CN115321485A - Method for extracting chemical elements from concentrated seawater - Google Patents
Method for extracting chemical elements from concentrated seawater Download PDFInfo
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- CN115321485A CN115321485A CN202211263800.3A CN202211263800A CN115321485A CN 115321485 A CN115321485 A CN 115321485A CN 202211263800 A CN202211263800 A CN 202211263800A CN 115321485 A CN115321485 A CN 115321485A
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- Prior art keywords
- magnesium
- carbon dioxide
- concentrated seawater
- calcium
- extraction system
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- 239000013535 sea water Substances 0.000 title claims abstract description 113
- 238000000034 method Methods 0.000 title claims abstract description 51
- 229910052729 chemical element Inorganic materials 0.000 title claims abstract description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 122
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 61
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 61
- 239000013505 freshwater Substances 0.000 claims abstract description 13
- 150000003839 salts Chemical class 0.000 claims description 82
- 238000000605 extraction Methods 0.000 claims description 72
- 239000007788 liquid Substances 0.000 claims description 62
- 239000011777 magnesium Substances 0.000 claims description 60
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 56
- 229910052749 magnesium Inorganic materials 0.000 claims description 56
- 239000011575 calcium Substances 0.000 claims description 44
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 claims description 40
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 claims description 40
- 229910052794 bromium Inorganic materials 0.000 claims description 40
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 38
- 229910052791 calcium Inorganic materials 0.000 claims description 37
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 238000003763 carbonization Methods 0.000 claims description 29
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 25
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 24
- 239000012065 filter cake Substances 0.000 claims description 21
- 238000002360 preparation method Methods 0.000 claims description 21
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 20
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 19
- 239000000047 product Substances 0.000 claims description 18
- 239000000243 solution Substances 0.000 claims description 18
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 17
- 238000000909 electrodialysis Methods 0.000 claims description 16
- 229910052700 potassium Inorganic materials 0.000 claims description 16
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 15
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 15
- 239000011591 potassium Substances 0.000 claims description 15
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims description 14
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 14
- 229910052744 lithium Inorganic materials 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 235000017550 sodium carbonate Nutrition 0.000 claims description 12
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 12
- 238000001223 reverse osmosis Methods 0.000 claims description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 10
- 239000003546 flue gas Substances 0.000 claims description 10
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims description 10
- 235000019341 magnesium sulphate Nutrition 0.000 claims description 10
- 230000002378 acidificating effect Effects 0.000 claims description 9
- 238000003860 storage Methods 0.000 claims description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 8
- 239000012267 brine Substances 0.000 claims description 8
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 8
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 8
- 229910001424 calcium ion Inorganic materials 0.000 claims description 7
- 239000008267 milk Substances 0.000 claims description 7
- 210000004080 milk Anatomy 0.000 claims description 7
- 235000013336 milk Nutrition 0.000 claims description 7
- 239000011780 sodium chloride Substances 0.000 claims description 7
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 7
- 235000011152 sodium sulphate Nutrition 0.000 claims description 7
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 6
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 6
- 230000000295 complement effect Effects 0.000 claims description 6
- 239000004571 lime Substances 0.000 claims description 6
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims description 6
- 239000001095 magnesium carbonate Substances 0.000 claims description 6
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 5
- 239000000460 chlorine Substances 0.000 claims description 5
- 229910052801 chlorine Inorganic materials 0.000 claims description 5
- 239000000395 magnesium oxide Substances 0.000 claims description 5
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 5
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 claims description 5
- 229940061634 magnesium sulfate heptahydrate Drugs 0.000 claims description 5
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 5
- NPYPAHLBTDXSSS-UHFFFAOYSA-N Potassium ion Chemical compound [K+] NPYPAHLBTDXSSS-UHFFFAOYSA-N 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 4
- 239000000347 magnesium hydroxide Substances 0.000 claims description 4
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 4
- 239000012528 membrane Substances 0.000 claims description 4
- 229910001414 potassium ion Inorganic materials 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 238000000967 suction filtration Methods 0.000 claims description 3
- 238000010000 carbonizing Methods 0.000 claims description 2
- 238000011085 pressure filtration Methods 0.000 claims description 2
- 239000010802 sludge Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052799 carbon Inorganic materials 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 238000010612 desalination reaction Methods 0.000 description 14
- 239000002253 acid Substances 0.000 description 9
- 230000018109 developmental process Effects 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 239000003651 drinking water Substances 0.000 description 4
- 235000020188 drinking water Nutrition 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 230000001376 precipitating effect Effects 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- CPELXLSAUQHCOX-UHFFFAOYSA-N Hydrogen bromide Chemical compound Br CPELXLSAUQHCOX-UHFFFAOYSA-N 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- -1 hydroxide ions Chemical class 0.000 description 2
- JGJLWPGRMCADHB-UHFFFAOYSA-N hypobromite Inorganic materials Br[O-] JGJLWPGRMCADHB-UHFFFAOYSA-N 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- BSKZDJXVMPWPRA-UHFFFAOYSA-N O.[Br] Chemical compound O.[Br] BSKZDJXVMPWPRA-UHFFFAOYSA-N 0.000 description 1
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 150000001669 calcium Chemical class 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000001944 continuous distillation Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000411 inducer Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 150000002680 magnesium Chemical class 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910052567 struvite Inorganic materials 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/09—Bromine; Hydrogen bromide
- C01B7/096—Bromine
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/18—Carbonates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/02—Magnesia
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/24—Magnesium carbonates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/40—Magnesium sulfates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/10—Obtaining alkali metals
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/10—Obtaining alkali metals
- C22B26/12—Obtaining lithium
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
-
- 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
- C25B1/14—Alkali metal compounds
- C25B1/16—Hydroxides
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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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
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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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
-
- 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
- C02F2103/08—Seawater, e.g. for desalination
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
Abstract
The invention provides a method for extracting chemical elements from concentrated seawater, belonging to the technical field of comprehensive utilization of concentrated seawater, wherein the concentrated seawater is a solution remained after seawater is desalted and fresh water is separated out. The method realizes zero discharge of the concentrated seawater, prepares a product with high added value, makes full use of the whole process by complementation before and after, realizes carbon emission reduction by utilizing waste thermoelectric carbon dioxide resources, and has good economic benefit and social benefit.
Description
Technical Field
The invention relates to a treatment method of concentrated seawater, in particular to a method for extracting various chemical elements from the concentrated seawater, belonging to the technical field of comprehensive utilization of the concentrated seawater.
Background
Since 2010, china sets development targets of three stages from 'twelve five' to 'fourteen five' successively aiming at the seawater desalination industry, and a plurality of support policies are developed to vigorously promote the industry development. Since fourteen years, the national policy is more heavily applied, and the national development reform committee and the natural resources department jointly issue an action plan for seawater desalination development and utilization (2021-2025), so as to promote the large-scale utilization of seawater desalination.
At present, 123 seawater desalination projects are built in China, and the seawater desalination capacity exceeds 160 ten thousand t/d. According to the action plan for seawater desalination development (2021-2025), by 2025, the total scale of seawater desalination in China reaches more than 290 million t/d, and the scale of newly-increased seawater desalination reaches more than 125 million t/d.
With the annual increase of the seawater desalination amount, the comprehensive utilization of concentrated seawater becomes more and more important. At present, the concentrated seawater is treated mainly by discharging seawater, and the method lacks effective utilization of the concentrated seawater. Concentrated seawater contains rich K, mg, br, li, na and other resources, and the development of the recovery technology and the industrial method of the ocean resources is the key research point of the seawater desalination technology.
At present, the comprehensive utilization technology of concentrated seawater has a certain research foundation at home and abroad, but the industrial application is less in view of higher cost. For example, patent CN10123476a proposes to extract potassium, magnesium, bromine, salt, gypsum and salt from desalinated concentrated seawater, and this process does not solve the problem of extracting bromine acidic wastewater, and has low product purity, low added value, large overall land occupation and poor economy. CN107311381A proposes multi-stage reverse osmosis concentrated seawater, and the concentrated water is evaporated in multiple effects, and the process has high energy consumption. CN108483710B proposes that by adding an inducer and a diluent, struvite is generated with calcium and magnesium ions in seawater, and then reverse osmosis is carried out, concentrated water enters an alkali factory, and the process is also high in energy consumption, low in added value of concentrated water products and low in economy. CN109574055B proposes to react salt slurry with flue gas to produce magnesium sulfate and calcium carbonate, which does not consider the problems of calcium and magnesium purification, high-end magnesium product preparation and flue gas capture, resulting in higher process cost. CN106186498A proposes that concentrated seawater is concentrated by a frequent reverse electrode electrodialysis device, electrodialysis concentrated water is evaporated and concentrated to obtain finished salt, the finished salt is desalted, concentrated, cooled and crystallized to prepare potassium chloride finished salt, and finally bromine is extracted from old brine. Therefore, the low-cost comprehensive utilization technology of seawater is one of the bottlenecks that restrict the sustainable development of the seawater.
Disclosure of Invention
Aiming at the problems, the invention provides a method for extracting chemical elements from concentrated seawater, which reduces the comprehensive cost of concentrated seawater treatment and produces multiple elements such as bromine, magnesium series products, calcium series products and the like with high additional values.
In order to achieve the purpose, the scheme of the invention is as follows: a method for extracting chemical elements from concentrated seawater is a solution left after seawater is desalted and fresh water is separated, and comprises the following steps of extracting each chemical element from the concentrated seawater through a bromine extraction system, a magnesium extraction system, a calcium extraction system, a concentrated liquid salt preparation system, a liquid salt potassium extraction system, a liquid salt lithium extraction system, a liquid salt concentrated salt preparation system and a carbon dioxide storage system, and comprises the following steps:
a bromine extraction system: treating the concentrated seawater by an air blowing method, and extracting to obtain bromine and the acidic concentrated seawater after bromine extraction;
b, magnesium extracting system: the acid concentrated seawater enters a magnesium extraction system after bromine extraction, predetermined amount of lime milk and anhydrous sodium sulphate are added, stirring reaction is carried out, the acid wastewater is neutralized, and meanwhile Mg in the concentrated seawater is added 2+ Part of Ca 2+ Precipitating, and performing filter pressing after the reaction is finished to obtain a magnesium mud filter cake and concentrated seawater after magnesium removal;
c, calcium extraction system: the concentrated seawater after magnesium removal enters a calcium extraction system, carbon dioxide is added into the system for carbonization by using a supergravity reactor, and a superfine calcium carbonate product and the concentrated seawater after calcium removal are prepared by filtering;
d, concentrating to prepare liquid salt system: the concentrated seawater after calcium removal enters an electrodialysis system to obtain liquid salt and light salt water, the light salt water enters a reverse osmosis system to be further desalinated to obtain fresh water, the fresh water is sold after meeting the water quality standard of GB5049-2022 drinking water, and the concentrated water obtained by the reverse osmosis system returns to a water collecting tank at the concentrated water side of electrodialysis;
e, sequentially extracting potassium from the liquid salt by combining a potassium ion membrane with an electrodialysis method in a liquid salt potassium extraction system, extracting lithium from the liquid salt lithium extraction system by an adsorption method, and preparing salt by multi-effect evaporation in a liquid salt concentration salt preparation system;
and C, providing carbon dioxide for the carbonization process of the calcium extraction system in the step C by the carbon dioxide storage system.
And further, in the bromine extraction system in the step A, concentrated seawater is acidified by sulfuric acid, oxidized by chlorine, blown out and absorbed by bromine, oxidized, distilled, cooled and separated to prepare bromine.
Furthermore, after the lime milk and the anhydrous sodium sulphate are added into the magnesium extracting system in the step B, the concentration of calcium ions in the concentrated seawater is less than 1.4g/L, the concentration of sulfate ions is 4-5g/L, and the concentration of hydroxide ions is 0.085-0.255g/L.
Further, adding water into the magnesium mud filter cake obtained in the magnesium extracting system in the step B, adding a predetermined amount of calcium sulfate dihydrate, adding carbon dioxide for carbonization, and performing suction filtration to obtain a calcium carbonate filter cake and a magnesium sulfate solution; the adding amount of the calcium sulfate dihydrate is as follows: the amount of magnesium hydroxide in the magnesium mud filter cake: the adding amount of the calcium sulfate dihydrate added with the amount of the calcium sulfate contained in the magnesium mud filter cake is 1:0.9, the solid-to-liquid ratio of the slurry obtained after adding the calcium sulfate dihydrate is 1:3-1:6; the carbon dioxide for carbonization is provided by a carbon dioxide storage system.
And further, drying a calcium carbonate filter cake obtained in the magnesium extracting system in the step B to prepare a common calcium carbonate product, wherein the magnesium sulfate solution is used for preparing magnesium sulfate heptahydrate, basic magnesium carbonate or magnesium oxide.
Further, carbon dioxide used for carbonizing the magnesium extracting system in the step B is obtained by concentrating carbon dioxide obtained by a thermoelectric flue device carbon dioxide complementary collection system, the concentration of the carbon dioxide in the thermoelectric flue gas is 13%, and the concentration of the concentrated carbon dioxide is 40% -50%; the carbon dioxide used for carbonization is pressurized by 2-3 kg when in use, the temperature is 50 ℃ during carbonization reaction, and the carbonization time is 60-120min.
Further, the carbon dioxide used for the carbonization of the calcium extraction system in the step C is obtained by concentrating the carbon dioxide obtained by the carbon dioxide complementary collection system of the thermoelectric flue device, the concentration of the carbon dioxide in the thermoelectric flue gas is 13%, and the concentration of the concentrated carbon dioxide is 40% -50%.
Furthermore, the carbon dioxide used for the carbonization of the calcium extraction system in the step C is pressurized by 2-3 kg when in use, sodium hydroxide needs to be added into the concentrated seawater after magnesium removal during carbonization, the calcium ion concentration in the concentrated seawater after calcium removal is less than 0.02g/L, and the carbonate ion concentration is 0.15-0.45 g/L.
And D, further, feeding the liquid salt obtained in the liquid salt preparation system obtained in the step D into a soda ash or chlor-alkali salt dissolving system to be used as a raw material for preparing soda ash or caustic soda.
Furthermore, the content of sodium chloride in the liquid salt obtained by the liquid salt system prepared by concentration in the step D is 120-180g/L.
Compared with the prior art, the invention has the beneficial effects that:
the invention really realizes zero discharge of concentrated seawater and full utilization of seawater resources, and prepares high-added-value bromine products, magnesium products (magnesium sulfate heptahydrate, basic magnesium carbonate and active magnesium oxide), calcium products (superfine calcium carbonate and common calcium carbonate), potassium and lithium products and sodium chloride finished salt, and fresh water which meets the standard of drinking water for life. The whole process is complementary, the best use is made of things, the economic performance is good, the carbon emission reduction is realized by using the waste thermoelectric flue gas carbon dioxide resource, the social benefit is obvious, and the synergistic green development of the thermoelectric industry and the seawater desalination, soda ash and caustic soda industry is promoted.
Drawings
FIG. 1 is a schematic view of the process flow of the concentrated seawater chemical element extraction system of the present invention.
Detailed Description
The technical solution in the embodiments of the present invention is clearly and completely described below with reference to the drawings in the embodiments of the present invention. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, however, the present invention may be practiced otherwise than as specifically described herein, and it will be appreciated by those skilled in the art that the present invention may be practiced without departing from the spirit and scope of the present invention and that the present invention is not limited by the specific embodiments disclosed below.
A method for extracting chemical elements from concentrated seawater is a solution left after seawater is desalted and fresh water is separated, and comprises the following steps of extracting each chemical element from the concentrated seawater through a bromine extraction system, a magnesium extraction system, a calcium extraction system, a concentrated liquid salt preparation system, a liquid salt potassium extraction system, a liquid salt lithium extraction system, a liquid salt concentrated salt preparation system and a carbon dioxide storage system, and comprises the following steps:
a bromine extraction system: treating the concentrated seawater by an air blowing method, extracting to obtain bromine and acidic concentrated seawater after bromine extraction; the specific bromine extraction step comprises the following steps: the concentrated seawater is acidified by sulfuric acid, oxidized by chlorine, blown out and absorbed by bromine, oxidized, distilled, cooled and separated to prepare bromine.
B, magnesium extracting system: the acid concentrated seawater enters a magnesium extraction system after bromine extraction, predetermined amount of lime milk and anhydrous sodium sulphate are added, stirring reaction is carried out, the acid wastewater is neutralized, and meanwhile Mg in the concentrated seawater is added 2+ Part of Ca 2+ Precipitating, and performing filter pressing after the reaction is finished to obtain a magnesium mud filter cake and concentrated seawater after magnesium removal; adding water into the magnesium mud filter cake, mixing, adding a predetermined amount of calcium sulfate dihydrate, adding carbon dioxide for carbonization, and performing suction filtration to obtain a calcium carbonate filter cake and a magnesium sulfate solution; drying the calcium carbonate filter cake to prepare a common calcium carbonate product, and using the magnesium sulfate solution to prepare magnesium sulfate heptahydrate,Basic magnesium carbonate or magnesium oxide;
the addition amount of the gray milk and the anhydrous sodium sulphate is that the concentration of calcium ions in the concentrated seawater is less than 1.4g/L, the concentration of sulfate ions is 4-5g/L, and the concentration of hydroxide ions is 0.085-0.255g/L; amount of magnesium hydroxide in magnesium sludge: the addition amount of the calcium sulfate dihydrate added to the amount of the calcium sulfate contained in the magnesium cement is =1: 0.9 (molar ratio); the solid-to-liquid ratio in the slurry is 1:3-1:6.
The carbon dioxide used for carbonization can be obtained by concentrating carbon dioxide obtained by a carbon dioxide complementary collection system of a thermoelectric flue device, the concentration of the carbon dioxide in the thermoelectric flue gas is 13 percent, the concentration of the concentrated carbon dioxide is 40 to 50 percent, and the carbon dioxide is pressurized by 2 to 3 kilograms when in use; and C, during the carbonization reaction of the magnesium extracting system in the step B, the temperature is 50 ℃, and the carbonization time is 60-120min.
C, calcium extraction system: the concentrated seawater after magnesium removal enters a calcium extraction system, carbon dioxide is added into the system for carbonization by using a supergravity reactor, and a superfine calcium carbonate product and the concentrated seawater after calcium removal are prepared by filtering;
the carbon dioxide used for carbonization can be obtained by concentrating carbon dioxide obtained by a carbon dioxide complementary collection system of a thermoelectric flue device, the concentration of the carbon dioxide in the thermoelectric flue gas is 13 percent, the concentration of the concentrated carbon dioxide is 40 to 50 percent, and 2 to 3 kilograms of carbon dioxide is pressurized when in use; and C, adding sodium hydroxide into the concentrated seawater after magnesium removal during the carbonization of the calcium extraction system in the step C, wherein the concentration of calcium ions in the concentrated seawater after calcium removal is less than 0.02g/L, and the concentration of carbonate ions is 0.15-0.45 g/L.
D, concentrating to prepare liquid salt system: the concentrated seawater after calcium removal enters an electrodialysis system to obtain liquid salt and light salt water, the light salt water enters a reverse osmosis system for further desalination to obtain fresh water, the fresh water is sold after meeting the water quality standard of GB5049-2022 drinking water, and the concentrated water obtained by the reverse osmosis system returns to a water collecting tank at the concentrated water side of electrodialysis;
the content of sodium chloride in the liquid salt obtained by the liquid salt concentration system is 120-180g/L.
The liquid salt obtained by the liquid salt concentration system can be treated in the following way: feeding into a soda ash or chlor-alkali salt system to be used as raw materials for preparing soda ash or caustic soda.
E, sequentially extracting potassium from the liquid salt by adopting a potassium ion membrane and an electrodialysis method in a liquid salt potassium extraction system, extracting lithium from the liquid salt by adopting an adsorption method in a liquid salt lithium extraction system, and preparing salt by adopting multi-effect evaporation in a liquid salt concentration salt preparation system;
and the carbon dioxide storage system provides carbon dioxide for the carbonization process of the magnesium extraction system in the step B and the carbonization process of the calcium extraction system in the step C.
Example 1
A method for extracting chemical elements from concentrated seawater, which is the solution left after seawater is desalinated and separated to obtain fresh water, comprises the steps of extracting each chemical element from the concentrated seawater through a bromine extraction system, a magnesium extraction system, a calcium extraction system, a concentrated liquid salt preparation system, a liquid salt potassium extraction system, a liquid salt lithium extraction system, a liquid salt concentrated salt preparation system and a carbon dioxide storage system, as shown in figure 1,
the bromine extraction system for extracting bromine comprises the following steps:
concentrating seawater after seawater desalination to extract bromine: the concentrated seawater comprises the following components: br - 120mg/L、Mg 2+ 1.61g/ L、SO4 2- 3.3g/ L、Ca 2+ 0.58g/ L、K + 0.5g/ L、Li + 0.4mg/ L、NaCl 37g/ L。2500m 3 Adding 129kg/h sulfuric acid into the concentrated seawater in a pipeline for acidification, and adjusting the pH value<3.5. The liquid chlorine is heated and gasified by the gasifier and then enters the acidic concentrated seawater pipe section, and the liquid chlorine and the acidic concentrated seawater pipe section jointly enter the oxidation tower to carry out oxidation reaction in the tower, so that bromide ions in the concentrated seawater are converted into free elemental bromine. The oxidized concentrated seawater enters a blow-off tower, sprays from the upper part of the blow-off tower, air is blown from the lower part of an air blower, free bromine is carried out by the air, and the acidic concentrated seawater after bromine extraction is discharged from the bottom of the tower and enters a magnesium extraction system. Bromine-containing air and SO 2 And the atomized water enters the absorption tower together to form HBr liquid drops in the absorption tower, so that the purpose of absorption and concentration is achieved. The absorbed solution is primary acid solution which enters a distillation tower from the upper part, chlorine and steam are introduced from the bottom of the tower, the primary acid solution flows along the surface of the filler from top to bottom and contacts with the chlorine and the steam from bottom to top, and the oxidized free bromine is heated and evaporated by the steam. Cooling the mixed gas obtained by distillation by a condenser, separating a bromine product by a liquid phase entering a bromine-water separator after two-stage separation to obtain 257kg/h, and returning bromine water to the distillation tower for continuous distillation. And discharging the evaporated liquid from the bottom of the distillation tower, cooling, and feeding into a dilute acid tank for acidifying concentrated seawater.
Absorbent SO 2 Is produced by burning sulfur, adding sulfur into a sulfur furnace, and providing air through a blower to burn the sulfur to produce SO 2 。
And (II) after bromine extraction, the acidic concentrated seawater enters a magnesium extraction system for magnesium extraction, and the method comprises the following steps:
to the acid concentrated seawater (2500 m) after bromine extraction 3 H) addition of 42m 3 Neutralizing the acid concentrated seawater by using/h lime milk and 21t/h anhydrous sodium sulphate, and simultaneously adding Mg in the concentrated seawater 2+ Part of Ca 2+ Precipitating, performing pressure filtration to obtain a magnesium mud filter cake (containing about 48 percent of water) and concentrated seawater after magnesium removal, adding water into the magnesium mud filter cake for size mixing (the weight ratio of the magnesium mud filter cake to the water is about 1:3-1:6), adding a certain amount of calcium sulfate dihydrate, and adding magnesium hydroxide into the magnesium mud filter cake: calcium sulfate =1, 0.7-1, 0.9 (mass), 40% -50% of carbon dioxide gas formed after the capture of thermoelectric flue gas carbon dioxide is pressurized and carbonized for 60-120min, the reaction temperature is 50 ℃, the solution is filtered, and filter cakes can be used for preparing common calcium carbonate products, and the filtrate is magnesium sulfate solution, about 0.46mol/L. Part of the magnesium sulfate solution is cooled to 20 ℃ to prepare magnesium sulfate heptahydrate. A part of the magnesium sulfate: the molar ratio of sodium carbonate is 1:1.1, adding sodium carbonate, stirring and reacting for 0.5h at 50 ℃, heating to 85 ℃, pyrolyzing for 2h, and aging for 0.5h to prepare basic magnesium carbonate; calcining the basic magnesium carbonate to prepare the active magnesium oxide. The conversion rate of magnesium ions reaches more than 80 percent.
And (III) the concentrated seawater after magnesium removal enters a calcium extraction system, and the calcium extraction comprises the following steps:
concentrated seawater (Ca) after magnesium extraction 2+ 1.4g/L、SO4 2- 4.32g/L、OH - 0.17 g/L) and 40-50 percent of carbon dioxide gas are introduced into a supergravity reactor, the solution is aged for a period of time after reaction, filtered (the filtrate is concentrated seawater after calcium removal), dried and prepared into a superfine calcium carbonate product. Concentrated seawater Ca after calcium removal 2+ 0.018g/L、CO3 2- 0.3g/L。
And (IV) after calcium removal, the concentrated seawater enters a concentrated liquid salt preparation system for treatment, and the method comprises the following steps:
liquid, method for producing the same and use thereofThe salt preparation adopts electrodialysis and reverse osmosis mode, and the seawater after calcium removal is about 2500m 3 The fresh water enters an electrodialysis system, the light salt water (containing 23g/L of sodium chloride) enters a three-stage reverse osmosis system for further desalination, and the fresh water (containing chloride ion content)<250 mg/L) meets the water quality standard of GB5049-2022 drinking water for sale, and reverse osmosis concentrated water (the content of sodium chloride is about 100 g/L) enters an electrodialysis concentrated water side water collecting tank. The concentration of the liquid salt produced by electrodialysis concentrated water side is about 122g/L and 733m 3 H, the main component content is as follows: k + 1.72g/L、Li + 1.17mg/L, naCl g/L. The liquid salt is treated by the following method, and the liquid salt is further prepared into salt by potassium ion sieve membrane plus electrodialysis method for extracting potassium, adsorption method for extracting lithium and multi-effect evaporation (wherein the methods for extracting potassium, extracting lithium and preparing salt are all the prior art, and other methods for extracting potassium, extracting lithium and preparing salt from the liquid salt can also be adopted in the embodiment).
Example 2
Example 2 is substantially the same as example 1 except that the concentrated seawater after calcium removal enters a concentrated liquid salt preparation system and the obtained liquid salt is treated by the following method, the liquid salt is directly sent into a soda ash and caustic soda salt preparation system to prepare saturated crude brine, and the saturated crude brine is refined to remove calcium and magnesium to prepare refined brine. Soda ash company uses refined brine to carbonize and prepare sodium bicarbonate, and then calcines to prepare soda ash. Chlor-alkali company electrolytically produces caustic soda from refined brine.
It should be apparent that the described embodiments are only some of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Claims (10)
1. A method for extracting chemical elements from concentrated seawater is characterized in that the concentrated seawater is a solution left after seawater is desalted and fresh water is separated, the method comprises the steps of extracting the chemical elements from the concentrated seawater through a bromine extraction system, a magnesium extraction system, a calcium extraction system, a concentrated liquid salt preparation system, a liquid salt potassium extraction system, a liquid salt lithium extraction system, a liquid salt concentrated salt preparation system and a carbon dioxide storage system, and the method comprises the following steps:
a bromine extraction system: treating the concentrated seawater by an air blowing method, and extracting to obtain bromine and the acidic concentrated seawater after bromine extraction;
b, magnesium extraction system: after bromine extraction, the acidic concentrated seawater enters a magnesium extraction system, a predetermined amount of lime milk and anhydrous sodium sulphate are added, stirring and reaction are carried out, and after the reaction is finished, a magnesium mud filter cake and concentrated seawater after magnesium removal are obtained through pressure filtration;
c, calcium extraction system: the concentrated seawater after magnesium removal enters a calcium extraction system, carbon dioxide is added into the system for carbonization by using a supergravity reactor, and a superfine calcium carbonate product and the concentrated seawater after calcium removal are prepared by filtering;
d, concentrating to prepare liquid salt system: the concentrated seawater after calcium removal enters an electrodialysis system to obtain liquid salt and light brine, the light brine enters a reverse osmosis system to be further desalinated to obtain fresh water, and the concentrated water obtained by the reverse osmosis system returns to a water collecting tank at the concentrated water side of the electrodialysis;
e, sequentially extracting potassium from the liquid salt by adopting a potassium ion membrane and an electrodialysis method in a liquid salt potassium extraction system, extracting lithium from the liquid salt by adopting an adsorption method in a liquid salt lithium extraction system, and preparing salt by adopting multi-effect evaporation in a liquid salt concentration salt preparation system;
and C, providing carbon dioxide for the carbonization process of the calcium extraction system in the step C by the carbon dioxide storage system.
2. The method of claim 1, wherein the bromine extraction system of step a is configured to acidify the concentrated seawater with sulfuric acid, oxidize chlorine, blow out and absorb bromine, oxidize and distill, cool and separate bromine.
3. The method for extracting chemical elements from concentrated seawater as claimed in claim 1, wherein the calcium ion concentration of concentrated seawater is less than 1.4g/L, the sulfate ion concentration is 4-5g/L, and the hydroxide ion concentration is 0.085-0.255g/L after the lime milk and anhydrous sodium sulphate are added into the magnesium extraction system in step B.
4. The method for extracting chemical elements from concentrated seawater according to claim 1, wherein the magnesium sludge filter cake obtained in the magnesium extraction system in the step B is added with water for size mixing, then a predetermined amount of calcium sulfate dihydrate is added, then carbon dioxide is added for carbonization, and then calcium carbonate filter cake and magnesium sulfate solution are obtained through suction filtration; the adding amount of the calcium sulfate dihydrate is as follows: the amount of magnesium hydroxide in the magnesium mud filter cake: the adding amount of the calcium sulfate dihydrate added with the amount of the calcium sulfate contained in the magnesium mud filter cake is 1:0.9, the solid-to-liquid ratio of the slurry obtained after adding the calcium sulfate dihydrate is 1:3-1:6; the carbon dioxide for carbonization is provided by a carbon dioxide storage system.
5. The method for extracting chemical elements from concentrated seawater as claimed in claim 4, wherein the calcium carbonate filter cake obtained in the magnesium extraction system in step B is dried to prepare a common calcium carbonate product, and the magnesium sulfate solution is used for preparing magnesium sulfate heptahydrate, basic magnesium carbonate or magnesium oxide.
6. The method for extracting chemical elements from concentrated seawater as claimed in claim 4, wherein the carbon dioxide used for carbonizing in the magnesium extraction system in step B is obtained by concentrating carbon dioxide obtained by a carbon dioxide complementary collection system of a thermoelectric flue device, the concentration of carbon dioxide in the thermoelectric flue gas is 13%, and the concentration of carbon dioxide after concentration is 40% -50%; the carbon dioxide used for carbonization is pressurized by 2-3 kg when in use, the temperature is 50 ℃ during carbonization reaction, and the carbonization time is 60-120min.
7. The method of claim 1, wherein the carbon dioxide used in the carbonization of the calcium extraction system in step C is concentrated by the carbon dioxide from the carbon dioxide collection system of the thermoelectric ductwork, the concentration of carbon dioxide in the thermoelectric flue gas is 13%, and the concentration of carbon dioxide after concentration is 40% -50%.
8. The method for extracting chemical elements from concentrated seawater as claimed in claim 1, wherein the carbon dioxide used in the carbonization of the calcium extraction system in step C is pressurized by 2-3 kg, sodium hydroxide is added to the concentrated seawater after magnesium removal during carbonization, the calcium ion concentration in the concentrated seawater after calcium removal is less than 0.02g/L, and the carbonate ion concentration is 0.15-0.45 g/L.
9. The method as claimed in claim 1, wherein the liquid salt obtained from the liquid salt preparation system is fed to a soda ash or chlor-alkali salt preparation system to be used as a raw material for soda ash or caustic soda preparation.
10. The method of claim 1, wherein the liquid salt obtained from the liquid salt preparation system of step D has a sodium chloride content of 120-180g/L.
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