WO2022254878A1 - 次亜塩素酸ナトリウム溶液の製造方法および製造装置 - Google Patents
次亜塩素酸ナトリウム溶液の製造方法および製造装置 Download PDFInfo
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- WO2022254878A1 WO2022254878A1 PCT/JP2022/012034 JP2022012034W WO2022254878A1 WO 2022254878 A1 WO2022254878 A1 WO 2022254878A1 JP 2022012034 W JP2022012034 W JP 2022012034W WO 2022254878 A1 WO2022254878 A1 WO 2022254878A1
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- Prior art keywords
- sodium hypochlorite
- hypochlorite solution
- producing
- anolyte
- salt
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- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 title claims abstract description 185
- 239000005708 Sodium hypochlorite Substances 0.000 title claims abstract description 184
- 238000000034 method Methods 0.000 title abstract description 36
- 239000000243 solution Substances 0.000 claims abstract description 194
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 168
- 150000003839 salts Chemical class 0.000 claims abstract description 151
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 136
- 238000006243 chemical reaction Methods 0.000 claims abstract description 87
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims abstract description 63
- 239000008213 purified water Substances 0.000 claims abstract description 46
- 239000000460 chlorine Substances 0.000 claims abstract description 45
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 44
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 43
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 40
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 38
- 239000007864 aqueous solution Substances 0.000 claims abstract description 37
- 239000012267 brine Substances 0.000 claims abstract description 33
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical group O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 33
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 27
- 239000003014 ion exchange membrane Substances 0.000 claims abstract description 24
- 239000011780 sodium chloride Substances 0.000 claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 claims description 85
- 238000003860 storage Methods 0.000 claims description 25
- 238000005341 cation exchange Methods 0.000 claims description 17
- 239000013522 chelant Substances 0.000 claims description 16
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 12
- 239000003729 cation exchange resin Substances 0.000 claims description 12
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 claims description 10
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 claims description 7
- 150000001732 carboxylic acid derivatives Chemical class 0.000 claims description 7
- 239000012528 membrane Substances 0.000 claims description 7
- 230000005484 gravity Effects 0.000 claims description 3
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 claims description 2
- 239000003012 bilayer membrane Substances 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 17
- 230000009920 chelation Effects 0.000 abstract description 3
- 235000002639 sodium chloride Nutrition 0.000 description 153
- XTEGARKTQYYJKE-UHFFFAOYSA-N chloric acid Chemical compound OCl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-N 0.000 description 16
- 229940005991 chloric acid Drugs 0.000 description 16
- 239000010410 layer Substances 0.000 description 15
- 238000006298 dechlorination reaction Methods 0.000 description 13
- 230000000052 comparative effect Effects 0.000 description 11
- 239000012535 impurity Substances 0.000 description 8
- 238000000746 purification Methods 0.000 description 7
- SXDBWCPKPHAZSM-UHFFFAOYSA-N bromic acid Chemical compound OBr(=O)=O SXDBWCPKPHAZSM-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 5
- 239000011575 calcium Substances 0.000 description 5
- 229910052791 calcium Inorganic materials 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 5
- 229910052749 magnesium Inorganic materials 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 229940006460 bromide ion Drugs 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- 239000012670 alkaline solution Substances 0.000 description 3
- 229910001424 calcium ion Inorganic materials 0.000 description 3
- 239000003518 caustics Substances 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- SXDBWCPKPHAZSM-UHFFFAOYSA-M bromate Inorganic materials [O-]Br(=O)=O SXDBWCPKPHAZSM-UHFFFAOYSA-M 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- -1 hydrogen ions Chemical class 0.000 description 2
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 235000010265 sodium sulphite Nutrition 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 235000020679 tap water Nutrition 0.000 description 2
- 239000010936 titanium Substances 0.000 description 2
- 229910052719 titanium Inorganic materials 0.000 description 2
- 229920003934 Aciplex® Polymers 0.000 description 1
- 229920003935 Flemion® Polymers 0.000 description 1
- 229920000557 Nafion® Polymers 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 206010039203 Road traffic accident Diseases 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 229910001514 alkali metal chloride Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 239000007844 bleaching agent Substances 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000006182 cathode active material Substances 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910001902 chlorine oxide Inorganic materials 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 239000000645 desinfectant Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 239000008151 electrolyte solution Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- NBZBKCUXIYYUSX-UHFFFAOYSA-N iminodiacetic acid Chemical compound OC(=O)CNCC(O)=O NBZBKCUXIYYUSX-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 235000015598 salt intake Nutrition 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 239000008234 soft water Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000009875 water degumming Methods 0.000 description 1
- 235000020681 well water Nutrition 0.000 description 1
- 239000002349 well water Substances 0.000 description 1
Images
Classifications
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- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
- C02F1/4674—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation with halogen or compound of halogens, e.g. chlorine, bromine
-
- 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
- C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
-
- 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
- C25B1/24—Halogens or compounds thereof
- C25B1/26—Chlorine; Compounds thereof
-
- 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
- C25B13/00—Diaphragms; Spacing elements
- C25B13/04—Diaphragms; Spacing elements characterised by the material
- C25B13/08—Diaphragms; Spacing elements characterised by the material based on organic materials
-
- 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
- C25B15/02—Process control or regulation
-
- 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
-
- 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
- C25B9/13—Single electrolytic cells with circulation of an electrolyte
-
- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/46115—Electrolytic cell with membranes or diaphragms
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4618—Supplying or removing reactants or electrolyte
Definitions
- the present invention relates to a sodium hypochlorite solution manufacturing method and a sodium hypochlorite solution manufacturing apparatus (hereinafter also simply referred to as “manufacturing method” and “manufacturing apparatus”). More specifically, the present invention uses an ion exchange membrane for the diaphragm of the electrolytic cell, and mixes the electrolysis products excluding hydrogen generated in the electrolytic cell in the reaction vessel to produce a sodium hypochlorite solution on-site. A method and apparatus for obtaining higher concentrations of sodium hypochlorite.
- Sodium hypochlorite is used as a representative bleaching agent and disinfectant in various fields, such as water and sewage treatment and wastewater treatment.
- a method for producing sodium hypochlorite there is a method in which chlorine obtained by electrolysis of saline water is reacted with an aqueous sodium hydroxide solution in a reaction tank, and an aqueous sodium chloride solution is electrolyzed in a non-diaphragm electrolytic tank.
- a common method is to decompose and directly produce sodium hypochlorite in a non-diaphragm electrolytic cell.
- a typical example of the application to which the former manufacturing method is applied is the method of manufacturing high-concentration sodium hypochlorite in a salt electrolysis plant.
- the salt electrolysis plant in order to maintain stable and highly efficient plant operation, a salt water refining system that removes metal impurities and unnecessary anions contained in the raw salt and raw water to a high degree, and salt that has been reduced in concentration after electrolysis
- a system for decomposing and removing the hypochlorous acid and chloric acid contained in the salt water after electrolysis and repurifying it is essential, and the equipment becomes large-scale.
- salt electrolysis plants The main purpose of salt electrolysis plants is not the production of sodium hypochlorite, but the production of sodium hydroxide and chlorine gas, which have many industrial uses. Many large-scale plants produce tens of thousands to hundreds of thousands of tons per year in terms of sodium. The number of salt electrolysis plants is overwhelmingly small compared to the number of water supply plants that require high-concentration sodium hypochlorite. must be transported to the waterworks and stored. For this reason, there is always the danger of human disasters and environmental destruction due to liquid leakage from storage facilities. In particular, with regard to chlorine gas, there have been major accidents in many countries where tank trucks used for transportation have been involved in traffic accidents, causing chlorine gas to scatter into the environment.
- Patent Document 1 an electrolytic cell in which a cation exchange membrane is provided between the anode and cathode is used, electrolysis is performed while adding an alkaline chloride solution to the anode chamber and water to the cathode chamber, and the electrolyte is discharged from the electrolytic cell.
- a technique for producing an alkaline hypochlorite solution having a predetermined effective chlorine concentration by mixing an anolyte, a catholyte that is a caustic alkaline solution, and chlorine gas is described.
- Patent Document 2 in an electrolytic cell divided into an anode chamber and a cathode chamber by an ion exchange membrane, an aqueous alkali metal chloride solution is supplied to the anode chamber and pure water is supplied to the cathode chamber to perform electrolysis, and electricity is generated.
- salt or chloride is used as the ion exchange membrane.
- an ion exchange membrane for generating high-concentration caustic alkali for potassium electrolysis, the anolyte or alkali metal hydroxide aqueous solution before being introduced into the reaction tank, or the anolyte, chlorine gas and alkali metal introduced into the reaction tank Techniques for adding water to a mixture of aqueous hydroxide solutions have been described.
- sodium hypochlorite is produced by reacting chlorine gas obtained by electrolyzing salt water with sodium hydroxide.
- Salt water which is the anolyte, is circulated between the anode chamber of the electrolytic cell and the anolyte storage tank, and at the same time, secondary salt water purified by a brine purifier is supplied to the anode chamber, the anolyte circulation pipe, or the anolyte storage tank. be done.
- purified water is supplied to the cathode chamber, the catholyte circulation pipe, or the catholyte reservoir at the same time that the sodium hydroxide aqueous solution, which is the catholyte, is circulated between the cathode chamber and the catholyte reservoir of the electrolytic cell.
- a sodium hypochlorite solution is generated in the reaction tank by the reaction between sodium hydroxide generated in the electrolytic tank and chlorine gas.
- the effective chlorine concentration is high, and salt A low concentration sodium hypochlorite solution can be easily generated.
- the salt decomposition rate is about 40%.
- the salt water discharged from the anode chamber, in which salt has been consumed by electrolysis, is reused through a dechlorination process.
- the dechlorination process uses large amounts of chemicals such as hydrochloric acid, aqueous sodium hydroxide solution, and sodium sulfite, and there are many types of equipment such as tanks and pumps for these chemicals. Therefore, when this facility is applied to an on-site sodium hypochlorite production facility, there is a problem that the footprint, initial cost, and running cost become high.
- an anolyte that is an alkaline chloride solution discharged from an electrolytic cell using a cation exchange membrane, a catholyte that is a caustic alkaline solution, and chlorine gas are mixed.
- a hypochlorite alkaline solution with an effective chlorine concentration of 2 to 6% by mass. Since the anolyte is mixed with the catholyte and chlorine gas into the alkaline hypochlorite solution, a dechlorination process is not required.
- the sodium hypochlorite solution is diluted by the anolyte, and the concentration of the sodium hydroxide aqueous solution generated at the cathode is low, so the effective chlorine concentration in the sodium hypochlorite solution is increased. I can't.
- the chlorine gas discharged from the anode chamber and the cathode chamber separated by an ion exchange membrane, the anolyte, and the catholyte are reacted in a reaction tank to produce hypochlorous acid. It is possible to produce sodium. Also in this method, the dechlorination step is not required as in Patent Document 1.
- the sodium hydroxide aqueous solution generated at the cathode has a high concentration, and a sodium hypochlorite solution with a higher effective chlorine concentration than that in Patent Document 1 can be generated. is consumed and flows into the reaction tank, a sodium hypochlorite solution with a low salt concentration cannot be produced.
- the chloric acid contained in the anolyte is also mixed with the sodium hypochlorite solution, compared to the method of contacting chlorine gas with an aqueous sodium hydroxide solution, a sodium hypochlorite solution with a high chloric acid concentration is used. It also has the drawback that it can only generate
- the grade of sodium hypochlorite solution is defined by the concentration of available chlorine, free alkali, bromic acid, chloric acid and salt. It is Class 3 sodium hypochlorite, which has an effective chlorine concentration of 12% or more, is regulated to have a salt concentration of 12.5% or less. Therefore, when a user requests sodium hypochlorite equivalent to class 3, the problem is that the method shown in Patent Document 2 cannot be used.
- the object of the present invention is to solve the above problems and to manufacture a sodium hypochlorite solution with a high effective chlorine concentration at low cost by on-site equipment. is to provide
- the salt water supplied to the anolyte contains impurities caused by raw salt.
- Calcium and magnesium which are typical impurities among them, can be removed by a brine purifier.
- bromine contained in raw salt cannot be removed by a brine purifier and is mixed in the anolyte and sodium hypochlorite solution as carcinogenic bromic acid.
- Standard values are also provided in the sodium hypochlorite section for water supply in the Water Works Association Standard (JWWA K120:2008). Therefore, in order to increase the salt decomposition rate, selection of an appropriate raw salt is also an issue.
- the present inventors have made intensive studies, and as a result, have improved the process of producing an aqueous sodium chloride solution from raw salt, and the reaction of the anolyte obtained by electrolysis, chlorine gas, and aqueous sodium hydroxide solution.
- By increasing the salt decomposition rate when producing a sodium hypochlorite solution in a reaction tank it is possible to produce a high-concentration sodium hypochlorite solution, and completed the present invention. came to.
- the method for producing a sodium hypochlorite solution of the present invention comprises supplying secondary salt water, which is an aqueous sodium chloride solution, to the anode chamber of an electrolytic cell partitioned into an anode chamber and a cathode chamber by an ion exchange membrane,
- the anolyte, chlorine gas and produced chlorine gas in the anode chamber after electrolysis and the aqueous sodium hydroxide solution produced in the cathode chamber are introduced into the reaction vessel to form the anolyte, chlorine gas and catholyte in the reaction vessel.
- a two-layer membrane composed of a sulfonic acid layer and a carboxylic acid layer is preferable to use as the ion exchange membrane.
- first switching means for switching whether or not the anode solution is introduced from the anode chamber to the reaction chamber is provided between the anode chamber and the reaction chamber, It is preferable to produce the sodium hypochlorite solution without introducing part or all of the anolyte into the reaction vessel, and between the anode chamber and the reaction vessel, the chlorine gas is introduced from the anode chamber. It is also preferable to provide a second switching means for switching whether or not to introduce the chlorine gas into the reaction tank, and to produce the sodium hypochlorite solution while supplying part or all of the chlorine gas to the facility using chlorine gas.
- two or more of the electrolytic cells are used, and the chlorine gas obtained from the one or more electrolytic cells is supplied to a facility using chlorine gas, and the one or more electrolytic cells are used.
- Said chlorine gas obtained from the tank can be used to produce a sodium hypochlorite solution.
- the effective chlorine concentration of the sodium hypochlorite solution produced in the reaction tank can be 8% or more.
- the production method of the present invention preferably includes a cation exchange step of treating raw water with a cation exchange resin to produce the purified water.
- a water softener in the cation exchange step.
- the first switching means and/or the second switching means are operated by a switch operation or an external signal based on instructions from an automatic control device capable of communicating with the outside of the manufacturing facility. can be activated.
- the sodium hypochlorite solution can be produced on-site near the facility where the sodium hypochlorite solution is used.
- an anolyte storage tank for storing the anolyte and a catholyte storage tank for storing the catholyte are provided near the electrolytic cell, and the anolyte storage tank and the cathode are provided in the vicinity of the electrolytic cell.
- the apparatus for producing a sodium hypochlorite solution of the present invention comprises an electrolytic cell which is partitioned into an anode chamber and a cathode chamber by an ion exchange membrane, is supplied with a secondary salt water which is an aqueous sodium chloride solution, and the anode after electrolysis.
- the apparatus for producing a sodium hypochlorite solution by reaction in the reaction vessel a primary salt water generation unit that dissolves raw salt containing sodium chloride as a main component in purified water to generate primary salt water; a chelate processing unit that chelates the primary salt water to generate the secondary salt water, It is characterized in that it is operated with a salt decomposition rate in the range of 80 to 95%.
- the ion exchange membrane is a two-layer membrane composed of a sulfonic acid layer and a carboxylic acid layer.
- a first switching means is provided between the anode chamber and the reaction vessel for switching whether or not the anolyte in the anode chamber is introduced from the anode chamber to the reaction vessel.
- a second switching means is provided between the anode chamber and the reaction vessel for switching whether chlorine gas generated in the anode chamber is introduced from the anode chamber to the reaction vessel. preferable.
- the production apparatus of the present invention is equipped with two or more of the electrolytic cells, and has a chlorine gas supply path for supplying chlorine gas obtained from one or more of the electrolytic cells to facilities using chlorine gas.
- the production apparatus of the present invention preferably has a purified water introduction path for introducing purified water into the reaction vessel.
- the production apparatus of the present invention is suitably used for producing a sodium hypochlorite solution having an available chlorine concentration of 8% or more.
- the manufacturing apparatus of the present invention includes a cation exchange treatment section that treats raw water with a cation exchange resin to generate the purified water.
- the cation exchange treatment section is composed of a water softener.
- the first switching means and/or the second switching means can be operated by a switch operation or an external signal via an automatic control device capable of communicating with the outside of the manufacturing facility.
- an automatic control device capable of communicating with the outside of the manufacturing facility.
- the production apparatus of the present invention is preferably installed in the vicinity of a sodium hypochlorite solution usage facility and used for on-site production of sodium hypochlorite solution.
- an anolyte storage tank for storing an anolyte and a catholyte storage tank for storing a catholyte are provided in the vicinity of the electrolytic cell, and the anolyte storage tank and the catholyte are It is preferable that the bottom of the reservoir is located above the 1/2 height of the electrolytic cell.
- the present invention it is possible to provide a sodium hypochlorite solution manufacturing method and manufacturing apparatus capable of manufacturing a sodium hypochlorite solution with a high available chlorine concentration at low cost using on-site equipment.
- FIG. 2 is a configuration diagram schematically showing another form of an apparatus for producing a sodium hypochlorite solution used in the present invention
- 4 is a graph showing the relationship between the salt unit consumption ratio and the salt decomposition rate in the present invention, with reference to a sodium hypochlorite solution manufacturing apparatus having a dechlorination process.
- FIG. 1 is an apparatus configuration diagram showing an example of a sodium hypochlorite solution manufacturing apparatus used in the present invention.
- FIG. 2 is an apparatus configuration diagram schematically showing another form of the apparatus for producing a sodium hypochlorite solution used in the present invention.
- the present invention relates to an improvement of a method and apparatus capable of producing a sodium hypochlorite solution on-site in the vicinity of a sodium hypochlorite solution usage facility.
- secondary salt water which is an aqueous sodium chloride solution
- the salt decomposition rate is set in the range of 80 to 95%, and the secondary salt water supplied to the anode chamber is generated from the raw salt. is dissolved to produce primary brine (primary brine production step), and then the primary brine is subjected to chelate treatment to produce secondary brine (chelate treatment step).
- primary brine production step primary brine production step
- chelate treatment step secondary brine
- the salt decomposition rate when producing a sodium hypochlorite solution needs to be in the range of 80-95%, preferably 82-93%. If the salt decomposition rate is less than 80%, it is difficult to produce a high-concentration sodium hypochlorite solution when sodium hypochlorite is produced by introducing the anolyte into the reaction tank without draining it. becomes. Further, as will be described in detail below, if the salt decomposition rate is less than 80% when sodium hypochlorite is produced while the anolyte is drained, economic efficiency cannot be ensured. On the other hand, if the salt decomposition rate exceeds 95%, the voltage of the apparatus will increase significantly regardless of whether the anolyte is introduced into the reaction tank or drained, and the operation cannot be continued substantially. Gone.
- the drained anolyte when draining the anolyte without introducing it into the reaction tank, the drained anolyte has a temperature of 50°C to 80°C, a pH of 4 to 5, and chlorine gas dissolved therein. It is not preferable to send the anolyte as it is to the waste water treatment facility from the viewpoint of the heat resistance of the facility and the generation of chlorine odor. Therefore, when the anolyte is drained, it is necessary to aerate it to drive out the chlorine, and send it to the waste water treatment facility after undergoing processes such as cooling and pH adjustment. Therefore, in consideration of economy, it is preferable to increase the salt decomposition rate and reduce the amount of wastewater.
- the dechlorination process uses large amounts of chemicals such as hydrochloric acid, aqueous sodium hydroxide solution, and sodium sulfite. There will be more devices such as Therefore, when this facility is applied to an on-site sodium hypochlorite production facility, the footprint becomes large, and the initial cost and running cost increase. In the present invention, since the dechlorination process is not used, the associated equipment and chemicals are not used, so the footprint, initial cost, and running cost can be suppressed. Since it is mixed with the sodium hypochlorite solution, which is the product, or is discharged outside the system by being discharged, the unit consumption of salt increases.
- FIG. 3 is a graph showing the relationship between the basic unit ratio of salt and the decomposition rate of salt in the present invention, based on a sodium hypochlorite solution manufacturing apparatus having a dechlorination process. According to FIG. 3, it is necessary to increase the salt decomposition rate to 80% or more in order to reduce the increase in the unit consumption of salt to 25% or less compared to equipment having a dechlorination process.
- the generation of the secondary brine in the present invention is carried out by providing a brine production unit for producing the secondary brine from the raw salt, which is attached to the main part of the sodium hypochlorite solution production apparatus. It can be a compact manufacturing plant that can be used on-site.
- the salt water production unit according to the present invention includes a primary salt water generation unit that dissolves raw salt, the main component of which is sodium chloride, in purified water to generate primary salt water; and a chelate processing unit for generating secondary salt water by performing as a basic configuration.
- the secondary salt water A when the secondary salt water A is generated, first, the raw salt G containing sodium chloride as a main component is dissolved in the purified water B, and the primary salt water is saturated salt water at room temperature. Generate H.
- the raw salt G can be dissolved in the purified water B in the salt dissolving tank 30 .
- raw salt G either sun-dried salt or rock salt may be used. It is more preferable to use the raw salt G as a raw material and further refine it to remove metal impurities such as calcium ions and magnesium ions to some extent to use a refined salt.
- Calcium and magnesium which are typical impurities in salt water, reduce the performance of ion exchange membranes, so the salt water supplied to the anode compartment is purified to reduce the concentration of impurities to a level that meets the standards for use of ion exchange membranes.
- a chelate resin may be used to remove cations such as calcium and magnesium.
- the bromide ion concentration in the raw salt is preferably less than 100 mg/kg, particularly about 69 mg/kg or less.
- the purified water B a commonly used industrial purified water may be used, and prior to the primary salt water generation unit, the raw water is treated with a cation exchange resin to produce purified water.
- the purified water B generated from the raw water I in the on-site facility may be used. That is, the present invention may include a cation exchange step of treating raw water I with a cation exchange resin to produce purified water prior to the primary salt water production step. Through this cation exchange step, calcium ions, magnesium ions and other heavy metal ions contained in the raw water are removed by adsorption and replaced with sodium ions and hydrogen ions, resulting in soft water with a lower hardness than raw water I. Purified water B can be obtained.
- raw water I used in the cation exchange process tap water, well water (ground water), industrial water, etc. available at the on-site manufacturing site near the facility where the sodium hypochlorite solution is used are used. can be used.
- the cation exchange resin used in the cation exchange step is not particularly limited, and may be Na type or H type.
- a water softener using a cation exchange resin can also be used as the cation exchange treatment unit 40 for performing the cation exchange step, instead of using the cation exchange resin alone.
- Regeneration of the degraded cation exchange resin may be performed by replacing the deteriorated cation exchange resin with a new cation exchange resin. Regeneration mechanisms and methods of regeneration using salts may also be used.
- the secondary salt water A is produced by subjecting the primary salt water H obtained in the above steps to a chelate treatment.
- a chelate treatment By subjecting the primary salt water H to a chelate treatment, the calcium ions and magnesium ions brought in from the raw salt G can be removed from the primary salt water, and a clean secondary salt water A can be produced.
- the chelation treatment of the primary brine H can be performed in the brine purifier 50 .
- the manufacturing process of the sodium hypochlorite solution in the present invention will be explained.
- Purified water B is supplied to chamber 3 to perform electrolysis. Thereafter, the anolyte C and the generated chlorine (Cl 2 ) gas D in the anode chamber 2 after electrolysis and the generated sodium hydroxide aqueous solution E in the cathode chamber 3 are introduced into the reaction vessel 20, and A sodium hypochlorite solution F is produced by the reaction of anolyte C, chlorine gas D and aqueous sodium hydroxide solution E at .
- the anolyte C is, for example, salt water whose concentration has been reduced to less than 100 g/liter after electrolysis.
- a sodium hypochlorite solution with a high available chlorine concentration can be stably and efficiently produced at a low cost in an on-site compact production facility.
- Sodium hypochlorite can be easily produced at the place where sodium hypochlorite is consumed.
- the sodium hypochlorite solution produced is diluted, so the available chlorine concentration cannot be increased. Therefore, it is necessary to reduce the amount of water in the reaction tank 20 by increasing the concentration of the aqueous sodium hydroxide solution E, which is the catholyte, and increase the concentration of the sodium hypochlorite solution.
- the concentration of the sodium hydroxide aqueous solution must be at least 22% by mass or more. was there.
- the concentration range of the aqueous sodium hydroxide solution when the anolyte C is introduced into the reaction tank 20 is preferably 22 to 30% by mass.
- the concentration of the sodium hydroxide aqueous solution must be at least 16% by mass or more. It was necessary to By increasing the concentration of the sodium hydroxide aqueous solution, the sodium hypochlorite solution can be made highly concentrated. However, when the concentration of the aqueous sodium hydroxide solution exceeds 23% by mass, salts may precipitate in the sodium hypochlorite solution. For this reason, the concentration range of the sodium hydroxide aqueous solution when the anolyte C is introduced into the reaction tank 20 is preferably 16 to 23% by mass.
- a first switching means 4 for switching whether or not to introduce the anolyte C from the anode chamber 2 into the reaction chamber 20 is provided between the anode chamber 2 and the reaction chamber 20. It is preferable to provide a sodium hypochlorite solution, thereby making it possible to produce a sodium hypochlorite solution without introducing part or all of the anolyte C into the reaction vessel 20 .
- the first switching means 4 capable of controlling the introduction of the anolyte C in this way, it is possible to select and manufacture sodium hypochlorite solutions with different salt concentrations and chloric acid concentrations as required. Become.
- a second switching means 5 for switching whether to introduce the chlorine gas D from the anode chamber 2 to the reaction chamber 20 can be provided between the anode chamber 2 and the reaction chamber 20, As a result, a sodium hypochlorite solution can be produced while part or all of the chlorine gas D is being supplied to the facility using chlorine gas.
- the second switching means 5 that can control the introduction of the chlorine gas D in this way, it is possible to manufacture the sodium hypochlorite solution while supplying the chlorine gas D to the facility where it is used on demand. becomes.
- the first and second switching means 4, 5 are configured by manual valves, electric valves, air-driven valves, or the like.
- these first and second switching means 4, 5 can communicate with the outside of the manufacturing facility. It can be configured to be operable by a switch operation or an external signal based on instructions from an automatic control device. Examples of such an automatic control device include the MELSEC-Q series manufactured by Mitsubishi Electric Corporation and SIMATIC S7 manufactured by SIEMENS, but are not limited to these.
- the automatic control device when manufacturing a sodium hypochlorite solution as one facility of a water treatment plant such as a water purification plant, the automatic control device can be operated based on an external signal from the central control system of the water treatment plant.
- the first switching means 4 according to the measurement results of sodium hypochlorite solution and salt concentration
- the second switching means 5 according to the necessity of injecting chlorine gas into the treated water, on-site It may be operated by an operator using a field switch or the like.
- a purified water introduction path for introducing purified water B into the reaction tank 20, so that when the sodium hypochlorite solution is generated in the reaction tank 20, the reaction tank Purified water B can be supplied to 20 to adjust the concentration of the sodium hypochlorite solution.
- the concentrations of the anolyte C and the sodium hydroxide aqueous solution E, which is the catholyte are combined, purified water B is supplied, and the effective chlorine concentration is It can be 8%.
- the effective chlorine concentration is high, the amount of chloric acid generated due to its decomposition increases.
- Diluting the sodium hypochlorite solution is effective in suppressing an increase in the concentration of chloric acid in hot regions or in summer, when sodium hypochlorite decomposes quickly.
- a sodium hypochlorite solution with an effective chlorine concentration of 1 to 8% it is possible to use a single-layer ion exchange membrane composed of a sulfonic acid layer that is highly resistant to impurities in salt water.
- the use of purified salt with few impurities can simplify the process of purifying brine.
- a sodium hypochlorite solution having an effective chlorine concentration of 8% or more, particularly 12 to 15%, can be easily produced in the reaction tank 20.
- an anolyte storage tank 6 for storing an anolyte C and a catholyte storage tank 7 for storing an aqueous sodium hydroxide solution E as a catholyte are provided in the vicinity of an electrolytic cell 10. It is preferable to arrange the bottoms 6b and 7b of the liquid storage tank 6 and the catholyte storage tank 7 above the 1/2 height position of the electrolytic cell 10 . With such an arrangement, the anolyte storage tank 6 and the anode chamber 2 and the catholyte storage tank 7 and the cathode chamber 3 are communicated with each other by pipes, thereby eliminating the need to provide flow means such as a pump.
- anolyte C and the aqueous sodium hydroxide solution E can be circulated between the anolyte reservoir 6 and the anode chamber 2, and between the catholyte reservoir 7 and the cathode chamber 3, respectively, by gravity difference. .
- flow means such as a pump may be further provided, and is not limited.
- any material may be used as the ion exchange membrane 1 in the electrolytic cell 10, but a two-layer membrane composed of a sulfonic acid layer (anode side) and a carboxylic acid layer (cathode side) is used. is preferred.
- the carboxylic acid layer suppresses the diffusion of hydroxide ions diffusing from the cathode side, so highly efficient production becomes possible.
- Examples of such a bilayer film include Nafion (registered trademark) N2050 manufactured by Chemours, Flemion (registered trademark) F-9010 manufactured by AGC, and Aciplex (registered trademark) F7001 manufactured by Asahi Kasei.
- the anode chamber 2 of the electrolytic cell 10 partitioned by the ion exchange membrane 1 is coated with an electrode catalyst material containing an oxide of a platinum group metal on a metal substrate such as titanium.
- An anode can be provided having a formed thereon.
- the cathode chamber 3 is provided with a cathode made of nickel, stainless steel, or titanium, or formed by coating these metals with a cathode active material that reduces the hydrogen overvoltage and has excellent long-term durability. be able to.
- the sodium hydroxide aqueous solution E can be supplied to the electrolytic cell 10 while controlling the concentration and flow rate according to the desired production amount of the sodium hypochlorite solution. Further, when the purified water B is introduced into the electrolytic cell 10, the flow rate of the purified water B can be similarly controlled according to the target production amount and concentration of the sodium hypochlorite solution.
- the generated aqueous sodium hydroxide solution E and hydrogen gas K are taken out. be. Further, from the upper part of the anode chamber 2, an anolyte C composed of an aqueous sodium chloride solution whose concentration has been lowered by electrolysis and a chlorine gas D are taken out through first and second switching means 4 and 5, respectively. , is supplied to the reaction vessel 20 .
- the reaction tank 20 chlorine and sodium hydroxide react to generate a sodium hypochlorite solution F.
- the sodium hypochlorite solution F taken out from the reaction tank 20 is taken out as a product, and is cooled by supplying it to the cooling device 8 using the cooling water L by a pump, and then circulating to the reaction tank 20. Therefore, it is possible to prevent the temperature rise of the electrolytic cell 10 and prevent the generated sodium hypochlorite from decomposing.
- Fig. 2 is an apparatus configuration diagram schematically showing another form of the sodium hypochlorite solution manufacturing apparatus used in the present invention.
- two or more electrolytic cells two electrolytic cells 10A and 10B in the example shown, are arranged, and one or more of them, one electrolytic cell 10A in the example shown.
- one electrolytic cell 10B is used to produce a sodium hypochlorite solution.
- a chlorine gas supply channel for supplying chlorine gas obtained from some of the multiple electrolytic cells to the chlorine gas using facility, chlorine gas can be supplied to the chlorine gas using facility. , and the production of the sodium hypochlorite solution can be carried out in parallel.
- the aqueous sodium hydroxide solution E produced in the chamber 3A and the cathode chamber 3B is mixed in the reaction tank 20 to produce a sodium hypochlorite solution.
- the second switching means 5 composed of an automatic valve is operated to switch the chlorine gas D generated in the electrolytic cell 10A into the system. can be taken out.
- a switching means (not shown) for switching whether or not the catholyte is introduced is installed and operated, and the sodium hydroxide aqueous solution E generated in the cathode chamber 3A is It is also possible to take it out of the system and store it.
- the chlorine gas D taken out of the system in this way can be used by directly injecting it into treated water at a water purification plant or the like.
- a sodium hypochlorite solution was produced in the apparatus having the configuration shown in FIG.
- the electrolysis area of the electrolytic cell was 8000 cm 2 and the electrolysis current was 2400A.
- As the ion-exchange membrane of the electrolytic cell F-9010 manufactured by AGC, which is a two-layer membrane composed of a sulfonic acid layer and a carboxylic acid layer, was used.
- Raw salt with a bromide ion concentration of 50 mg/kg was dissolved in purified water to generate primary salt water, and then the obtained primary salt water was subjected to chelate treatment to generate secondary salt water.
- the bromide ion concentration in the raw salt is 50 mg / kg
- the bromate concentration in the sodium hypochlorite solution in Example 1 described later is 15 mg / kg
- the sodium hypochlorite solution in Example 2 The bromate concentration was 18 mg/kg, which was lower than 50 mg/kg, which is the standard value for sodium hypochlorite for tap water use in the first grade of the Japan Water Works Association standard (JWWA K120:2008). Since the bromide ion is an anion, it cannot be removed by the chelate resin used in the brine purification.
- the pH of the salt water in which the raw salt was dissolved using purified water was 7.8 before purification.
- the concentration of calcium and magnesium in the brine before purification was 16 mg/L, and the concentration of calcium and magnesium in the brine after purification was 10 ⁇ g/L.
- the operation was started.
- the temperature of the electrolytic solution during operation was 75° C., and purified water was supplied to the cathode chamber to adjust the sodium hydroxide aqueous solution concentration in the cathode chamber.
- the amount of sodium hydroxide aqueous solution supplied to the reaction tank was adjusted so that the sodium hydroxide aqueous solution concentration in the sodium hypochlorite solution was 1%.
- the temperature of the reactor was cooled to 30°C.
- a first switching means is provided between the anode chamber and the reaction tank to switch whether or not the anode solution is introduced from the anode chamber to the reaction tank, and the introduction and discharge of the anode solution into and out of the reaction tank are controlled by an automatic valve. Simultaneously with switching, the amount of purified water supplied to the cathode chamber was adjusted to conduct tests for each example and comparative example.
- purified water was used for dissolving raw salt and adding to the cathode chamber. Although it is possible to use ion-exchanged water instead of purified water, it is preferable to use purified water from the viewpoint of cost.
- the silica concentration in purified water and secondary brine was 12 mg/L. Although the silica concentration in the secondary brine was intentionally adjusted to 40 mg/L and the electrolysis was continued for two months, the amount of chlorine produced and the voltage were stable.
- purified water is supplied to the cathode chamber to adjust the concentration of the aqueous sodium hydroxide solution, but purified water may be supplied to the reaction tank to adjust the concentration of the sodium hypochlorite solution.
- anolyte storage tank and the anode chamber, and the catholyte storage tank and the cathode chamber were communicated by piping, and no flow means such as a pump was provided.
- no flow means such as a pump was provided.
- the anolyte and catholyte reservoirs were positioned above the half height of the electrolytic cell, the anolyte and catholyte respectively circulated well between the reservoir and the electrolytic cell. , operating voltage, operating temperature and operating pressure were all stable.
- the bottom of each storage tank was placed below the half height of the electrolytic cell, good circulation was not obtained and the operating pressure was unstable.
- Example 1 A sodium hypochlorite solution was produced while introducing the anolyte into the reactor.
- the salt decomposition rate is 80.4% and the concentration of the sodium hydroxide aqueous solution of the catholyte is 28.0% by mass
- the available chlorine concentration, salt concentration and chloric acid concentration in the sodium hypochlorite solution obtained were 12.2%, 13.5% and 0.18% by weight, respectively. Since the reactor was operated with the anolyte introduced into the reactor, the amount of anolyte discharged was zero.
- Example 2 A sodium hypochlorite solution was produced while introducing the anolyte into the reactor.
- the salt decomposition rate is 89.4% and the concentration of the sodium hydroxide aqueous solution of the catholyte is 26.2% by mass
- the available chlorine concentration, salt concentration and chloric acid concentration in the sodium hypochlorite solution obtained were 12.8%, 13.0% and 0.17% by weight, respectively. Since the reactor was operated with the anolyte introduced into the reactor, the amount of anolyte discharged was zero.
- Example 3 A sodium hypochlorite solution was produced while draining the anolyte.
- the salt decomposition rate is 81.1% and the concentration of the sodium hydroxide aqueous solution of the catholyte is 16.3% by mass
- the available chlorine concentration, salt concentration and chloric acid concentration in the sodium hypochlorite solution obtained were 12.3% by weight, 10.4% by weight and 0.06% by weight, respectively.
- the anolyte discharge rate was 9.5 L/h.
- Example 4 A sodium hypochlorite solution was produced while draining the anolyte.
- the salt decomposition rate is 89.1% and the concentration of the sodium hydroxide aqueous solution of the catholyte is 16.0% by mass
- the available chlorine concentration, salt concentration and chloric acid concentration in the sodium hypochlorite solution obtained were 12.0% by weight, 10.1% by weight and 0.06% by weight, respectively.
- the anolyte discharge rate was 6.5 L/h.
- Example 5 A sodium hypochlorite solution was produced while part of the anolyte was introduced into the reactor and part of the anolyte was discharged.
- the ratio of the amount of anolyte introduced into the reaction tank and the amount of wastewater was set to 1:1.
- the salt decomposition rate is 86.7% and the concentration of the sodium hydroxide aqueous solution of the catholyte is 17.4% by mass
- the available chlorine concentration, salt concentration and chloric acid concentration in the sodium hypochlorite solution obtained were 12.1% by weight, 11.0% by weight and 0.08% by weight, respectively.
- the anolyte discharge rate was 3.7 L/hour.
- Comparative Example 1 compared to Examples 1 and 2, the salt decomposition rate was low, so the effective chlorine concentration in the sodium hypochlorite solution was low and the salt concentration was high.
- Comparative Example 2 resulted in a large amount of waste water.
- the salt decomposition rate must be 80% or more to produce a high-concentration sodium hypochlorite solution. was found to be necessary. On the other hand, if the salt decomposition rate exceeds 95%, the voltage rises significantly and the operation cannot be continued. Therefore, from the viewpoint of operational stability, it is necessary to set the upper limit of the salt decomposition rate to 95%. Confirmed.
- Cooling device 10 10A, 10B Electrolytic tank 20 Reaction tank 30 Salt dissolving tank 40 Cation exchange treatment unit 50 Salt water purifier A Secondary salt water B Purified water C Anolyte D Chlorine gas E Sodium hydroxide aqueous solution F Sodium hypochlorite solution G Raw salt H Primary salt water I Raw water K Hydrogen gas L Cooling water
Abstract
Description
2NaCl+2H2O = 2NaOH+Cl2+H2
一方、電解槽で生成した水酸化ナトリウムと塩素ガスとの反応により、反応槽で次亜塩素酸ナトリウム溶液が生成される。この反応槽における反応は、下記式により表される。
2NaOH+Cl2 = NaClO+NaCl+H2O
精製水に対し、塩化ナトリウムが主成分である原塩を溶解して一次塩水を生成する一次塩水生成工程と、
前記一次塩水に対しキレート処理を行って前記二次塩水を生成するキレート処理工程と、を含み、
塩の分解率を80~95%の範囲とすることを特徴とするものである。
精製水に対し、塩化ナトリウムが主成分である原塩を溶解して一次塩水を生成する一次塩水生成部と、
前記一次塩水に対しキレート処理を行って前記二次塩水を生成するキレート処理部と、を含み、
塩の分解率が80~95%の範囲で運転されることを特徴とするものである。
上述したように、本発明においては、二次塩水Aを生成するに際し、まず、精製水Bに対し、塩化ナトリウムが主成分である原塩Gを溶解して、室温における飽和塩水である一次塩水Hを生成する。精製水Bに対する原塩Gの溶解は、塩溶解槽30において行うことができる。
本発明においては、上記工程で得られた一次塩水Hに対しキレート処理を行って、二次塩水Aを生成する。一次塩水Hに対しキレート処理を行うことで、原塩Gから持ち込まれたカルシウムイオンおよびマグネシウムイオンを一次塩水中より除去して、清浄な二次塩水Aを生成することができる。一次塩水Hのキレート処理は、塩水精製器50において行うことができる。
反応槽へ陽極液を導入しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を80.4%、陰極液の水酸化ナトリウム水溶液の濃度を28.0質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ12.2質量%、13.5質量%および0.18質量%であった。反応槽へ陽極液を導入して運転しているため、陽極液の排水量はゼロであった。
反応槽へ陽極液を導入しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を89.4%、陰極液の水酸化ナトリウム水溶液の濃度を26.2質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ12.8質量%、13.0質量%および0.17質量%であった。反応槽へ陽極液を導入して運転しているため、陽極液の排水量はゼロであった。
陽極液を排水しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を81.1%、陰極液の水酸化ナトリウム水溶液の濃度を16.3質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ12.3質量%、10.4質量%および0.06質量%であった。陽極液の排水量は9.5L/時であった。
陽極液を排水しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を89.1%、陰極液の水酸化ナトリウム水溶液の濃度を16.0質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ12.0質量%、10.1質量%および0.06質量%であった。陽極液の排水量は6.5L/時であった。
陽極液の一部を反応槽に導入すると同時に、陽極液の一部を排水しながら、次亜塩素酸ナトリウム溶液の製造を行った。陽極液の反応槽への導入量と排水量との比率を1:1とした。塩の分解率を86.7%、陰極液の水酸化ナトリウム水溶液の濃度を17.4質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ12.1質量%、11.0質量%および0.08質量%であった。陽極液の排水量は3.7L/時であった。
反応槽へ陽極液を導入しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を45.1%、陰極液の水酸化ナトリウム水溶液の濃度を32.3質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ5.5質量%、18.4質量%および0.12質量%であった。反応槽へ陽極液を導入して運転しているため、陽極液の排水量はゼロであった。
陽極液を排水しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を47.0%、陰極液の水酸化ナトリウム水溶液の濃度を16.3質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ12.3質量%、10.1質量%および0.04質量%であった。陽極液の排水量は27.8L/時であった。
陽極液を排水しながら次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を96.2%としたとき、電圧上昇が起こり、次亜塩素酸ナトリウム溶液の濃度が安定するまでの運転を継続できなかった。運転停止時の陰極液の水酸化ナトリウム水溶液の濃度は18.1質量%であった。塩の分解率が96%に到達してから停止するまでの30分間の間の排水量は3.5L/時であった。
反応槽へ陽極液を導入しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を77.9%、陰極液の水酸化ナトリウム水溶液の濃度を29.3質量%としたとき、得られた次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ11.3質量%、14.9質量%および0.14質量%であった。反応槽へ陽極液を導入して運転しているため、陽極液の排水量はゼロであった。
陽極液を排水しながら、次亜塩素酸ナトリウム溶液の製造を行った。塩の分解率を75.6%、陰極液の水酸化ナトリウム水溶液の濃度を16.5質量%としたとき、次亜塩素酸ナトリウム溶液中の有効塩素濃度、食塩濃度および塩素酸濃度はそれぞれ12.1質量%、10.3質量%および0.06質量%であった。陽極液の排水量は11.7L/時であった。
2,2A,2B 陽極室
3,3A,3B 陰極室
4 第一の切替手段
5 第二の切替手段
6 陽極液貯留槽
6b 陽極液貯留槽の底部
7 陰極液貯留槽
7b 陰極液貯留槽の底部
8 冷却装置
10,10A,10B 電解槽
20 反応槽
30 塩溶解槽
40 陽イオン交換処理部
50 塩水精製器
A 二次塩水
B 精製水
C 陽極液
D 塩素ガス
E 水酸化ナトリウム水溶液
F 次亜塩素酸ナトリウム溶液
G 原塩
H 一次塩水
I 原料水
K 水素ガス
L 冷却水
Claims (26)
- イオン交換膜により陽極室と陰極室とに区画された電解槽の、該陽極室に塩化ナトリウム水溶液である二次塩水を供給し、電気分解後の該陽極室内の陽極液および生成塩素ガス、並びに、該陰極室内の生成水酸化ナトリウム水溶液を反応槽に導入して、該反応槽内での陽極液、塩素ガスおよび陰極液である生成水酸化ナトリウム水溶液の反応により次亜塩素酸ナトリウム溶液を製造するにあたり、
精製水に対し、塩化ナトリウムが主成分である原塩を溶解して一次塩水を生成する一次塩水生成工程と、
前記一次塩水に対しキレート処理を行って前記二次塩水を生成するキレート処理工程と、を含み、
塩の分解率を80~95%の範囲とすることを特徴とする次亜塩素酸ナトリウム溶液の製造方法。 - 前記イオン交換膜として、スルホン酸層とカルボン酸層とで構成された二層膜を用いる請求項1記載の次亜塩素酸ナトリウム溶液の製造方法。
- 前記陽極室と前記反応槽との間に、前記陽極液を該陽極室から該反応槽へ導入するか否かを切り替える第一の切替手段を設け、該陽極液の一部あるいは全量を該反応槽へ導入せずに次亜塩素酸ナトリウム溶液の製造を行う請求項1または2記載の次亜塩素酸ナトリウム溶液の製造方法。
- 前記陽極室と前記反応槽との間に、前記塩素ガスを該陽極室から該反応槽へ導入するか否かを切り替える第二の切替手段を設け、該塩素ガスの一部あるいは全量を塩素ガス使用施設に供給しつつ次亜塩素酸ナトリウム溶液の製造を行う請求項1~3のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造方法。
- 2個以上の前記電解槽を用いて、1個以上の該電解槽から得られる前記塩素ガスを塩素ガス使用施設に供給するとともに、1個以上の該電解槽から得られる前記塩素ガスを用いて次亜塩素酸ナトリウム溶液を製造する請求項1~4のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造方法。
- 前記反応槽に精製水を導入して、次亜塩素酸ナトリウム溶液の濃度を調整する請求項1~5のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造方法。
- 前記反応槽で生成する次亜塩素酸ナトリウム溶液の有効塩素濃度を8%以上とする請求項1~6のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造方法。
- 原料水を、陽イオン交換樹脂で処理して前記精製水を生成する陽イオン交換工程を含む請求項1~7のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造方法。
- 前記陽イオン交換工程において軟水器を用いる請求項8記載の次亜塩素酸ナトリウム溶液の製造方法。
- 製造施設の外部と通信可能な自動制御装置からの指示に基づき、スイッチ操作または外部信号により前記第一の切替手段を作動させる請求項3記載の次亜塩素酸ナトリウム溶液の製造方法。
- 製造施設の外部と通信可能な自動制御装置からの指示に基づき、スイッチ操作または外部信号により前記第二の切替手段を作動させる請求項4記載の次亜塩素酸ナトリウム溶液の製造方法。
- 次亜塩素酸ナトリウム溶液の使用施設の近傍で、オンサイトで次亜塩素酸ナトリウム溶液を製造する請求項1~11のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造方法。
- 前記電解槽の近傍に、前記陽極液を貯留する陽極液貯留槽および前記陰極液を貯留する陰極液貯留槽を設け、該陽極液貯留槽および該陰極液貯留槽の底部を、該電解槽の1/2高さの位置よりも上方に配置して、該陽極液および該陰極液をそれぞれ、該陽極液貯留槽と前記陽極室との間、および、該陰極液貯留槽と前記陰極室との間で重力差によって循環させる請求項1~12のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造方法。
- イオン交換膜により陽極室と陰極室とに区画され、塩化ナトリウム水溶液である二次塩水が供給される電解槽と、電気分解後における該陽極室および該陰極室内の生成物が導入される反応槽と、を備え、該反応槽内での反応により次亜塩素酸ナトリウム溶液を製造する装置であって、
精製水に対し、塩化ナトリウムが主成分である原塩を溶解して一次塩水を生成する一次塩水生成部と、
前記一次塩水に対しキレート処理を行って前記二次塩水を生成するキレート処理部と、を含み、
塩の分解率が80~95%の範囲で運転されることを特徴とする次亜塩素酸ナトリウム溶液の製造装置。 - 前記イオン交換膜が、スルホン酸層とカルボン酸層とで構成された二層膜である請求項14記載の次亜塩素酸ナトリウム溶液の製造装置。
- 前記陽極室と前記反応槽との間に、該陽極室内の陽極液を該陽極室から該反応槽へ導入するか否かを切り替える第一の切替手段を備える請求項14または15記載の次亜塩素酸ナトリウム溶液の製造装置。
- 前記陽極室と前記反応槽との間に、該陽極室内で生成する塩素ガスを該陽極室から該反応槽へ導入するか否かを切り替える第二の切替手段を備える請求項14~16のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造装置。
- 2個以上の前記電解槽を備えるとともに、1個以上の該電解槽から得られる塩素ガスを塩素ガス使用施設に供給するための塩素ガス供給路を有する請求項14~17のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造装置。
- 前記反応槽に精製水を導入するための精製水導入路を有する請求項14~18のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造装置。
- 有効塩素濃度が8%以上である次亜塩素酸ナトリウム溶液の製造に用いられる請求項14~19のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造装置。
- 原料水を、陽イオン交換樹脂で処理して前記精製水を生成する陽イオン交換処理部を含む請求項14~20のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造装置。
- 前記陽イオン交換処理部が軟水器からなる請求項21記載の次亜塩素酸ナトリウム溶液の製造装置。
- 製造施設の外部と通信可能な自動制御装置を介して、スイッチ操作または外部信号により前記第一の切替手段が作動可能に形成されている請求項16記載の次亜塩素酸ナトリウム溶液の製造装置。
- 製造施設の外部と通信可能な自動制御装置を介して、スイッチ操作または外部信号により前記第二の切替手段が作動可能に形成されている請求項17記載の次亜塩素酸ナトリウム溶液の製造装置。
- 次亜塩素酸ナトリウム溶液の使用施設の近傍に設置されて、オンサイトでの次亜塩素酸ナトリウム溶液の製造に用いられる請求項14~24のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造装置。
- 前記電解槽の近傍に、陽極液を貯留する陽極液貯留槽および陰極液を貯留する陰極液貯留槽を有し、該陽極液貯留槽および該陰極液貯留槽の底部が、該電解槽の1/2高さの位置よりも上方に配置されている請求項14~25のうちいずれか一項記載の次亜塩素酸ナトリウム溶液の製造装置。
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JP2022184083A (ja) | 2022-12-13 |
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CN117280078A (zh) | 2023-12-22 |
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