CN111501059A - Technological process of thirty-two percent ion membrane caustic soda - Google Patents

Technological process of thirty-two percent ion membrane caustic soda Download PDF

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CN111501059A
CN111501059A CN202010428671.3A CN202010428671A CN111501059A CN 111501059 A CN111501059 A CN 111501059A CN 202010428671 A CN202010428671 A CN 202010428671A CN 111501059 A CN111501059 A CN 111501059A
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brine
caustic soda
chlorine
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thirty
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洪建新
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Nanjing Jiutuo Technology Service Co ltd
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Nanjing Jiutuo Technology Service Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • C25B1/46—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in diaphragm cells
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/24—Cements from oil shales, residues or waste other than slag
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/12—Halogens or halogen-containing compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Electrochemistry (AREA)
  • Metallurgy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Ceramic Engineering (AREA)
  • Structural Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

The invention discloses a technological process of thirty-two percent ion membrane caustic soda, which comprises the following steps: removing natural organic matter impurities from brine water in a brine storage and denitrated low-mango brine through a salt dissolving process; feeding a refining agent to remove some impurity ions in the process that the chemical products with the impurities removed automatically flow through the manger and then are sent to a DrM filter; delivering the filtered refined brine to an ion exchange membrane working section, and electrolyzing by an ion exchange membrane electric tank to generate 32% finished caustic soda, hydrogen, chlorine and light brine; and (3) the light brine is subjected to dechlorination reaction in a dechlorinating tower, after chlorine is removed, the light brine enters a denitration tower to react to generate mirabilite and low-awn brine, and the residual light brine after electrolysis is subjected to dechlorination and denitration to generate low-awn brine which can be used in the salt dissolving step again. The invention can recycle the waste generated after the electrolysis of the ion membrane electric cell, improves the utilization rate of the salt mud, and effectively improves the utilization rate by adopting the salt mud to prepare the ecological cement.

Description

Technological process of thirty-two percent ion membrane caustic soda
Technical Field
The invention relates to the technical field of caustic soda preparation, in particular to a technological process of thirty-two percent ionic membrane caustic soda.
Background
Along with the rapid development of social economy, people have more and more extensive use of caustic soda, the demand for caustic soda is large, sodium hydroxide has a chemical formula of NaOH, is commonly called caustic soda, caustic soda and caustic soda, is strong caustic soda with strong corrosiveness, is generally in a sheet or block shape, is easy to dissolve in water (release heat when dissolved in water) and form an alkaline solution, has deliquescence, is easy to absorb water vapor (deliquescence) and carbon dioxide (deterioration) in air, can be added with hydrochloric acid to check whether deterioration occurs, and has a diaphragm electrolysis method and an ion exchange membrane method in the preparation process, wherein the ion membrane exchange method is to refine brine by a traditional method after primary refined brine is filtered by a sintered carbon tubular filter and then secondarily refined by a chelating ion exchange resin tower to reduce the content of calcium and magnesium in the brine to be below 0.002 percent and electrolyzes the secondary refined brine, chlorine is generated in the anode chamber, Na + in the brine in the anode chamber enters the cathode chamber and OH in the cathode chamber through the ionic membrane to generate sodium hydroxide.
However, the existing ionic membrane caustic soda preparation process is not sufficient for the weak brine after refined salt reaction; thus, the existing requirements are not met, and a process flow of thirty-two percent ion membrane caustic soda is provided for the requirements.
Disclosure of Invention
The invention aims to provide a process flow of thirty-two percent ionic membrane caustic soda, which aims to solve the problems that the conventional ionic membrane caustic soda preparation process in the background art is insufficient in the use of light salt water after refined salt reaction and the like.
In order to achieve the purpose, the invention provides the following technical scheme: a technological process of thirty-two percent ion membrane caustic soda comprises the following steps:
the method comprises the following steps: removing natural organic matter impurities from brine water in a brine storage and denitrated low-mango brine through a salt dissolving process;
step two: feeding a refining agent to remove some impurity ions in the process that the chemical products with the impurities removed automatically flow through the manger, then sending the chemical products to a DrM filter, and filtering out salt mud;
step three: delivering the filtered refined brine to an ion exchange membrane working section, and electrolyzing by an ion exchange membrane electric tank to generate 32% finished caustic soda, hydrogen, chlorine and light brine;
step four: the light brine is subjected to dechlorination reaction in a dechlorination tower, after chlorine is removed, the light brine enters a denitration tower to react to generate mirabilite and low-awn brine, and the residual light brine after electrolysis is subjected to dechlorination and denitration to generate low-awn brine which can be used in the salt dissolving step again;
step five: chlorine gas is sent to a liquid chlorine working procedure for liquefaction after being dried and compressed to produce liquid chlorine;
step six: the hydrogen is dried, compressed and stored in a gas tank and is sent to a hydrogen department for use.
Preferably, the ion exchange membrane electrobath in the third step is a multi-pole type electrobath, the total voltage of the electrobath is the sum of the voltages of all unit electrobaths, all the electrobaths in the circuit are connected in parallel to generate an electrolytic reaction, and the electrolytic reaction formula is as follows:
2NaCl+2H2O＝2NaOH+H2↑+Cl2↑
the H + is directly discharged on the cathode to generate hydrogen. In the electrolysis process, adding a proper amount of high-purity hydrochloric acid into the anode chamber to neutralize the returned OH < - >, adding required pure water into the cathode chamber, and adjusting the temperature of the electrolytic cell to be less than 88 ℃; the power consumption of the caustic soda is less than 2300 KWh; the header hydrogen pressure is less than 2.7mH 2O; the pressure of the chlorine in the header pipe is less than 2.3mH2O, and the bipolar ion exchange membrane electric tank is closed in time after the use, so that the service life of the machine is effectively prolonged.
Preferably, the main indexes of 32% finished product alkali in the third step are as follows: sodium hydroxide is more than or equal to 32 percent, sodium chloride is less than or equal to 0.004 percent, and the generated 32 percent of finished product alkali can be directly used as a liquid alkali product or further decocted to be concentrated to prepare a solid caustic soda finished product.
Preferably, the chlorine gas is dried by using concentrated sulfuric acid with a concentration of 82% in the drying in the fifth step, and after the sulfuric acid is contacted with the wet chlorine gas, the moisture in the chlorine gas is absorbed by the concentrated sulfuric acid with a concentration of 82%.
Preferably, calcium oxide is used for drying in the sixth step, and the reaction formula is as follows:
CaO+H2O＝Ca(OH)2。
preferably, the dechlorination in the fourth step is carried out by a chemical method and a physical method at the same time, the solubility of chlorine in the acidic brine is reduced along with the reduction of the pH value, so the light brine needs to be subjected to acid treatment before dechlorination, and the reaction formula is as follows:
Cl2+H2＝＝HCl+HclO；
since free chlorine in the dilute brine has strong oxidizing property, it can be subjected to redox reaction with reducing substances such as sodium sulfite and the like under alkaline conditions to remove chlorine, and the reaction formula is:
Cl2+NaSO3+2NaOH＝＝NaSO4+2NaCl+H2O。
preferably, the salt mud in the second step is put into a filter press for filter pressing, part of salt water can be further filtered out after filter pressing, the salt water is put into a salt dissolving step for reuse, the utilization rate of the salt mud is improved, and the filtered salt mud is put into calcium chloride for producing ecological cement for relevant departments to use.
Preferably, the physical method specifically adopts an air blowing method, wherein the air blowing method is to introduce a large amount of air into the fresh brine by using an air blower, and the air is fully mixed and contacted with the fresh brine to destroy the equilibrium concentration of a gas-liquid interface, so that chlorine dissolved in a liquid phase is transferred to a gas phase and is taken away by air, and the dechlorination effect is achieved.
Compared with the prior art, the invention has the beneficial effects that:
1. the invention adopts the ion exchange membrane electric tank to electrolyze to prepare the caustic soda, the quality of the caustic soda is high, and the quality requirement of chemical fiber, pharmacy and other industries on the high-purity caustic soda can be met;
2. the energy consumption is low through the ionic membrane caustic soda method, the energy is effectively saved, and the cost is reduced;
3. the chemical method and the physical method are synchronously used when the light salt brine is dechlorinated, so that the dechlorination effect of the light salt brine is effectively improved;
4. the method comprises the steps of drying and compressing hydrogen and chlorine generated by preparing caustic soda by electrolyzing an ion exchange membrane electric tank;
5. the residual fresh brine after electrolysis is subjected to dechlorination and denitration to generate low-mango brine which can be reused in the salt dissolving step, so that the utilization rate is improved;
6. the salt slurry is subjected to filter pressing and further filtered, the salt water is put into the salt dissolving step again, and the excess salt slurry is added with calcium chloride to be used for producing ecological cement for relevant departments to use.
Drawings
FIG. 1 is an overall process flow diagram of the present invention;
FIG. 2 is an electrolytic flow diagram of an ion exchange membrane cell of the present invention;
FIG. 3 is a flow diagram of the dechlorination of the dilute brine of the present invention;
FIG. 4 is a flow chart of the present invention for treating and recycling salty mud.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
Referring to fig. 1-4, an embodiment of the present invention is shown: a technological process of thirty-two percent ion membrane caustic soda comprises the following steps:
the method comprises the following steps: removing natural organic matter impurities from brine water in a brine storage and denitrated low-mango brine through a salt dissolving process;
step two: feeding a refining agent to remove some impurity ions in the process that the chemical products with the impurities removed automatically flow through the manger, then sending the chemical products to a DrM filter, and filtering out salt mud;
step three: delivering the filtered refined brine to an ion exchange membrane working section, and electrolyzing by an ion exchange membrane electric tank to generate 32% finished caustic soda, hydrogen, chlorine and light brine;
step four: the light brine is subjected to dechlorination reaction in a dechlorination tower, after chlorine is removed, the light brine enters a denitration tower to react to generate mirabilite and low-awn brine, and the residual light brine after electrolysis is subjected to dechlorination and denitration to generate low-awn brine which can be used in the salt dissolving step again, so that the utilization rate is improved;
step five: chlorine gas is sent to a liquid chlorine working procedure for liquefaction after being dried and compressed to produce liquid chlorine;
step six: the hydrogen is dried, compressed and stored in a gas tank and is sent to a hydrogen department for use.
Further, the ion exchange membrane electrobath in the third step adopts a multi-pole type electrobath, the total voltage of the electrobath is the sum of the voltages of all unit electrobaths, all the electrobaths in the circuit are connected in parallel to generate an electrolytic reaction, and the electrolytic reaction formula is as follows:
2NaCl+2H2O＝2NaOH+H2↑+Cl2↑
the H + is directly discharged on the cathode to generate hydrogen. In the electrolysis process, adding a proper amount of high-purity hydrochloric acid into the anode chamber to neutralize the returned OH < - >, adding required pure water into the cathode chamber, and adjusting the temperature of the electrolytic cell to be less than 88 ℃; the power consumption of the caustic soda is less than 2300 KWh; the header hydrogen pressure is less than 2.7mH 2O; the pressure of the chlorine in the header pipe is less than 2.3mH2O, and the bipolar ion exchange membrane electric tank is closed in time after the use, so that the service life of the machine is effectively prolonged.
Further, the main indexes of 32% finished product alkali in the third step are as follows: sodium hydroxide is more than or equal to 32 percent, sodium chloride is less than or equal to 0.004 percent, and the generated 32 percent of finished product alkali can be directly used as a liquid alkali product or further decocted to be concentrated to prepare a solid caustic soda finished product.
Further, in the step five, the chlorine gas is dried by using concentrated sulfuric acid with the concentration of 82%, and after the sulfuric acid is contacted with the wet chlorine gas, the water in the chlorine gas is absorbed by the concentrated sulfuric acid with the concentration of 82%.
Further, calcium oxide is adopted for drying in the sixth step, and the reaction formula is as follows:
CaO+H2O＝Ca(OH)2。
furthermore, in the fourth step, the dechlorination is carried out efficiently by adopting a chemical method and a physical method, the solubility of chlorine in the acidic brine is reduced along with the reduction of the pH value, so the light brine needs to be treated by adding acid before dechlorination, and the reaction formula is as follows:
Cl2+H2＝＝HCl+HclO；
since free chlorine in the dilute brine has strong oxidizing property, it can be subjected to redox reaction with reducing substances such as sodium sulfite and the like under alkaline conditions to remove chlorine, and the reaction formula is:
Cl2+NaSO3+2NaOH＝＝NaSO4+2NaCl+H2O。
and further, the salt mud in the step two is put into a filter press for filter pressing, partial salt water can be further filtered out after filter pressing, the salt water is put into a salt dissolving process for recycling, the utilization rate of the salt mud is improved, and the filtered salt mud is put into calcium chloride for producing ecological cement for relevant departments to use.
Further, the physical method specifically adopts an air blowing method, the air blowing method is that a large amount of air is blown into the fresh brine by an air blower and is fully mixed and contacted with the fresh brine, the equilibrium concentration of a gas-liquid interface is destroyed, and chlorine dissolved in a liquid phase is transferred to a gas phase and taken away by air, so that the dechlorination effect is achieved, and the chemical method and the physical method are synchronously used when the dechlorination is carried out on the fresh brine, so that the dechlorination effect of the fresh brine is effectively improved.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.

Claims (8)

1. A technological process of thirty-two percent ion membrane caustic soda comprises the following steps:
the method comprises the following steps: removing natural organic matter impurities from brine water in a brine storage and denitrated low-mango brine through a salt dissolving process;
step two: feeding a refining agent to remove some impurity ions in the process that the chemical products with the impurities removed automatically flow through the manger, then sending the chemical products to a DrM filter, and filtering out salt mud;
step three: delivering the filtered refined brine to an ion exchange membrane working section, and electrolyzing by an ion exchange membrane electric tank to generate 32% finished caustic soda, hydrogen, chlorine and light brine;
step four: the light brine is subjected to dechlorination reaction in a dechlorination tower, after chlorine is removed, the light brine enters a denitration tower to react to generate mirabilite and low-awn brine, and the residual light brine after electrolysis is subjected to dechlorination and denitration to generate low-awn brine which can be used in the salt dissolving step again;
step five: chlorine gas is sent to a liquid chlorine working procedure for liquefaction after being dried and compressed to produce liquid chlorine;
step six: the hydrogen is dried, compressed and stored in a gas tank and is sent to a hydrogen department for use.
2. The process of thirty-two percent ionic membrane caustic soda as claimed in claim 1, wherein: the ion exchange membrane electrobath in the third step adopts a multi-pole type electrobath, the total voltage of the electrobath is the sum of the voltages of all unit electrobaths, all the electrobaths in the circuit are connected in parallel to generate an electrolytic reaction, and the electrolytic reaction formula is as follows:
2NaCl+2H2O＝2NaOH+H2↑+Cl2↑
the H + is directly discharged on the cathode to generate hydrogen. In the electrolysis process, adding a proper amount of high-purity hydrochloric acid into the anode chamber to neutralize the returned OH < - >, adding required pure water into the cathode chamber, and adjusting the temperature of the electrolytic cell to be less than 88 ℃; the power consumption of the caustic soda is less than 2300 KWh; the header hydrogen pressure is less than 2.7mH 2O; the pressure of the chlorine in the header pipe is less than 2.3mH2O, and the bipolar ion exchange membrane electric tank is closed in time after the use, so that the service life of the machine is effectively prolonged.
3. The process of thirty-two percent ionic membrane caustic soda as claimed in claim 1, wherein: the main indexes of 32 percent of finished product alkali in the third step are as follows: sodium hydroxide is more than or equal to 32 percent, sodium chloride is less than or equal to 0.004 percent, and the generated 32 percent of finished product alkali can be directly used as a liquid alkali product or further decocted to be concentrated to prepare a solid caustic soda finished product.
4. The process of thirty-two percent ionic membrane caustic soda as claimed in claim 1, wherein: and in the step five, the chlorine gas is dried by adopting concentrated sulfuric acid with the concentration of 82%, and after the sulfuric acid is contacted with the wet chlorine gas, the water in the chlorine gas is absorbed by the concentrated sulfuric acid with the concentration of 82%.
5. The process of thirty-two percent ionic membrane caustic soda as claimed in claim 4, wherein: the drying in the sixth step adopts calcium oxide, and the reaction formula is as follows:
CaO+H2O＝Ca(OH)2。
6. the process of thirty-two percent ionic membrane caustic soda as claimed in claim 1, wherein: in the fourth step, the dechlorination is carried out efficiently by adopting a chemical method and a physical method, the solubility of chlorine in the acidic brine is reduced along with the reduction of the pH value, so the light brine needs to be treated by adding acid before dechlorination, and the reaction formula is as follows:
Cl2+H2＝＝HCl+HclO；
since free chlorine in the dilute brine has strong oxidizing property, it can be subjected to redox reaction with reducing substances such as sodium sulfite and the like under alkaline conditions to remove chlorine, and the reaction formula is:
Cl2+NaSO3+2NaOH＝＝NaSO4+2NaCl+H2O。
7. the process of thirty-two percent ionic membrane caustic soda as claimed in claim 1, wherein: and D, putting the salt slurry obtained in the step II into a filter press for filter pressing, further filtering out partial salt water after filter pressing, putting the salt water into a salt dissolving process for reuse, improving the utilization rate of the salt slurry, and putting the filtered salt slurry into calcium chloride for producing ecological cement for relevant departments to use.
8. The process of thirty-two percent ionic membrane caustic soda as claimed in claim 6, wherein: the physical method specifically adopts an air blowing method, wherein the air blowing method is to utilize an air blower to introduce a large amount of air into the fresh brine, and the air is fully mixed and contacted with the fresh brine to destroy the equilibrium concentration of a gas-liquid interface, so that chlorine dissolved in a liquid phase is transferred to a gas phase and is taken away by the air, and the dechlorination effect is achieved.
CN202010428671.3A 2020-05-20 2020-05-20 Technological process of thirty-two percent ion membrane caustic soda Withdrawn CN111501059A (en)

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Application publication date: 20200807