CN212655861U - Caustic soda production system of high-efficient retrieval and utilization condensation acid - Google Patents
Caustic soda production system of high-efficient retrieval and utilization condensation acid Download PDFInfo
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- CN212655861U CN212655861U CN202021330015.1U CN202021330015U CN212655861U CN 212655861 U CN212655861 U CN 212655861U CN 202021330015 U CN202021330015 U CN 202021330015U CN 212655861 U CN212655861 U CN 212655861U
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Abstract
The utility model discloses a caustic soda production system of high-efficient retrieval and utilization condensation acid, including refined unit of salt solution, electrolysis trough, synthetic furnace, anolyte circulating unit, catholyte circulating unit, condensation acid retrieval and utilization unit and controller. The utility model has the advantages that: through setting up condensation acid retrieval and utilization unit and chlorate decomposer, collect condensation acid and be used for chlorate to decompose, because light salt solution itself just contains free chlorine, consequently does not have the requirement to condensation acid's free chlorine content, need not to add sodium sulfite when the salt solution is refined and dechlorinate, reduced condensation acid retrieval and utilization cost. The light salt water output from the chlorate decomposer enters a dechlorinating tower, and the dechlorinating tower can remove and recycle free chlorine in the light salt water, so that the risk of damaging a chelate resin tower due to incomplete dechlorination of condensed acid is reduced, and the recycling of the free chlorine in the condensed acid is realized.
Description
The technical field is as follows:
the utility model relates to a chlor-alkali chemical industry field, specifically speaking relate to a caustic soda production system of high-efficient retrieval and utilization condensation acid.
Background art:
as a novel process for preparing caustic soda, the ion membrane process for preparing caustic soda is increasingly applied in recent years. When the ion membrane method is used for preparing alkali, industrial salt is firstly dissolved in water to obtain crude brine, and the crude brine is sent into an anode chamber of an ion membrane electrolytic cell for electrolysis after being refined. Na in brine in anode chamber during electrolysis+Passing through the ionic membrane, entering the cathode chamber, and reacting with OH in water-Combine to form NaOH, remaining H+And Cl-Hydrogen and chlorine are generated separately. Discharging NaOH together with the catholyte, and feeding the NaOH into an evaporation device to obtain finished caustic soda; the NaCl content in the electrolyzed anode liquid is reduced to become light salt water, and the light salt water is discharged from an anode liquid outlet to prepare for recycling.
However, since the electrolytic cellThe ion membrane generates pinholes after being used for a period of time, so that OH in catholyte is generated-The sodium chlorate passes through the ionic membrane and enters the cathode, which affects the quality of caustic soda and can corrode subsequent nickel equipment.
In addition, hydrogen and chlorine are discharged into the synthesis furnace from the gas outlets of the anode and the cathode, respectively, to generate hydrogen chloride. Because the hydrogen entering the synthesis furnace contains certain moisture, the water is sent out of the synthesis furnace along with the hydrogen chloride gas, and because the environmental temperature is low, the hydrogen chloride is condensed and absorbed to form condensed acid which is used for refining the brine. However, when hydrogen chloride is produced by the reaction in the synthesis furnace, free chlorine remains in the hydrogen chloride gas due to insufficient reaction, and the free chlorine remains after the hydrogen chloride is produced into a condensed acid. Free chlorine has stronger oxidability, and the traditional method is to add sodium sulfite into the primary brine refining process for dechlorination so as to meet the use requirement of brine refining and improve the cost of recycling condensed acid; meanwhile, if the free chlorine is not completely removed, the chelating resin of the chelating resin tower may lose adsorption capacity, the refining effect of the brine is affected, the brine with poor refining effect contains impurities, the ionic membrane of the electrolytic cell is damaged, and the service life of the electrolytic cell is shortened.
The utility model has the following contents:
an object of the utility model is to provide a with the sour retrieval and utilization of condensation to chlorate decomposer, reduce the sour retrieval and utilization cost of condensation and manufacturing cost's caustic soda production system.
The utility model discloses by following technical scheme implement: a caustic soda production system for efficiently recycling condensed acid comprises a brine refining unit, an electrolytic cell, a synthesis furnace, an anolyte circulating unit and a catholyte circulating unit;
the liquid outlet of the chelate resin tower of the brine refining unit is communicated with the anode liquid inlet of the electrolytic cell, the gas outlets of the anode and the cathode of the electrolytic cell are communicated with the gas inlet of the synthesis furnace, the anode liquid outlet is communicated with the anode liquid inlet, the liquid inlet of the second brine heat exchanger of the anolyte circulating unit and the liquid inlet of the dechlorination tower, the cathode liquid outlet is communicated with the caustic soda tank liquid inlet and the circulating cooler liquid inlet of the catholyte circulating unit, and the cathode liquid inlet is communicated with the circulating cooler liquid outlet of the catholyte circulating unit; a liquid outlet of the dechlorination tower of the anolyte circulating unit is communicated with a liquid inlet of a water distribution tank of the brine refining unit;
the system also comprises a condensed acid recycling unit and a controller, wherein the condensed acid recycling unit comprises a condensed acid tank, a recycling tank and a high-purity hydrochloric acid tank, a liquid inlet is formed in the top of the condensed acid tank, a liquid outlet is formed in the bottom of the condensed acid tank, a first liquid level meter is arranged on one side of the condensed acid tank, and the liquid inlet of the condensed acid tank is communicated with a gas outlet of the synthesis furnace; a liquid inlet is formed in the top of the recycling tank, a liquid outlet is formed in the bottom of the recycling tank, and the liquid inlet is communicated with the liquid outlet of the condensed acid tank and the liquid outlet of the high-purity hydrochloric acid tank; the anolyte circulating unit is provided with a chlorate decomposing tank, one side of the chlorate decomposing tank is provided with an acid inlet, the acid inlet of the chlorate decomposing tank is communicated with the liquid outlet of the recycling tank, the liquid outlet of the condensed acid tank, the liquid outlet of the recycling tank and the liquid outlet of the high-purity hydrochloric acid tank are respectively provided with a conveying pump, and a pipeline for communicating the liquid outlet of the recycling tank and the acid inlet of the chlorate decomposing tank is sequentially provided with a flowmeter and a first self-regulating valve;
the first liquid level meter and the flow meter are in signal connection with the input end of the controller, and the delivery pump arranged at the liquid outlet of the condensed acid tank and the first self-regulating valve are in signal connection with the output end of the controller.
Further, a second self-regulating valve is arranged on a pipeline which communicates the liquid outlet of the high-purity hydrochloric acid tank with the liquid inlet of the recycling tank; and a second liquid level meter is arranged on one side of the recycling tank and is in signal connection with the input end of the controller, and a second self-regulating valve is in signal connection with the output end of the controller.
Further, the brine refining unit comprises the water distribution tank, a membrane filter, a first brine heat exchanger and the chelating resin tower, wherein a liquid outlet of the water distribution tank is communicated with a liquid inlet of the membrane filter; the liquid outlet of the membrane filter is communicated with the liquid inlet of the first brine heat exchanger, the liquid outlet of the first brine heat exchanger is communicated with the liquid inlet of the chelate resin tower, and the regeneration port of the chelate resin tower is communicated with the liquid outlet of the high-purity hydrochloric acid tank.
Further, the anolyte circulating unit comprises the second brine heat exchanger, the chlorate decomposition tank and the dechlorination tower, a liquid outlet of the second brine heat exchanger is communicated with a liquid inlet of the chlorate decomposition tank, a liquid outlet of the chlorate decomposition tank is communicated with a liquid inlet of the dechlorination tower, and a liquid outlet of the dechlorination tower is communicated with a liquid inlet of a water distribution tank of the brine refining unit.
Further, the catholyte circulating unit comprises the caustic soda tank, an evaporating device and the circulating cooler, and a liquid outlet of the caustic soda tank is communicated with a liquid inlet of the evaporating device.
The utility model has the advantages that:
1. by arranging the condensation acid recycling unit and the chlorate decomposing tank, the invention recycles the condensation acid and uses the condensation acid for decomposing sodium chlorate, reduces the content of sodium chlorate in the anolyte and improves the quality of caustic soda.
2. In the invention, when the condensed acid is used for decomposing chlorate, the content of free chlorine is not required, sodium sulfite is not required to be added, and the recycling cost of the condensed acid is reduced; the light salt water output by the chlorate decomposer can also enter a dechlorinating tower to remove free chlorine and recycle the free chlorine, so that the risk that the chelating resin tower loses the regeneration capacity due to incomplete dechlorination of the condensed acid is reduced, and the recycling of the free chlorine in the condensed acid is realized.
3. The high-purity hydrochloric acid tank is arranged in the condensed acid recycling unit, and the second self-regulating valve is arranged on a pipeline connecting a liquid outlet of the high-purity hydrochloric acid tank and a liquid inlet of the recycling tank; the second liquid level meter is arranged on one side of the recycling tank, when the generation amount of the condensed acid cannot meet the requirement of the chlorate decomposer, and the liquid level of the recycling tank is reduced, high-purity hydrochloric acid can be supplemented to the recycling tank, so that the continuous input of hydrochloric acid in the chlorate decomposer is ensured, and the liquid level of the recycling tank is kept stable.
4. According to the invention, the liquid outlet of the high-purity hydrochloric acid tank is communicated with the regeneration port of the chelate resin tower, and after the chelate resin tower loses adsorption capacity, high-purity hydrochloric acid can be introduced into the chelate resin tower to regenerate the chelate resin, so that the chelate resin has adsorption capacity again.
Description of the drawings:
FIG. 1 is a schematic view of the present invention;
fig. 2 is an electric control diagram of the present invention.
1-a brine refining unit; 1.1-water distribution tank; 1.2-membrane filter; 1.3-a first brine heat exchanger; 1.4-chelating resin column; 2-an electrolytic cell; 3-a synthetic furnace; 4-anolyte circulation unit; 4.1-second brine heat exchanger; 4.2-chlorate decomposer; 4.3-dechlorination tower; 5-catholyte circulation unit; 5.1-caustic soda pot; 5.2-circulation cooler; 5.3-an evaporation device; 6-a condensed acid recycling unit; 6.1-condensation acid tank; 6.2-recycling tank; 6.3-high purity hydrochloric acid tank; 6.4-first level gauge; 6.5-second level meter; 6.6-transfer pump; 6.7-flow meter; 6.8-first self-regulating valve; 6.9-second self-regulating valve; 7-a controller.
The specific implementation mode is as follows:
as shown in fig. 1 and 2, a caustic soda production system for efficiently recycling condensed acid comprises a brine refining unit 1, an electrolytic cell 2, a synthesis furnace 3, an anolyte circulating unit 4, a catholyte circulating unit 5, a condensed acid recycling unit 6 and a controller 7.
The brine refining unit 1 comprises a water distribution tank 1.1, a membrane filter 1.2, a first brine heat exchanger 1.3 and a chelating resin tower 1.4. The liquid outlet of the water distribution tank 1.1 is communicated with the liquid inlet of the membrane filter 1.2, the liquid outlet of the membrane filter 1.2 is communicated with the liquid inlet of the first brine heat exchanger 1.3, the liquid inlet of the chelate resin tower 1.4 is communicated with the liquid outlet of the first brine heat exchanger 1.3, the liquid outlet of the chelate resin tower 1.4 is communicated with the liquid inlet of the anode of the electrolytic cell 2, the prepared crude brine is firstly refined through the membrane filter 1.2, and then enters the chelate resin tower 1.4 for secondary refining after being heated by the first brine heat exchanger 1.3, and then is sent to the electrolytic cell 2 for electrolysis.
During electrolysis, hydrogen is produced in the anode compartment and sodium hydroxide and chlorine are produced in the cathode compartment. The gas outlets of the anode and the cathode of the electrolytic cell 2 are communicated with the gas inlet of the synthesis furnace 3, and hydrogen and chlorine generated by electrolytic reaction enter the synthesis furnace 3 through the gas outlet of the anode and the gas outlet of the cathode respectively. Discharging the anolyte through an anolyte outlet, returning one part of anolyte to the anolyte inlet and entering the anolyte circulating unit 4 through the other part of anolyte; the catholyte is discharged into the catholyte circulating unit 5 through the cathode liquid outlet.
The anolyte circulation unit 4 comprises a second brine heat exchanger 4.1, a chlorate decomposer 4.2 and a dechlorination tower 4.3. An anode liquid outlet of the electrolytic tank 2 is communicated with a liquid inlet of a second brine heat exchanger 4.1 and a liquid inlet of a dechlorination tower 4.3, a liquid outlet of the second brine heat exchanger 4.1 is communicated with a liquid inlet of a chlorate decomposing tank 4.2, a liquid outlet of the chlorate decomposing tank 4.2 is communicated with a liquid inlet of a dechlorination tower 4.3, and a liquid outlet of the dechlorination tower 4.3 is communicated with a liquid inlet of a water distribution tank 1.1. One part of the anolyte discharged into the anolyte circulating unit 4 directly enters a dechlorination tower 4.3 for dechlorination, the other part of the anolyte is heated in a second brine heat exchanger 4.1 and then is sent into a chlorate decomposition tank 4.2 for removing sodium chlorate, and then enters the dechlorination tower 4.3 for dechlorination, and the anolyte after dechlorination returns to a water distribution tank 1.1 for recycling.
The catholyte circulating unit 5 comprises a caustic soda tank 5.1, a circulating cooler 5.2 and an evaporating device 5.3, wherein a catholyte outlet of the electrolytic bath 2 is communicated with a catholyte inlet of the caustic soda tank 5.1 and a catholyte inlet of the circulating cooler 5.2, a catholyte inlet of the evaporating device 5.3 is communicated with a catholyte outlet of the caustic soda tank 5.1, and a catholyte outlet of the circulating cooler 5.2 is communicated with a catholyte inlet of the electrolytic bath 2. After the catholyte is discharged, a part of catholyte enters an evaporation device 5.3 through a caustic soda tank 5.1 to be evaporated, so that caustic soda with different concentrations is obtained; the other part is cooled in a circulation cooler 5.2 and returned to the cathode of the electrolytic cell 2.
The condensed acid recycling unit 6 comprises a condensed acid tank 6.1, a recycling tank 6.2 and a high-purity hydrochloric acid tank 6.3. A liquid inlet is formed in the top of the condensed acid tank 6.1, a liquid outlet is formed in the bottom of the condensed acid tank, and a first liquid level meter 6.4 is arranged on one side of the condensed acid tank. The liquid inlet is communicated with the gas outlet of the synthesis furnace 3 to collect condensed acid generated when the hydrogen chloride gas is discharged. The top of the recycling tank 6.2 is provided with a liquid inlet, the bottom is provided with a liquid outlet, and one side is provided with a second liquid level meter 6.5. The liquid inlet of the recycling tank 6.2 is communicated with the liquid outlet of the condensed acid tank 6.1 and the liquid outlet of the high-purity hydrochloric acid tank 6.3, and the liquid outlet is communicated with the acid inlet of the chlorate decomposing tank 4.2. The condensed acid in the condensed acid tank 6.1 is combined with the hydrochloric acid in the high-purity hydrochloric acid tank 6.3 in the recycling tank 6.2, and enters the chlorate decomposition tank 4.2 to participate in decomposing chlorate. The liquid outlet of the high-purity hydrochloric acid tank 6.3 is also communicated with the regeneration port of the chelate resin tower 1.4, and high-purity hydrochloric acid required by the regeneration of the chelate resin tower 1.4 can be input from the high-purity hydrochloric acid tank 6.3. A delivery pump 6.6 is arranged on each of a liquid outlet of the condensed acid tank 6.1, a liquid outlet of the recycling tank 6.2 and a liquid outlet of the high-purity hydrochloric acid tank 6.3, and a flow meter 6.7 and a first self-regulating valve 6.8 are sequentially arranged on a pipeline which communicates the liquid outlet of the recycling tank 6.2 with an acid inlet of the chloride decomposition tank 4.2; a second self-regulating valve 6.9 is arranged on a pipeline which communicates the liquid outlet of the high-purity hydrochloric acid tank 6.3 with the liquid inlet of the recycling tank 6.2.
The first liquid level meter 6.4, the second liquid level meter 6.5 and the flow meter 6.7 are in signal connection with the input end of the controller 7; the delivery pump 6.6, the first self-regulating valve 6.8 and the second self-regulating valve 6.9 which are arranged at the liquid outlet of the condensed acid tank 6.1 are in signal connection with the output end of the controller 7. The first liquid level meter 6.4 can measure the liquid level of the condensed acid tank 6.1, the flow meter 6.7 can measure the flow of the acid input into the chlorate decomposing tank 4.2 from the recycling tank 6.2, and the controller 7 can adjust the first self-regulating valve 6.8 according to the data measured by the flow meter 6.7 to realize the automatic control of the input flow of the acid in the chlorate decomposing tank 4.2; the second liquid level meter 6.5 can measure the liquid level of the recycling tank 6.2, the controller 7 can adjust the second self-regulating valve 6.9 according to the liquid level of the recycling tank 6.2, and then adjust the hydrochloric acid amount input into the recycling tank 6.2 by the high-purity hydrochloric acid tank 6.3, and the automatic adjustment of the liquid level of the recycling tank 6.2 is realized.
The working principle is as follows: during the production process, industrial salt is firstly dissolved in water to obtain crude salt water, and the crude salt water is introduced into a water distribution tank 1.1. The crude brine in the water distribution tank 1.1 firstly enters a membrane filter 1.2 for primary brine refining, and impurities in the crude brine are removed to obtain primary refined brine. But the primary refined brine still contains a certain amount of Ca2+And Mg2+The ions need to be heated by a first brine heat exchanger 1.3 and then enter a chelating resin tower 1.4, and Ca is treated by chelating resin2+And Mg2+And adsorbing to obtain secondary refined brine. The secondary refined brine is sent to the anode of the electrolytic cell 2 for electrolysis to generate sodium hydroxide, hydrogen and chlorine. After the reaction, a part of catholyte is discharged into an evaporation device 5.3 through a caustic soda tank 5.1, and the catholyte is not obtainedAnd the other part of the caustic soda with the same concentration is cooled by a circulating cooler 5.2 and then returned to the cathode chamber for recycling. The anolyte is discharged from the anolyte outlet, one part of the anolyte returns to the anolyte inlet for recycling, and the other part of the anolyte enters the anolyte circulating unit 4. And one part of the anolyte entering the anolyte circulating unit 4 enters a dechlorinating tower 4.3 for dechlorination, the other part of the anolyte enters a second brine heat exchanger 4.1 for heating to 90 ℃, then enters a chlorate decomposer 4.2 for decomposing chlorate to reduce the content of sodium chlorate, and then enters the dechlorinating tower 4.3 for dechlorination. The anode liquid discharged from the dechlorination tower 4.3 returns to the water distribution tank 1.1 for recycling. The hydrogen and the chlorine enter the synthesis furnace 3 through the gas outlet and react to generate hydrogen chloride. Because the hydrogen entering the synthesis furnace 3 contains certain moisture, the water is sent out of the synthesis furnace 3 along with the hydrogen chloride gas, and because the environmental temperature is low, the hydrogen chloride is condensed and absorbed to form condensed acid which is discharged into the condensed acid tank 6.1. The demand of the chlorate decomposer 4.2 cannot be met due to the small production of the condensed acid, and the liquid level in the condensed acid tank 6.1 gradually decreases as the production proceeds. In order to prevent the damage caused by too little condensed acid in the condensed acid tank 6.1 and the idle running of the delivery pump 6.6 at the liquid outlet, only when the liquid level in the condensed acid tank 6.1 is higher than the safety value, the delivery pump 6.6 at the liquid outlet of the condensed acid tank 6.1 is started, and the condensed acid is delivered into the chlorate decomposition tank 4.2 through the recycling tank 6.2 to decompose chlorate. The controller 7 can adjust the first self-regulating valve 6.8 according to the flow of the liquid outlet of the recycling tank 6.2 measured by the flow meter 6.7, so as to ensure that the input flow of the acid of the chlorate decomposing tank 4.2 is stable. Because hydrochloric acid needs to be continuously input into the chlorate decomposing tank 4.2, and the condensed acid in the condensed acid tank 6.1 cannot be continuously input into the recycling tank 6.2, in order to ensure that the amount of the hydrochloric acid in the recycling tank 6.2 meets the use requirement, the controller 7 can adjust the flow of the second self-regulating valve 6.9 according to the liquid level of the recycling tank 6.2 measured by the second liquid level meter 6.5, namely the amount of the hydrochloric acid input into the recycling tank 6.2 from the high-purity hydrochloric acid tank 6.3, so as to ensure that the liquid level in the recycling tank 6.2 is kept stable, and meet the use requirement of the chlorate decomposing tank 4.2.
Furthermore, chelate resin para-Ca2+And Mg2+After adsorption, the adsorption capacity is lost, and the high-purity hydrochloric acid in the high-purity hydrochloric acid tank 6.3 needs to be treatedAnd introducing the resin into a chelating resin tower 1.4 to regenerate the resin so that the resin has adsorption capacity again.
In the description of the present invention, it should be noted that, as the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. appear, the indicated orientation or positional relationship is based on the orientation or positional relationship shown in the drawings, and is only for convenience of description and simplification of description, but does not indicate or imply that the system or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" as appearing herein are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.
Claims (5)
1. A caustic soda production system for efficiently recycling condensed acid comprises a brine refining unit, an electrolytic cell, a synthesis furnace, an anolyte circulating unit and a catholyte circulating unit;
the liquid outlet of the chelate resin tower of the brine refining unit is communicated with the anode liquid inlet of the electrolytic cell, the gas outlets of the anode and the cathode of the electrolytic cell are communicated with the gas inlet of the synthesis furnace, the anode liquid outlet is communicated with the anode liquid inlet, the liquid inlet of the second brine heat exchanger of the anolyte circulating unit and the liquid inlet of the dechlorination tower, the cathode liquid outlet is communicated with the caustic soda tank liquid inlet and the circulating cooler liquid inlet of the catholyte circulating unit, and the cathode liquid inlet is communicated with the circulating cooler liquid outlet of the catholyte circulating unit; a liquid outlet of the dechlorination tower of the anolyte circulating unit is communicated with a liquid inlet of a water distribution tank of the brine refining unit;
the system is characterized by also comprising a condensed acid recycling unit and a controller, wherein the condensed acid recycling unit comprises a condensed acid tank, a recycling tank and a high-purity hydrochloric acid tank, the top of the condensed acid tank is provided with a liquid inlet, the bottom of the condensed acid tank is provided with a liquid outlet, one side of the condensed acid tank is provided with a first liquid level meter, and the liquid inlet of the condensed acid tank is communicated with the gas outlet of the synthesis furnace; a liquid inlet is formed in the top of the recycling tank, a liquid outlet is formed in the bottom of the recycling tank, and the liquid inlet is communicated with the liquid outlet of the condensed acid tank and the liquid outlet of the high-purity hydrochloric acid tank; the anolyte circulating unit is provided with a chlorate decomposing tank, one side of the chlorate decomposing tank is provided with an acid inlet, the acid inlet of the chlorate decomposing tank is communicated with the liquid outlet of the recycling tank, the liquid outlet of the condensed acid tank, the liquid outlet of the recycling tank and the liquid outlet of the high-purity hydrochloric acid tank are respectively provided with a conveying pump, and a pipeline for communicating the liquid outlet of the recycling tank and the acid inlet of the chlorate decomposing tank is sequentially provided with a flowmeter and a first self-regulating valve;
the first liquid level meter and the flow meter are in signal connection with the input end of the controller, and the delivery pump arranged at the liquid outlet of the condensed acid tank and the first self-regulating valve are in signal connection with the output end of the controller.
2. The caustic soda production system for efficiently recycling condensed acid according to claim 1, wherein a second self-regulating valve is arranged on a pipeline communicating the liquid outlet of the high-purity hydrochloric acid tank with the liquid inlet of the recycling tank; and a second liquid level meter is arranged on one side of the recycling tank and is in signal connection with the input end of the controller, and a second self-regulating valve is in signal connection with the output end of the controller.
3. The system for producing the caustic soda with the high efficiency recycled condensed acid according to claim 2, wherein the brine refining unit comprises the water distribution tank, a membrane filter, a first brine heat exchanger and the chelating resin tower, and a liquid outlet of the water distribution tank is communicated with a liquid inlet of the membrane filter; the liquid outlet of the membrane filter is communicated with the liquid inlet of the first brine heat exchanger, the liquid outlet of the first brine heat exchanger is communicated with the liquid inlet of the chelate resin tower, and the regeneration port of the chelate resin tower is communicated with the liquid outlet of the high-purity hydrochloric acid tank.
4. The system as claimed in claim 3, wherein the anolyte circulating unit comprises the second brine heat exchanger, the chlorate decomposition tank and the dechlorination tower, the liquid outlet of the second brine heat exchanger is communicated with the liquid inlet of the chlorate decomposition tank, the liquid outlet of the chlorate decomposition tank is communicated with the liquid inlet of the dechlorination tower, and the liquid outlet of the dechlorination tower is communicated with the liquid inlet of the water distribution tank of the brine refining unit.
5. The caustic soda production system for efficiently recycling condensed acid according to claim 3, wherein the catholyte circulating unit comprises the caustic soda tank, an evaporation device and the circulating cooler, and a liquid outlet of the caustic soda tank is communicated with a liquid inlet of the evaporation device.
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