfer pump 501. It is preferable that a heater 503 is provided on the transfer line to heat the saturated brine and then remove the hardness (Ca / Mg) in the saturated brine after passing through the saturated brine water softener 504. The term "saturated brine" means about 25 to 30 wt% of brine.

The soft water supplied to the salt storage tank and the cathode water circulation tank is supplied by a soft water line 601 connected to a water softener 6 for softening the raw water. Here, the training device 6 may be a water softener or a device such as RO / NF.

The chlorine gas of the anode water circulating tank 2 storing the chlorine gas (Cl ₂ ) generated through the anode electrode reaction, the hydroxide ions (OH ^- ) generated through the cathode electrode reaction and the sodium ions (NaOH) generated from sodium hydroxide (Na ⁺ ) is subjected to gas-liquid contact reaction in the reactor (7) to produce sodium hypochlorite (NaOCl).

The sodium hypochlorite produced in the reaction apparatus is stored in the storage tank 8 and then supplied to the use place.

In order to produce chlorine (Cl ₂ ) and caustic soda (NaOH) or hydrochloric acid (HCl) produced in the diaphragm type electrolytic cell, if necessary, a reaction tank for producing sodium hypochlorite (NaOCl) Or a reservoir.

FIG. 2 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a second embodiment of the present invention.

Most of the configuration of the second embodiment shown in the figure is the same as that of the first embodiment, so that the same configuration will be replaced with the description of the first embodiment to avoid redundant description, and only differences will be described below.

The second embodiment is different from the second embodiment in that the position of the outside air supply means 403 for supplying the outside air is not provided at the entrance of the outside air supply line 404 but is provided at the upper part of the adsorption tank 407a in which the activated carbon is contained to discharge the air from which the chlorine gas has been removed Which is formed on the air discharge line 408 formed in the air discharge line 408.

When the outside air supply means 403 is installed on the air discharge line 408, the evaporation and concentration tank 402 is provided with a reduced pressure by the suction force of the outside air supply means, so that the air is introduced into the evaporation concentration tank 402, The contact area between the air supplied through the outside air supply line 404 and the anode water is increased so that a much larger amount of water is evaporated into the hot and humid air in the anode water heated by the concentration heater to be in a state of high temperature and high humidity . Therefore, the concentration efficiency of the anode water has the same effect as that in the case where the outside air supply means 403 is installed at the inlet of the outside air supply line 404 as in the first embodiment.

By operating the inside of the evaporation and concentration tank 402 in a reduced pressure state, it is possible to prevent some chlorine gas from leaking to the outside air due to breakage of the evaporation tank and piping, thereby providing a facility with more safety.

3 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a third embodiment of the present invention.

Most of the configuration of the third embodiment shown in FIG. 3 is the same as that of the first embodiment, so that the same configuration will be replaced with the description of the first embodiment to avoid redundant description, and only differences will be described below.

Example 3 is different from Example 1 in that the water vapor and the chlorine gas discharged from the discharged evaporation condenser are not removed using the adsorption tank 407a in which the activated carbon is contained but the caustic soda supply line 303 to remove and remove caustic soda mixed with the cathode water through bubbling or scrubbing through the absorption tank 407b which receives and stores the caustic soda mixed with the cathode water. When the chlorine gas is supplied to the absorption tank in which the caustic soda is stored, caustic soda and chlorine gas exothermically produce sodium hypochlorite.

Therefore, unlike the first embodiment, the supply of the caustic soda solution produced in the cathode water circulation tank 3 and the chlorine contained in the air in the hot and humid water vapor are absorbed by the reaction device 7 through the metering pump 304 A low sodium hypochlorite is formed by reacting in the bath 407b, and a caustic soda solution containing a part of the sodium hypochlorite formed is supplied through the absorption liquid supply line 305.

On the other hand, in order to cool the heat generated while generating sodium hypochlorite in the absorption tank 407b, a heat exchange line 410 is provided in the absorption tank, and a heat exchange is performed on the transfer line 502 for supplying saturated brine to the anode water circulation tank 2 A unit 505 is provided to exchange the absorption liquid with the saturated brine being conveyed. According to this configuration, the heater 503 provided in the first embodiment may not be separately provided.

FIG. 4 is a general view showing a brine electrolysis apparatus having an evaporation concentration apparatus according to a fourth embodiment of the present invention.

Most of the configuration of the fourth embodiment shown in FIG. 3 is the same as that of the third embodiment, so that the same configuration is replaced with the description of the third embodiment to avoid redundant description, and only differences will be described below.

In the fourth embodiment, the position of the blower 403 for supplying outside air is not provided at the beginning of the outside air supply line 404, (Not shown).

The operation of introducing the low-temperature and low-humidity air by the reduced pressure through the outside-air supply line 404 of the evaporation-concentrating tank 402 by the outside-air supply means 403 provided on the air discharge line 408 is similar to that The diluted anode water is concentrated by the same action. A more detailed description will be omitted and replaced with the description of the second embodiment in order to avoid redundant description.

5 is an exemplary view showing the structure of an evaporation and concentration tank according to a fifth embodiment of the present invention. As shown in the figure, it is understood that the lower structure is inclined differently from the lower structure of the evaporation and concentration tank 402 used in the first to fourth embodiments.

The dilute anode water supply line 401 and the anode water supply line 409 formed between the evaporation concentrator 402 and the anode water circulating tank 2 constituted by inclining lower parts are constituted only by one substance exchange line 411 And it is a simplified structure. At this time, it is preferable to set the position of the evaporation / condensation tank slightly higher than the height of the anode water circulation bath.

When the one substance exchange line 411 is constructed as described above, the level of the anode water level between the evaporation concentrator 402 and the anode water circulation tank 2 is automatically adjusted, and the concentration of the salt water in the anode water is automatically adjusted .

6 is an exemplary view showing a dilute anode water supply configuration supplied to an evaporation and concentration tank according to a sixth embodiment of the present invention.

As shown in the figure, according to the configuration of the sixth embodiment, the dilute anode water supply line 401 for supplying the diluted anode water of the anode water circulating tank 2 to the evaporation and concentration tank 402 is connected to the electrolytic water circulating tank 2, Is branched to the anode water supply line (202) at the rear end of the anode water circulating tank circulation pump (201) circulating and supplying the anode water to the anode chamber (102) of the evaporator (1).

With this configuration, the dilute anode water supply line 401 is connected to the lower portion of the evaporation and concentration tank 402, as shown in Examples 1 to 4, and the diluted anode water is supplied to the anode The anode water diluted by the pressure of the anode water circulation tank circulation pump 201 is supplied to the evaporation tank without being transferred from the water circulation tank to a more stable system.

7 is an exemplary view showing a dilute anode water supply configuration supplied to an evaporation and concentration tank according to a seventh embodiment of the present invention,

As shown in the drawing, according to the configuration of the sixth embodiment, the dilute anode water supply line 401 for supplying the diluted anode water of the anode water circulating tank 2 to the evaporation and concentration tank 402 is different from the anode water supply line 401 of the first to fourth embodiments Branched on the anode water supply line 202 at the downstream end of the anode water circulation pump circulation pump 201 for circulating and supplying the anode water from the circulation tank 2 to the anode chamber 102 of the electrolyzer 1 and supplied to the evaporation and concentration tank 402 So that the anode water diluted by the pressure of the anode water circulation tank circulation pump 201 is supplied.

The diluted anode water is supplied to the lower part of the evaporation tank through the dilute anode water injection nozzle 413 located at the upper part of the evaporation tank 402 by the pressure of the anode water circulation tank circulation pump 201.

In addition, the diluted anode water particles sprayed into the evaporation tank are kept in the atmospheric state for a long time, and a plurality of layers of diaphragms 414 are installed and stored in the lower part so that the surface area can be kept wide.

The principle of evaporating water in the dilute anode water according to this structure is that the operation for evaporating water in the dilute anode water located in the lower portion of the evaporation condenser is externally supplied through the same operating principle as in the description of Embodiments 1 to 4 The other part is further humidified by the water contained in the diluted anolyte water injected from the upper part of the evaporation condenser into the air discharged from the upper air layer of the evaporation condenser so that the saturated water vapor So that a much larger amount of water is evaporated in the low-temperature and low-humidity air, so that the air can be discharged as hot and humid air in a saturated water vapor state. Therefore, it is possible to enhance the effect that the concentration efficiency of the anode water is drastically increased.

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.

(1): diaphragm electrolytic cell (2): anode water circulation tank
(4): Evaporation concentrator (5): Salt storage tank
(6): Water softener (7): Reactor
(8): Reservoir (101): Diaphragm
(102): anode chamber (102): cathode chamber
(201): anode water circulation tank circulation pump (202): anode water supply line
(203): anode water recovery line (204): chlorine gas supply line
(205): sensor (301): soft water supply line
(302): cathode water recovery line (303): caustic soda supply line
(304): metering pump (305): absorption liquid supply line
(401): diluting anode water supply line (402): evaporation condensing tank
(403): outside air supply means (404): outside air supply line
(405): Concentrating heater (406): air transfer line
(407a): adsorption tank (407b): absorption tank
(408): air discharge line (409): anode water supply line
(410): Heat exchange line (411): Material exchange line
(412): diffuser 413: diluting anode water injection nozzle
(414): diaphragm (501): feed pump
(502): transfer line (503): heater
(504): saturated brine water softener (505): heat exchanger
(601): Training line

Claims (20)

A diaphragm type electrolytic cell comprising a cathode chamber for electrolyzing salt water of a high concentration circulated and supplied from the anode water circulating tank through the diaphragm and a cathode chamber for electrolyzing the soft water circulated and supplied from the cathode water circulating tank;
After the cathode reaction in the anode chamber, the low-temperature and low-humidity air is introduced into the evaporation tank through which the diluted anode water stored in the anode water circulation tank is supplied to the evaporation tank, and then the air is converted into hot and humid water vapor. And an evaporation concentrator for discharging the concentrated anode water and re-supplying the concentrated anode water to the anode water circulation tank.
The method according to claim 1 or 2,
Wherein a concentrated heater for heating the diluted anode water is inserted in the evaporation tank.
The method according to claim 1 or 2,
Wherein the evaporated thickener is supplied with the diluted anode water of the anode water circulating tank via the dilute anode water supply line and the concentrated brine is supplied again to the anode water circulating tank through the anode water supply line. .
The method of claim 3,
Wherein the diluted anode water supply line of the evaporation condenser is connected to the lower end of the anode water circulation tank and the lower end of the evaporation condenser so as to be conveyed to the evaporation tank through the anode water circulation tank by the pressure caused by the water level difference of the anode water circulation tank An electrolytic apparatus having a brine evaporation concentration process.
The method of claim 3,
Wherein the diluted anode water supply line of the evaporation condenser is branched on the anode water supply line at the downstream end of the anode water circulation tank circulation pump and is transferred to the evaporation concentrating tank.
The method according to claim 1 or 2,
The evaporation / condensation tank is constructed such that the lower portion is inclined to press the anode water stored on the lower side, and the cathode water circulation tank is connected to the anode water circulation tank through a single material exchange line so that the anode water level between both sides is automatically adjusted to the salt water concentration Wherein the electrolytic apparatus has a brine evaporation concentration process.
The method according to claim 1 or 2,
Wherein the outside air supply line is configured to increase the contact area with the anode water diluted by the bubbling by supplying the low temperature and low humidity air into the diluted anode water of the evaporation condenser. Device.
The method of claim 7,
Wherein an air diffuser is connected to an end portion of the outside air supply line to cause fine bubbling.
The method according to claim 1 or 2,
Wherein the evaporation condenser further comprises a dilute anode water injection nozzle for spraying the diluted anode water supplied through the dilute anode water supply line at an upper end thereof.
The method of claim 9,
Wherein the dilute anode water supply line is branched on the anode water supply line at the rear end of the anode water circulation tank circulation pump and is transferred to the evaporation concentrating tank.
The method of claim 9,
Wherein an evaporator is provided in the evaporation tank with a diaphragm for increasing the residence time of the diluted anode in the evaporation tank.
The method of claim 11,
Wherein the diaphragm is composed of upper and lower stages.
The method according to claim 1 or 2,
Wherein the air to be supplied to the evaporation and concentration tank is formed by bubbling and supplying the air into the diluted anode water stored in the evaporation concentration tank by supplying the air to the outside air supply means provided at the upstream side of the outside air supply line. Decomposition device.
The method according to claim 1 or 2,
The air to be supplied to the evaporation condenser is decompressed inside the evaporator to supply the outside air from the outside air supply line into the diluted anode water stored in the evaporator, Wherein the electrolytic apparatus has a brine evaporation concentration process.
The method according to claim 1 or 2,
Wherein the evaporation and concentration apparatus further comprises an adsorption tank in which activated carbon is contained to remove chlorine components contained in hot and humid air discharged through an air transfer line, .
The method according to claim 1 or 2,
The evaporation and concentration apparatus further comprises an absorption tank for receiving and storing the cathode water containing caustic soda from the cathode water circulation tank to remove chlorine components contained in the high temperature and high humidity air discharged through the air transfer line Wherein the electrolytic apparatus has a brine evaporation concentration process.
18. The method of claim 16,
Wherein the high-temperature and high-humidity air chlorine components are bubbled or scrubbed so that an absorption reaction can take place in the cathode water containing caustic soda stored in the absorption tank.
18. The method of claim 16,
The absorption liquid heated by the exothermic reaction in the formation of sodium hypochlorite in the absorption tank is sent to the heat exchanger provided on the transfer line for supplying the saturated brine from the salt reservoir to the anode water circulation tank through the heat exchange line installed in the absorption tank, And the temperature of the saturated brine is increased.
18. The method of claim 16,
The absorption liquid, which is a caustic soda solution containing a part of sodium hypochlorite discharged from the absorption tank, is supplied to the reaction apparatus together with the chlorine gas discharged through the chlorine gas supply line connected to the upper part of the anode water circulation tank, Wherein the electrolytic apparatus is configured to generate the brine evaporation concentration process.
The method according to claim 1 or 2,
A conductivity measurement sensor provided at any point of the anode water supply line or the anode water recovery line connecting the anode water circulation tank and the anode chamber of the electrolytic cell and a level sensor for level measurement installed in the anode water circulation tank, , And when the water level of the anode water circulation tank is equal to or lower than the set value, the saturated brine of the salt storage tank is supplied to the anode water circulation tank through the saturated brine transfer line. Electrolysis device.

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