CN117947467A - System and method for preparing iron by hydro-electric reduction of iron ore - Google Patents
System and method for preparing iron by hydro-electric reduction of iron ore Download PDFInfo
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- CN117947467A CN117947467A CN202211414722.2A CN202211414722A CN117947467A CN 117947467 A CN117947467 A CN 117947467A CN 202211414722 A CN202211414722 A CN 202211414722A CN 117947467 A CN117947467 A CN 117947467A
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- iron
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 340
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 164
- 230000009467 reduction Effects 0.000 title claims abstract description 88
- 238000000034 method Methods 0.000 title claims abstract description 53
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 130
- 239000001257 hydrogen Substances 0.000 claims abstract description 130
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 130
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 117
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 90
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 55
- 230000023556 desulfurization Effects 0.000 claims abstract description 55
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims abstract description 50
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 230000008569 process Effects 0.000 claims abstract description 32
- 238000001914 filtration Methods 0.000 claims abstract description 31
- 239000001301 oxygen Substances 0.000 claims abstract description 30
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 30
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 29
- 238000000746 purification Methods 0.000 claims abstract description 26
- 239000002893 slag Substances 0.000 claims abstract description 23
- 239000011790 ferrous sulphate Substances 0.000 claims abstract description 20
- 235000003891 ferrous sulphate Nutrition 0.000 claims abstract description 20
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims abstract description 20
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims abstract description 20
- 239000012141 concentrate Substances 0.000 claims abstract description 10
- 238000002360 preparation method Methods 0.000 claims abstract description 5
- 238000006722 reduction reaction Methods 0.000 claims description 121
- 239000007788 liquid Substances 0.000 claims description 80
- 239000000243 solution Substances 0.000 claims description 71
- 239000012528 membrane Substances 0.000 claims description 52
- 238000004519 manufacturing process Methods 0.000 claims description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- 239000007789 gas Substances 0.000 claims description 32
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 28
- 229910052802 copper Inorganic materials 0.000 claims description 28
- 239000010949 copper Substances 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 28
- 239000007787 solid Substances 0.000 claims description 23
- 239000000047 product Substances 0.000 claims description 21
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 20
- 239000010936 titanium Substances 0.000 claims description 20
- 230000005611 electricity Effects 0.000 claims description 19
- 150000003839 salts Chemical class 0.000 claims description 18
- 238000005868 electrolysis reaction Methods 0.000 claims description 16
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 claims description 14
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 12
- 230000009471 action Effects 0.000 claims description 12
- 230000002829 reductive effect Effects 0.000 claims description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 229910001200 Ferrotitanium Inorganic materials 0.000 claims description 10
- 229910000978 Pb alloy Inorganic materials 0.000 claims description 10
- KACAUYDQOUENGF-UHFFFAOYSA-N [Ta].[Ru].[Ir] Chemical compound [Ta].[Ru].[Ir] KACAUYDQOUENGF-UHFFFAOYSA-N 0.000 claims description 10
- 239000004568 cement Substances 0.000 claims description 10
- 238000011946 reduction process Methods 0.000 claims description 10
- 239000010935 stainless steel Substances 0.000 claims description 10
- 229910001220 stainless steel Inorganic materials 0.000 claims description 10
- 229910052719 titanium Inorganic materials 0.000 claims description 10
- 239000006227 byproduct Substances 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical group [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- 229910052595 hematite Inorganic materials 0.000 claims description 7
- 239000011019 hematite Substances 0.000 claims description 7
- 229910052786 argon Inorganic materials 0.000 claims description 6
- 239000003638 chemical reducing agent Substances 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 6
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 239000012266 salt solution Substances 0.000 claims description 5
- 238000005243 fluidization Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 4
- 239000011734 sodium Substances 0.000 claims description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 3
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 claims 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 claims description 3
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 239000011575 calcium Substances 0.000 claims description 3
- 229910052791 calcium Inorganic materials 0.000 claims description 3
- 229910001447 ferric ion Inorganic materials 0.000 claims description 3
- 238000001728 nano-filtration Methods 0.000 claims description 3
- 238000001223 reverse osmosis Methods 0.000 claims description 3
- 239000010703 silicon Substances 0.000 claims description 3
- 229910052710 silicon Inorganic materials 0.000 claims description 3
- 229910052708 sodium Inorganic materials 0.000 claims description 3
- 238000000108 ultra-filtration Methods 0.000 claims description 3
- 238000000909 electrodialysis Methods 0.000 claims description 2
- 229910001448 ferrous ion Inorganic materials 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 230000003009 desulfurizing effect Effects 0.000 claims 1
- 238000004064 recycling Methods 0.000 abstract description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 8
- 239000002253 acid Substances 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000001569 carbon dioxide Substances 0.000 abstract description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 3
- 238000005272 metallurgy Methods 0.000 abstract description 3
- 229910052717 sulfur Inorganic materials 0.000 abstract description 3
- 239000011593 sulfur Substances 0.000 abstract description 3
- 238000003763 carbonization Methods 0.000 abstract description 2
- 230000008929 regeneration Effects 0.000 abstract description 2
- 238000011069 regeneration method Methods 0.000 abstract description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 239000003792 electrolyte Substances 0.000 description 12
- 239000011248 coating agent Substances 0.000 description 8
- 238000000576 coating method Methods 0.000 description 8
- 239000012535 impurity Substances 0.000 description 8
- 238000002386 leaching Methods 0.000 description 8
- 230000002378 acidificating effect Effects 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- 238000003723 Smelting Methods 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 4
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 4
- 238000004090 dissolution Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 239000003011 anion exchange membrane Substances 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 238000002848 electrochemical method Methods 0.000 description 3
- 239000008151 electrolyte solution Substances 0.000 description 3
- 229940021013 electrolyte solution Drugs 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 150000002505 iron Chemical class 0.000 description 3
- 229910052683 pyrite Inorganic materials 0.000 description 3
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 3
- 239000011028 pyrite Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 239000003929 acidic solution Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000000151 deposition Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000010416 ion conductor Substances 0.000 description 2
- -1 iron ion Chemical class 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- YDZQQRWRVYGNER-UHFFFAOYSA-N iron;titanium;trihydrate Chemical compound O.O.O.[Ti].[Fe] YDZQQRWRVYGNER-UHFFFAOYSA-N 0.000 description 2
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 230000009897 systematic effect Effects 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910001341 Crude steel Inorganic materials 0.000 description 1
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 229910001209 Low-carbon steel Inorganic materials 0.000 description 1
- 229910000503 Na-aluminosilicate Inorganic materials 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 239000010405 anode material Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- NFMAZVUSKIJEIH-UHFFFAOYSA-N bis(sulfanylidene)iron Chemical compound S=[Fe]=S NFMAZVUSKIJEIH-UHFFFAOYSA-N 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000000404 calcium aluminium silicate Substances 0.000 description 1
- 235000012215 calcium aluminium silicate Nutrition 0.000 description 1
- WNCYAPRTYDMSFP-UHFFFAOYSA-N calcium aluminosilicate Chemical compound [Al+3].[Al+3].[Ca+2].[O-][Si]([O-])=O.[O-][Si]([O-])=O.[O-][Si]([O-])=O.[O-][Si]([O-])=O WNCYAPRTYDMSFP-UHFFFAOYSA-N 0.000 description 1
- 229940078583 calcium aluminosilicate Drugs 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229960002089 ferrous chloride Drugs 0.000 description 1
- 229940096119 hydromet Drugs 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 229910001510 metal chloride Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000000429 sodium aluminium silicate Substances 0.000 description 1
- 235000012217 sodium aluminium silicate Nutrition 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- SONHXMAHPHADTF-UHFFFAOYSA-M sodium;2-methylprop-2-enoate Chemical compound [Na+].CC(=C)C([O-])=O SONHXMAHPHADTF-UHFFFAOYSA-M 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention belongs to the field of energy and metallurgy. In particular, the invention discloses a system and a method for preparing iron by hydro-electric reduction of iron ore. The fluidized hydrogen is used for reducing the iron concentrate into low-valence iron oxide, so that the acidolysis efficiency is improved, and the low-acid conversion is realized. Through high-temperature desulfurization, the recycling utilization of acidolysis slag and purification slag and the recycling of sulfur element are realized. The acidolysis process is enhanced by the reducibility of sulfur dioxide through the acidolysis filtering process of sulfur dioxide. The valence state control of ferrous sulfate solution, the preparation of pure iron, the regeneration of sulfuric acid, and the recycling of oxygen and hydrogen are realized through electroreduction. The solar furnace generates a high-temperature medium to supply heat for fluidized hydrogen reduction and high-temperature desulfurization processes, so that low-carbonization of energy is realized. The invention is suitable for large-scale continuous hydrogen electro-reduction iron ore to prepare iron, and has the advantages of high efficiency, low energy consumption, no pollution, ultralow carbon dioxide emission and the like.
Description
Technical Field
The invention belongs to the field of energy and metallurgy, and particularly relates to a system and a method for preparing iron by hydrogen electro-reduction of iron ore.
Background
The crude steel output of China in 2021 is about 10 hundred million tons, and the discharged CO 2 is about 18 hundred million tons, which accounts for 16 percent of the total discharged of China. The steel industry in China mainly uses the equal-length flow modes of a blast furnace and a converter (accounting for 90 percent of the flow), wherein blast furnace ironmaking is a main section for discharging CO 2, and accounts for about 70 percent of the whole flow. The blast furnace ironmaking uses coke as a reducing agent to remove oxygen in the iron ore, obtain molten iron and discharge a large amount of CO 2. In the context of "carbon peaks", "carbon neutralization", the iron and steel industry is highly in need of developing a revolutionary low carbon iron making technology.
The currently developed ultra-low carbon iron making technology is mainly a technical route for replacing coke. Including hydrogen reduction instead of carbon reduction and electrical reduction instead of carbon reduction.
The hydrogen reduction route, namely, hydrogen production by water electrolysis and hydrogen reduction of iron. Patent CN112159880B discloses a method and apparatus for hydrogen-making, in which iron-ore-containing raw materials are subjected to microwave irradiation in a hydrogen or hydrogen-rich gas atmosphere to achieve hydrogen-rich or pure hydrogen-containing smelting of iron ore, and direct reduced iron can be obtained. Solves the problem that the reduction of iron oxide by hydrogen-rich gas in the existing hydrogen iron making still causes the discharge of a large amount of carbon dioxide. Patent application CN102586527a discloses a new process for smelting and reducing iron by hydrogen and carbon, the heat required by the whole process is provided by oxy-coal combustion and secondary combustion of reducing gas, and compared with the existing process, the emission of CO 2 is reduced by about 10%. Patent application CN105886688A discloses a green cyclic production system, in the metal smelting process, hydrogen replaces carbon to reduce iron ore into elemental iron, CO 2 is not generated in the process, water vapor generated by smelting generates electricity, and H 2 generated by electrolysis water is recycled. However, the current industrial water electrolysis hydrogen production is mainly an alkaline water solution system, the energy efficiency is about 60%, and the hydrogen production efficiency is low. In the process of reducing iron by hydrogen, the thermodynamic equilibrium is limited, so that the single conversion rate is low, multiple cycles are needed, and the energy consumption is increased. Meanwhile, the thermal effect of hydrogen to reduce iron is poor, and a large amount of heat energy needs to be additionally supplemented. Overall, "hydro metallurgy" consumes essentially green electrical energy, which is electro-metallurgy. The development of one-step electrochemical reduction of iron is also of great significance.
Under the electrochemical action, the iron ore can be decomposed into metallic iron and release oxygen. To achieve this, it is generally done in three typical systems, namely a high temperature molten salt/molten iron oxide system, an alkaline system and an acidic system. High temperature molten salt/molten iron oxide system. Patent application CN114232033A discloses a method for preparing high-purity iron by high-temperature fused salt electroreduction, which adopts a CaCl 2-Fe2O3 -CaO fused salt system, and under a certain current density and an inert atmosphere of argon at 850 ℃, a high-purity iron product with the purity of 99.94% can be obtained by fused salt electroreduction. Patent CN101906646B discloses a method for preparing metallic iron by electrolyzing iron ore with molten salt, which adopts Fe 2O3-Al2O3-SiO2 molten salt system, and obtains metallic iron by molten salt electroreduction under certain current density and electrolysis temperature (1580-1620 ℃). Patent CN109477232B discloses a preparation method of reducing iron by using an electrolytic deposition method through fused salt electroreduction under a certain voltage (1.5V/2.5V) and an electrolysis temperature (1000 ℃) by adopting a Na 2O2-B2O3-Fe2O3 fused salt system to obtain metal iron with 97% purity. At present, the main problems of the high-temperature molten salt/molten ferric oxide system are the development of economic inert anode materials, a proper electrolyte system, the purification of raw materials and the like.
An alkaline solution electroreduction iron-making technical route. Allanore A et al (DOI: 10.1149/1.2790285) have experimentally confirmed the possibility of iron formation by electrolytic suspension of a solution of iron oxide particles (iron ion concentration 2.6X10- -3 M) in a sodium hydroxide solution (mass concentration 50%, temperature 110 ℃ C.), but also mention the problem of very low reduction efficiency due to low hematite solubility in the system. Patent CN101696510B discloses a method and apparatus for preparing high-purity iron powder by electrolytic deoxidation, which relates to an electrochemical method for obtaining high-purity iron from solid iron oxide. The solid ferric oxide is a sintered body or ore with single or mixed Fe 2O3、Fe3O4 and FeO, the cathode and the anode are respectively positioned at two ends of the electrolytic tank, an ion conductor membrane and a high-temperature hydroxide solution (sodium hydroxide or potassium hydroxide, the temperature is 700-800 ℃) are arranged in the electrolytic tank, a preset voltage is arranged between the cathode and the anode to drive oxygen ions to diffuse from the ferric oxide in the cathode basket to the anode, and high-purity iron can be obtained on the cathode. However, the anode in the patent must be a solid material with strong alkali resistance, corrosion resistance and good conductivity, and the solid oxygen ion conductor membrane must also have the characteristics of alkali resistance and corrosion resistance, so that the cost is high. In addition, in order to prevent the dissolution of impurities in solid iron oxide in high-temperature alkaline solution from adversely affecting the electrolyte performance, the iron oxide needs to be subjected to impurity removal pretreatment, and this process leads to a significant increase in economic and environmental costs.
An acidic solution electroreduction process for preparing iron. Researchers have performed a great deal of work on the electroreduction of acidic iron-containing solutions to produce iron, primarily for the purpose of producing high purity metallic iron and pure iron powders. In this process, the most common electrolyte solutions are ferrous chloride and ferrous sulfate. The patent application CN107955952A discloses a method for producing high-purity iron powder by utilizing iron slag, which comprises the steps of removing inorganic components such as silicon dioxide and the like in the iron slag by leaching (the components of leaching liquid comprise 15-19 parts of sodium hydroxide, 5-9 parts of sodium methacrylate sulfonate and 260-300 parts of water), improving the content of iron particles in filter residues, adding electrolyte which comprises 6-9 parts of hydrochloric acid with the volume fraction of 15%, 10-14 parts of magnesium sulfate and 900-1000 parts of water for electrolysis, and finally cleaning the surface of the iron powder by utilizing ethylenediamine tetraacetic acid solution with the mass fraction of 18-22% to obtain the high-purity iron powder. In the patent, a large amount of sodium hydroxide and hydrochloric acid are consumed in the leaching and electrolysis processes, and the leaching liquid and the electrolyte cannot be recycled due to the influence of factors such as impurities and concentration, so that the subsequent treatment is difficult. Patent CN101517129B discloses an electrochemical method for recovering iron metal and chlorine from iron-rich metal chloride solution, the pH of the catholyte is 0.9-1.1, the electroreduction temperature is 80-85 ℃, the cathode current density is 200-500A/m 2, the current efficiency is 96.4% -97.9%, and the purity of the electroreduced iron is 99.99%. The patent has high requirements for the control of impurity content and pH in the solution, and requires the adjustment of the ferric chloride solution at a relatively low pH to prevent co-precipitation caused by the pH rising above the precipitation pH of the remaining impurities at the cathode surface, but also cannot be too low to prevent the evolution of byproduct hydrogen.
Acidic FeSO 4 electrolyte solution. Patent application CN113481540A discloses a method for preparing high-purity iron, which adopts a soluble anode, electrolyte mainly contains FeSO 4 and a small amount of stabilizer, the current density of the cathode is 100-230A/m 2, the pH value of the electrolyte is 1.00-4.00, the temperature of the electrolyte is 20-100 ℃, the purity of the electrolytically prepared iron is 99.90-99.99%, and the deposition thickness is 20 mu m-3 cm. The patent adopts a sulfuric acid system, and the soluble anode is industrial pure iron, low-carbon steel and the like, so that the electrolyte solution has higher purity. If the electrolyte purity is reduced, a plurality of side reactions, current efficiency reduction, impurity pollution and other problems are caused. Patent CN102084034B discloses an electrochemical method for recovering metallic iron or iron-rich alloy, oxygen and sulfuric acid from iron-rich metal sulfate waste (ilmenite sulfate method by-product), wherein electrolyte is iron-rich metal sulfate solution, pH of the electrolyte is 1.4-3.5, temperature of the electrolyte is 25-60 ℃, current density of a cathode used is 300-1000A/m 2, purity of prepared iron by electrolysis can reach 99.99%, and current efficiency is 95% -98%. The iron-rich metal sulfate solution in this patent must be pretreated (e.g., pH adjusted) and then electroreduced, and the acidic insoluble solids produced by this process are not readily handled. In addition, E.Mostad et al (DOI: 10.1016/j.hydromet.2007.07.014) mentioned that one of the smelters in Norway had been using pyrite (FeS 2) as a raw material during 1947 to 1957, and carried out semi-industrial tests on FeSO 4 solutions produced by calcination, sulfuric acid leaching and the like in pilot plant, to finally obtain high purity metallic iron. The process takes iron ore (pyrite) as a raw material for the first time, and produces metallic iron through electric reduction, and 1.5 multiplied by 10 5 kg of high-purity iron is produced in the two years 1955-1957, wherein the current efficiency reaches 85%, and the energy consumption is 4.25kWh/kg of iron. Badenhorst et al (DOI: 10.3390/membranes 9110137) found that the use of the novel BM-5AEM anion exchange membrane achieved a current efficiency of 95% for electrolytic iron, an energy consumption of 3.53kWh/kg iron, better stability and lower energy consumption than existing Pyror process flows. Meanwhile, the study found that when the concentration of iron in the solution was less than 5g/L, the side reaction of the cathode resulted in a decrease in the process efficiency. However, these documents mainly use pyrite or ferrous sulfate as a raw material, and are less studied for a wider range of hematite or magnetite. Patent applications WO2022204379A1 and WO2022197954A1 disclose a process for producing pure iron from iron ore and for removing impurities from the solution by first thermally reducing one or more non-magnetite iron oxide components of the iron ore in the presence of a reducing agent to form magnetite, then dissolving the magnetite using an acid to form an acidic iron salt solution, partially separating undissolved impurities, and then subjecting the acidic iron salt to electrolysis to obtain high purity iron, the remaining solution being recycled back to the acidolysis tank. However, the reducing agent mentioned in the patent is mainly hydrogen, and the hydrogen is generated by the chemical reaction of iron metal and acid, so that the cost is increased by adding iron metal, and meanwhile, a great amount of hydrogen and heat are easily and instantaneously generated by the exothermic reaction, so that the device and the safety are greatly influenced. In addition, the method reduces iron ore into magnetite by thermal reduction, that is, reduces the valence state of part of iron in the iron ore by thermal reduction means so as to promote dissolution of the ore, mainly because the higher the reduction degree of iron in the iron ore, the higher the leaching rate (DOI: 10.3321/j. Issn: 1005-3026.2008.12.017), but there is no mention in the patent of how reduction of the iron ore is achieved in an efficient manner, and the heat generated in the process cannot be recycled. In addition, the acidity of the acid used in the method for dissolving magnetite is high, and the acidity of the solution recycled back to the acidolysis tank after electrolysis is low, so that the problem that the magnetite is difficult to dissolve due to unmatched acidity is easily caused. Patent applications WO2022204387A1, WO2022204391A1 and WO2022204394A1 disclose a method for iron ore dissolution, conversion and systematic operation, in which iron-containing ore is dissolved into an acidic iron salt solution, fe 3+ is reduced in a first electrolytic cell to form Fe 2+, the Fe 2+ formed is subsequently transferred from the first electrolytic cell to a second electrolytic cell for reduction to high purity iron, and the remaining solution is returned to the dissolution tank. In the method, a Proton Exchange Membrane (PEM) and an Anion Exchange Membrane (AEM) are respectively adopted in the first electrolytic cell and the second electrolytic cell, and the types of the diaphragms of the electrolytic cells are increased by two different types of ion membranes, so that the use cost is increased. Also, it is mentioned in the patent that the volume of solution entering the cathode compartment is smaller than the volume of solution entering the anode compartment in the second electrolytic cell, which increases the complexity of the process and at the same time will lead to a reduced efficiency of iron utilization. Because hydrochloric acid is also used for dissolving magnetite in the patent, the introduction of chloride ions can lead to the occurrence of competitive reaction of the anode, increase the risk of separating out chlorine, and simultaneously easily aggravate the loss of an ionic membrane and increase the cost. In addition, the patent does not propose recycling of the precipitated oxygen.
Currently, ferrous electrolytes in acidic solution electroreduction iron production generally take ferrous iron as a main component, and raw materials mainly come from pyrite and ilmenite containing ferrous iron. When using the wider hematite or magnetite as raw materials, the related reports are less, and a series of new problems are faced: the acid production of the electroreduction anode is not matched with the acidity of the leaching electrode, and the acidity of the leaching final acid is not matched with the acidity of the electroreduction cathode, so that sulfuric acid medium is difficult to circulate, acidolysis is strengthened, water in membrane (ionic membrane) electroreduction is circulated, ferric sulfate solution is purified, acidolysis/purification slag is difficult to use, and the like. In summary, the current technology for producing iron by hydrogen reduction or electric reduction still has a restriction bottleneck. Therefore, by technological innovation, the development of a systematic new low-carbon electrometallurgical technology of iron ore has important significance.
Disclosure of Invention
Aiming at the problems, the invention provides a system and a method for preparing iron by hydro-electric reduction of iron ore, so as to realize efficient treatment of preparing iron by large-scale continuous hydro-electric reduction of iron ore and recycling of byproduct resources. In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a method for preparing iron by hydrogen electro-reduction of iron ore, which comprises a hydrogen reduction process 1, an acidolysis purification process 2 and an electro-reduction iron preparation process 3;
the hydrogen reduction process 1 comprises a fluidized hydrogen reduction device 1-1 and an electrolyzed water hydrogen production device 1-2;
the acidolysis purification process 2 comprises an acidolysis filter device 2-1, a purification device 2-2, a high-temperature desulfurization device 2-3, a sulfuric acid heat exchanger 2-4, a solar furnace 2-5 and a sulfur dioxide heat exchanger 2-6;
The electroreduction iron making process 3 comprises a valence state control device 3-1, an electroreduction device 3-2, a membrane separation device 3-3, a catholyte heat exchange device 3-4 and an anolyte heat exchange device 3-5;
The feed inlet of the fluidized hydrogen reduction device 1-1 is connected with an iron concentrate feeding pipeline; the discharge port of the fluidized hydrogen reduction device 1-1 is connected with the solid feed port of the acidolysis filtering device 2-1 through a pipeline; the liquid inlet of the electrolytic water hydrogen production device 1-2 is connected with an aqueous solution pipeline; the anode of the water electrolysis hydrogen production device 1-2 is connected with the anode of the direct current green electricity through a conductive copper beam; the cathode of the water electrolysis hydrogen production device 1-2 is connected with the cathode of the direct current green electricity through a conductive copper beam; the cathode hydrogen outlet of the electrolytic water hydrogen production device 1-2 is connected with the gas inlet of the fluidization hydrogen reduction device 1-1 and the gas inlet of the high-temperature desulfurization device 2-3 through pipelines; the anode oxygen outlet of the electrolytic water hydrogen production device 1-2 is connected with an oxygen product pipeline; the fluidized hydrogen reduction device 1-1 is provided with a heat exchange jacket, and an inlet of the heat exchange jacket is connected with a solar furnace high-temperature medium through a pipeline; the outlet of the heat exchange jacket is connected with a solar furnace low-temperature medium through a pipeline;
The gas-liquid feed inlet of the acidolysis filtering device 2-1 is connected with the liquid outlet of the sulfuric acid heat exchanger 2-4, the sulfur dioxide gas outlet of the sulfur dioxide heat exchanger 2-6 and the liquid outlet of the sulfuric acid solution main pipe through pipelines; the solid discharge port of the acidolysis filtering device 2-1 is connected with the solid feed port of the high-temperature desulfurization device 2-3 through a pipeline; the liquid outlet of the acidolysis filtering device 2-1 is connected with the liquid inlet of the purifying device 2-2 through a pipeline; the liquid outlet of the purification device 2-2 is connected with the liquid inlet of the catholyte heat exchange device 3-4 through a pipeline, and the solid discharge port of the purification device 2-2 is connected with the solid feed port of the high-temperature desulfurization device 2-3 through a pipeline; the solid discharge port of the high-temperature desulfurization device 2-3 is connected with a cement clinker pipeline; the air outlet of the high-temperature desulfurization device 2-3 is connected with the air inlet of the sulfur dioxide heat exchanger 2-6 through a pipeline; a heat exchange jacket is arranged in the high-temperature desulfurization device 2-3, and a high-temperature medium inlet of the heat exchange jacket is connected with a high-temperature medium outlet of the solar furnace 2-5; the low-temperature medium outlet of the heat exchange jacket is connected with the low-temperature medium inlet of the solar furnace 2-5; the liquid inlet of the sulfuric acid heat exchanger 2-4 is connected with the liquid outlet of the anode of the electric reduction device 3-2; the air outlet of the sulfuric acid heat exchanger 2-4 is connected with a low-temperature air evacuation port; the solar furnace 2-5 is provided with a receiving window for receiving solar energy; the air inlet of the sulfur dioxide heat exchanger 2-6 is connected with an air main pipe; the high-temperature air outlet of the sulfur dioxide heat exchanger 2-6 is connected with the air inlet of the sulfuric acid heat exchanger 2-4, the air inlet 3-4 of the catholyte heat exchange device and the air inlet 3-5 of the anolyte heat exchange device through pipelines;
The cathode liquid inlet of the valence state control device 3-1 is connected with the liquid outlet of the cathode liquid heat exchange device 3-4; the anode liquid inlet of the valence state control device 3-1 is connected with the liquid outlet of the anode liquid heat exchange device 3-5; the anode liquid outlet of the valence state control device 3-1 is connected with the anode liquid inlet of the electric reduction device 3-2 and the liquid inlet of the anolyte heat exchange device 3-5 through a pipeline; the anode gas outlet of the valence state control device 3-1 is connected with an oxygen product pipeline; the cathode liquid outlet of the valence state control device 3-1 is connected with the cathode liquid inlet of the electric reduction device 3-2 through a pipeline; the anode of the valence state control device 3-1 is connected with the anode of the direct current green electricity through a conductive copper beam; the cathode of the valence state control device 3-1 is connected with the cathode of the direct current green electricity through a conductive copper beam; the cathode liquid inlet of the electro-reduction device 3-2 is connected with the ferrous sulfate solution discharge port of the membrane separation device 3-3 through a pipeline; the anode of the electric reduction device 3-2 is connected with the anode of the direct-current green electricity through a conductive copper beam; the cathode of the electric reduction device 3-2 is connected with the cathode of the direct-current green electricity through a conductive copper beam; the anode gas outlet of the electroreduction device 3-2 is connected with an oxygen product pipeline; the cathode liquid outlet of the electro-reduction device 3-2 is connected with the liquid inlet of the membrane separation device 3-3 through a pipeline; the cathode outlet of the electric reduction device 3-2 is connected with the hydrogen outlet and the hydrogen product inlet of the electrolytic water hydrogen production device 1-2 through pipelines; the pure iron outlet of the electroreduction device 3-2 is designed to be open; the regenerated water outlet of the membrane separation device 3-3 is connected with the liquid inlet of the anolyte heat exchange device 3-5; the air outlet of the catholyte heat exchange device 3-4 is connected with a low-temperature air evacuation pipe; the air outlet of the anolyte heat exchange device 3-5 is connected with a low-temperature air evacuation pipe.
The method for preparing iron by hydro-electro-reduction of iron ore based on the system of the invention comprises the following steps:
the iron concentrate is sent into the fluidized hydrogen reduction device 1-1 and undergoes a reduction reaction with green hydrogen from the electrolytic water hydrogen production device 1-2 and the electric reduction device 3-2 to obtain low-valence iron oxide; delivering the low-valence iron oxide to the acidolysis filtering device 2-1; in the fluidized hydrogen reduction device 1-1, a solar furnace high-temperature medium is adopted to circularly provide reaction heat;
In the acidolysis filtering device 2-1, the low-valence iron oxide reacts with concentrated sulfuric acid from a liquid outlet of the sulfuric acid heat exchanger 2-4, sulfur dioxide from a gas outlet of the sulfur dioxide heat exchanger 2-6 and sulfuric acid in a sulfuric acid solution main pipe to obtain acidolysis slurry; the sulfuric acid solution is used for starting the system for the first time; filtering acidolysis slurry to obtain acidolysis slag and acidolysis solution; delivering acidolysis slag to a high-temperature desulfurization device 2-3 for treatment; delivering acidolysis solution to a purifying device (2-2) for treatment; in the high-temperature desulfurization device 2-3, acidolysis slag and purified slag from the purification device 2-2 are subjected to high-temperature desulfurization reaction in the presence of hydrogen to obtain sulfur dioxide gas and cement clinker; delivering and utilizing cement clinker; the solar furnace 2-5 converts solar energy into heat energy, preheats a medium, and the high-temperature medium circulates to provide reaction heat for the high-temperature desulfurization device 2-3; in the purifying device 2-2, the purified ferric sulfate solution is preheated by a catholyte heat exchange device 3-4 and then sent to the valence state control device 3-1; the high-temperature sulfur dioxide discharged from the high-temperature desulfurization device 2-3 exchanges heat with air through the sulfur dioxide heat exchanger 2-6, and the cooled sulfur dioxide is sent to acidolysis filtration (2-1); the preheated high-temperature air enters the catholyte heat exchange device 3-4, the anolyte heat exchange device 3-5 and the sulfuric acid heat exchanger 2-4 respectively, and heat is provided for the preheated high-temperature air through heat exchange;
in the valence state control device 3-1, the cathode chamber ferric salt solution is electrically reduced into ferrous sulfate under the action of direct current; the valence state control device 3-1 separates out oxygen and generates sulfuric acid under the action of direct current in the anode chamber solution; an oxygen product delivery pipe; mixing 1% -20% of the sulfuric acid solution with the regenerated water generated by the membrane separation device 3-3, circulating to the anolyte heat exchange device 3-5, entering the anolyte inlet of the valence state control device 3-1, and delivering the rest sulfuric acid solution into the anode chamber of the electroreduction device 3-2; in the electroreduction device 3-2, ferrous sulfate solution from the cathode chamber of the valence control device 3-1 and the membrane separation device 3-3 is reduced into pure iron, hydrogen gas as a byproduct and residual dilute ferrous sulfate solution under the action of direct current; hydrogen is sent to the fluidized hydrogen reduction device 1-1 and the high temperature desulfurization device 2-3 for utilization or used as a hydrogen product; and delivering the dilute ferrous sulfate solution to the membrane separation device 3-3 for treatment.
One of the features of the present invention is that: the fluidized hydrogen reduction device 1-1 adopts a fluidized bed reactor, green hydrogen is used as a reducing agent, the reaction temperature is 300-800 ℃, and the residence time is as follows: 10min-50min.
The second feature of the present invention is that: the iron concentrate is hematite and/or magnetite, and the iron oxide grade is not lower than 90%.
The third feature of the present invention is that: in the acidolysis filter device 2-1, sulfuric acid solution is used for starting the system for the first time, the concentration of the concentrated sulfuric acid solution is not lower than 100g/L, and the acidolysis temperature is 50-100 ℃.
The fourth feature of the invention is that: in the acidolysis filter device 2-1, part of ferric ions generated in the acidolysis process are reduced into ferrous ions under the action of sulfur dioxide, so that the reduction acidolysis is realized, the acidolysis efficiency is improved, and the acidolysis rate is more than 98%.
The fifth characteristic of the invention is that: in the high-temperature desulfurization device 2-3, a fluidized bed or rotary kiln reactor is adopted, the reaction temperature is 1000-1500 ℃, and the desulfurization rate is more than 99%.
The sixth feature of the invention is that: in the valence control device 3-1, the diaphragm is made of an ionic membrane or a porous membrane, wherein the seepage rate of the porous membrane is 1% -30%, the current density is 50A/m 2-1000A/m2, the anode is a lead alloy or titanium-based ruthenium iridium tantalum coating electrode, the cathode is made of iron, copper, titanium or stainless steel, and the reaction temperature is 20 ℃ -100 ℃.
The seventh feature of the invention is that: in the electro-reduction device 3-2, the diaphragm is made of an ionic membrane or a porous membrane, wherein the seepage rate of the porous membrane is 1% -30%, the current density is 50A/m 2-2000A/m2, the anode is a lead alloy and/or titanium-based ruthenium iridium tantalum coating electrode, the cathode comprises one or more of iron, copper, titanium and stainless steel materials, the reaction temperature is 60-100 ℃, the current efficiency is above 95%, the purity of the cathode iron is above 99%, and the direct current consumption per ton of iron is lower than 3500kWh.
The eighth feature of the present invention is that: the membrane separation device 3-3 comprises one or more of reverse osmosis, ultrafiltration, nanofiltration and electrodialysis.
The ninth aspect of the present invention is characterized in that: the solar furnace 2-5 converts solar energy into heat energy, the solar heating medium can be molten salt and/or gas, the molten salt comprises one or more of elements such as silicon, sodium, oxygen, calcium, aluminum and the like, the gas comprises nitrogen and/or argon, namely, the heating medium can be molten salt comprising elements such as silicon, sodium, oxygen, calcium, aluminum and the like, and can also be gas comprising nitrogen, argon and mixed gas thereof.
The invention is characterized in that: the solar furnace 2-5 is adopted to heat to obtain a high-temperature medium to provide heat for high-temperature desulfurization.
The eleventh feature of the present invention is that: the air and the high-temperature sulfur dioxide are adopted for heat exchange to obtain high-temperature air, and heat is supplied to catholyte, anolyte and sulfuric acid solution, so that energy cascade utilization is realized.
The invention has twelve characteristics that: and the hydrogen gas part which is a byproduct of the electro-reduction process is used as a reducing agent in the high-temperature desulfurization process and the fluidization hydrogen reduction process, and the rest is used as a hydrogen product.
The invention is characterized in that: the electroreduction iron making process adopts a valence state control and electroreduction two-step method, solves the influence of ferric ions in the process of electrodepositing iron, and improves the production efficiency.
The fourteenth feature of the invention is: the solar furnace 2-5 is adopted to heat to obtain a high-temperature medium to provide heat for the fluidized hydrogen reduction process.
According to the invention, the fluidized hydrogen is used for reducing the iron concentrate into the low-valence iron oxide, so that the acidolysis efficiency is improved, and the low-acid conversion is realized. Through high-temperature desulfurization, the recycling utilization of acidolysis slag and purification slag and the recycling of sulfur element are realized. The acidolysis process is enhanced by the reducibility of sulfur dioxide through the acidolysis filtering process of sulfur dioxide. The valence state control of ferrous sulfate solution, the preparation of pure iron, the regeneration of sulfuric acid, and the recycling of oxygen and hydrogen are realized through electroreduction. Through the membrane separation of the dilute ferrous sulfate solution, the cross circulation of catholyte and anolyte is realized, and the production efficiency is improved. The solar furnace generates a high-temperature medium to supply heat for fluidized hydrogen reduction and high-temperature desulfurization processes, so that low-carbonization of energy is realized. The high-temperature sulfur dioxide is used for preheating air, and the high-temperature air is used for supplying heat for the processes of electric reduction iron production and acidolysis filtration, so that the cascade utilization of heat is realized.
Compared with the prior art, the invention has the following outstanding advantages:
(1) The energy source for producing hydrogen by electrolyzing water is green electric energy, and the produced hydrogen and oxygen can be recycled;
(2) The sulfur element can be recycled in the system without emission, so that the system is safe and environment-friendly;
(3) The acidolysis slag and the purification slag can be recycled to be made into cement clinker;
(4) The process is simple, the production cost is low, and the product purity is high;
(5) Realizing ultralow emission of carbon dioxide;
The method for preparing iron by hydrogen electro-reduction of iron ore can not only obtain high-purity iron, but also realize the recycling of acidolysis slag and purification slag and the recycling of sulfuric acid byproducts. The invention is suitable for large-scale continuous hydrogen electro-reduction iron ore to prepare iron, and has the advantages of high efficiency, low energy consumption, no pollution, ultralow carbon dioxide emission and the like.
Drawings
Fig. 1 is a schematic configuration diagram of a system for producing iron by hydro-electric reduction of iron ore according to the present invention.
Reference numerals
The method comprises the steps of (1) a hydrogen reduction process, (1-1) a fluidized hydrogen reduction device, (1-2) an electrolytic water hydrogen production device, (2) an acidolysis purification process, (2-1) an acidolysis filtration device, (2-2) a purification device, (2-3) a high-temperature desulfurization device, (2-4) a sulfuric acid heat exchanger, (2-5) a solar furnace, (2-6) a sulfur dioxide heat exchanger, (3) an electric reduction iron production process, (3-1) a valence control device, (3-2) an electric reduction device, (3-3) a membrane separation device, (3-4) a catholyte heat exchange device and (3-5) an anolyte heat exchange device.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present invention more apparent, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. It should be noted that the examples are only for illustrating the technical scheme of the present invention and are not limiting. Fig. 1 is a schematic diagram of a system and a method for producing iron by hydro-electric reduction of iron ore according to the present invention.
Example 1
Referring to fig. 1, the system for producing iron by hydrogen electro-reduction of iron ore used in the present embodiment includes a hydrogen reduction process 1, an acidolysis purification process 2, and an electro-reduction iron production process 3;
the hydrogen reduction process 1 comprises a fluidized hydrogen reduction device 1-1 and an electrolyzed water hydrogen production device 1-2;
the acidolysis purification process 2 comprises an acidolysis filter device 2-1, a purification device 2-2, a high-temperature desulfurization device 2-3, a sulfuric acid heat exchanger 2-4, a solar furnace 2-5 and a sulfur dioxide heat exchanger 2-6;
The electroreduction iron making process 3 comprises a valence state control device 3-1, an electroreduction device 3-2, a membrane separation device 3-3, a catholyte heat exchange device 3-4 and an anolyte heat exchange device 3-5;
The feed inlet of the fluidized hydrogen reduction device 1-1 is connected with an iron concentrate feeding pipeline; the discharge port of the fluidized hydrogen reduction device 1-1 is connected with the solid feed port of the acidolysis filtering device 2-1 through a pipeline; the liquid inlet of the electrolytic water hydrogen production device 1-2 is connected with an aqueous solution pipeline; the anode of the water electrolysis hydrogen production device 1-2 is connected with the anode of the direct current green electricity through a conductive copper beam; the cathode of the water electrolysis hydrogen production device 1-2 is connected with the cathode of the direct current green electricity through a conductive copper beam; the cathode hydrogen outlet of the electrolytic water hydrogen production device 1-2 is connected with the gas inlet of the fluidization hydrogen reduction device 1-1 and the gas inlet of the high-temperature desulfurization device 2-3 through pipelines; the anode oxygen outlet of the electrolytic water hydrogen production device 1-2 is connected with an oxygen product pipeline; the fluidized hydrogen reduction device 1-1 is provided with a heat exchange jacket, and an inlet of the heat exchange jacket is connected with a solar furnace high-temperature medium through a pipeline; the outlet of the heat exchange jacket is connected with a solar furnace low-temperature medium through a pipeline;
The gas-liquid feed inlet of the acidolysis filtering device 2-1 is connected with the liquid outlet of the sulfuric acid heat exchanger 2-4, the sulfur dioxide gas outlet of the sulfur dioxide heat exchanger 2-6 and the liquid outlet of the sulfuric acid solution main pipe through pipelines; the solid discharge port of the acidolysis filtering device 2-1 is connected with the solid feed port of the high-temperature desulfurization device 2-3 through a pipeline; the liquid outlet of the acidolysis filtering device 2-1 is connected with the liquid inlet of the purifying device 2-2 through a pipeline; the liquid outlet of the purification device 2-2 is connected with the liquid inlet of the catholyte heat exchange device 3-4 through a pipeline, and the solid discharge port of the purification device 2-2 is connected with the solid feed port of the high-temperature desulfurization device 2-3 through a pipeline; the solid discharge port of the high-temperature desulfurization device 2-3 is connected with a cement clinker pipeline; the air outlet of the high-temperature desulfurization device 2-3 is connected with the air inlet of the sulfur dioxide heat exchanger 2-6 through a pipeline; a heat exchange jacket is arranged in the high-temperature desulfurization device 2-3, and a high-temperature medium inlet of the heat exchange jacket is connected with a high-temperature medium outlet of the solar furnace 2-5; the low-temperature medium outlet of the heat exchange jacket is connected with the low-temperature medium inlet of the solar furnace 2-5; the liquid inlet of the sulfuric acid heat exchanger 2-4 is connected with the liquid outlet of the anode of the electric reduction device 3-2; the air outlet of the sulfuric acid heat exchanger 2-4 is connected with a low-temperature air evacuation port; the solar furnace 2-5 is provided with a receiving window for receiving solar energy; the air inlet of the sulfur dioxide heat exchanger 2-6 is connected with an air main pipe; the high-temperature air outlet of the sulfur dioxide heat exchanger 2-6 is connected with the air inlet of the sulfuric acid heat exchanger 2-4, the air inlet 3-4 of the catholyte heat exchange device and the air inlet 3-5 of the anolyte heat exchange device through pipelines;
The cathode liquid inlet of the valence state control device 3-1 is connected with the liquid outlet of the cathode liquid heat exchange device 3-4; the anode liquid inlet of the valence state control device 3-1 is connected with the liquid outlet of the anode liquid heat exchange device 3-5; the anode liquid outlet of the valence state control device 3-1 is connected with the anode liquid inlet of the electric reduction device 3-2 and the liquid inlet of the anolyte heat exchange device 3-5 through a pipeline; the anode gas outlet of the valence state control device 3-1 is connected with an oxygen product pipeline; the cathode liquid outlet of the valence state control device 3-1 is connected with the cathode liquid inlet of the electric reduction device 3-2 through a pipeline; the anode of the valence state control device 3-1 is connected with the anode of the direct current green electricity through a conductive copper beam; the cathode of the valence state control device 3-1 is connected with the cathode of the direct current green electricity through a conductive copper beam; the cathode liquid inlet of the electro-reduction device 3-2 is connected with the ferrous sulfate solution discharge port of the membrane separation device 3-3 through a pipeline; the anode of the electric reduction device 3-2 is connected with the anode of the direct-current green electricity through a conductive copper beam; the cathode of the electric reduction device 3-2 is connected with the cathode of the direct-current green electricity through a conductive copper beam; the anode gas outlet of the electroreduction device 3-2 is connected with an oxygen product pipeline; the cathode liquid outlet of the electro-reduction device 3-2 is connected with the liquid inlet of the membrane separation device 3-3 through a pipeline; the cathode outlet of the electric reduction device 3-2 is connected with the hydrogen outlet and the hydrogen product inlet of the electrolytic water hydrogen production device 1-2 through pipelines; the pure iron outlet of the electroreduction device 3-2 is designed to be open; the regenerated water outlet of the membrane separation device 3-3 is connected with the liquid inlet of the anolyte heat exchange device 3-5; the air outlet of the catholyte heat exchange device 3-4 is connected with a low-temperature air evacuation pipe; the air outlet of the anolyte heat exchange device 3-5 is connected with a low-temperature air evacuation pipe.
Example 2
This example uses a system for producing iron by hydro-electro-reduction of iron ore as described in example 1, comprising the steps of:
the iron concentrate is sent into the fluidized hydrogen reduction device 1-1 and undergoes a reduction reaction with green hydrogen from the electrolytic water hydrogen production device 1-2 and the electric reduction device 3-2 to obtain low-valence iron oxide; delivering the low-valence iron oxide to the acidolysis filtering device 2-1; in the fluidized hydrogen reduction device 1-1, a solar furnace high-temperature medium is adopted to circularly provide reaction heat;
In the acidolysis filtering device 2-1, the low-valence iron oxide reacts with concentrated sulfuric acid from a liquid outlet of the sulfuric acid heat exchanger 2-4, sulfur dioxide from a gas outlet of the sulfur dioxide heat exchanger 2-6 and sulfuric acid in a sulfuric acid solution main pipe to obtain acidolysis slurry; the sulfuric acid solution is used for starting the system for the first time; filtering acidolysis slurry to obtain acidolysis slag and acidolysis solution; delivering acidolysis slag to a high-temperature desulfurization device 2-3 for treatment; the acidolysis solution is sent to a purifying device 2-2 for treatment; in the high-temperature desulfurization device 2-3, acidolysis slag and purified slag from the purification device 2-2 are subjected to high-temperature desulfurization reaction in the presence of hydrogen to obtain sulfur dioxide gas and cement clinker; delivering and utilizing cement clinker; the solar furnace 2-5 converts solar energy into heat energy, preheats a medium, and the high-temperature medium circulates to provide reaction heat for the high-temperature desulfurization device 2-3; in the purifying device 2-2, the purified ferric sulfate solution is preheated by a catholyte heat exchange device 3-4 and then sent to the valence state control device 3-1; the high-temperature sulfur dioxide discharged from the high-temperature desulfurization device 2-3 exchanges heat with air through the sulfur dioxide heat exchanger 2-6, and the cooled sulfur dioxide is sent to acidolysis filtration (2-1); the preheated high-temperature air enters the catholyte heat exchange device 3-4, the anolyte heat exchange device 3-5 and the sulfuric acid heat exchanger 2-4 respectively, and heat is provided for the preheated high-temperature air through heat exchange;
In the valence state control device 3-1, the cathode chamber ferric salt solution is electrically reduced into ferrous sulfate under the action of direct current; the valence state control device 3-1 separates out oxygen and generates sulfuric acid under the action of direct current in the anode chamber solution; an oxygen product delivery pipe; 10% of the sulfuric acid solution is mixed with the regenerated water generated by the membrane separation device 3-3, circulated to the anolyte heat exchange device 3-5, then enters the anolyte inlet of the valence control device 3-1, and the rest sulfuric acid solution is sent into the anode chamber of the electroreduction device 3-2; in the electroreduction device 3-2, ferrous sulfate solution from the cathode chamber of the valence control device 3-1 and the membrane separation device 3-3 is reduced into pure iron, hydrogen gas as a byproduct and residual dilute ferrous sulfate solution under the action of direct current; hydrogen is sent to the fluidized hydrogen reduction device 1-1 and the high temperature desulfurization device 2-3 for utilization or used as a hydrogen product; and delivering the dilute ferrous sulfate solution to the membrane separation device 3-3 for treatment.
Example 3
In the embodiment, hematite of a certain enterprise is taken as a treatment object, and the grade of ferric oxide is 90%; a fluidized bed reactor is adopted in the fluidized hydrogen reduction device 1-1, the reaction temperature is 300 ℃, and the residence time is 50min; in acidolysis filtration 2-1, sulfuric acid solution is used for the first start of the system, the concentration is 100g/L, the acidolysis temperature is 50 ℃, and the acidolysis rate is 98%; the high-temperature desulfurization device 2-3 adopts a fluidized bed reactor, the reaction temperature is 1000 ℃, and the desulfurization rate reaches 99%; in the valence state control device 3-1, the diaphragm material is an ionic membrane, the electric reduction current density is 50A/m 2, and the reaction temperature is 20 ℃; the anode is a lead alloy or titanium-based ruthenium iridium tantalum coating electrode, and the cathode is made of iron, copper, titanium or stainless steel; in the electro-reduction device 3-2, the diaphragm is made of an ionic membrane, the electro-reduction current density is 50A/m 2, the reaction temperature is 60 ℃, the current efficiency is 95%, the purity of cathode iron is 99%, and the direct current consumption of each ton of iron is 3450kWh; the anode is a lead alloy or titanium-based ruthenium iridium tantalum coating electrode, and the cathode is made of iron, copper, titanium or stainless steel; the membrane separation device 3-3 is reverse osmosis. Solar energy is converted into heat energy by solar furnace 2-5, and the solar energy is used as a heating medium, wherein the medium is mixed molten salt of sodium aluminosilicate and calcium aluminosilicate.
Example 4
In the embodiment, hematite of a certain enterprise is taken as a treatment object, and the grade of ferric oxide is 92%; a fluidized bed reactor is adopted in the fluidized hydrogen reduction device 1-1, the reaction temperature is 500 ℃, and the residence time is 30min; in the acidolysis filter device 2-1, sulfuric acid solution is used for the first start of the system, the concentration is 120g/L, the acidolysis temperature is 80 ℃, and the acidolysis rate is 99%; the high-temperature desulfurization device 2-3 adopts a fluidized bed reactor, the reaction temperature is 1100 ℃, and the desulfurization rate reaches 99.8%; in the valence state control device 3-1, the diaphragm material is a porous film, wherein the seepage rate of the porous film is 1%, the electric reduction current density is 500A/m 2, and the reaction temperature is 60 ℃; the anode is a lead alloy or titanium-based ruthenium iridium tantalum coating electrode, and the cathode is made of iron, copper, titanium or stainless steel; in the electro-reduction device 3-2, the diaphragm is made of a porous film, wherein the seepage rate of the porous film is 1%, the electro-reduction current density is 500A/m 2, the reaction temperature is 80 ℃, the current efficiency is 98%, the purity of cathode iron is 99.5%, and the direct current consumption of each ton of iron is lower than 3390kWh; the anode is a lead alloy or titanium-based ruthenium iridium tantalum coating electrode, and the cathode is made of iron, copper, titanium or stainless steel; the membrane separation device 3-3 is nanofiltration. Solar furnace 2-5 converts solar energy into heat energy, and the solar energy heats a medium, wherein the medium is a mixed gas of nitrogen and argon.
Example 5
In the embodiment, magnetite of a certain enterprise is used as a treatment object, and the grade of ferric oxide is 92%; a fluidized bed reactor is adopted in the fluidized hydrogen reduction device 1-1, the reaction temperature is 800 ℃, and the residence time is 10min; in the acidolysis filter device 2-1, sulfuric acid solution is used for the first start of the system, the concentration is 150g/L, the acidolysis temperature is 100 ℃, and the acidolysis rate is 99%; the high-temperature desulfurization device 2-3 adopts a rotary kiln reactor, the reaction temperature is 1500 ℃, and the desulfurization rate reaches 99.9%; in the valence state control device 3-1, the diaphragm material is a porous membrane, wherein the seepage rate of the porous membrane is 30%, the electroreduction current density is 1000A/m 2, and the electroreduction temperature is 100 ℃; the anode is a lead alloy or titanium-based ruthenium iridium tantalum coating electrode, and the cathode is made of iron, copper, titanium or stainless steel; in the electro-reduction device 3-2, the diaphragm is made of a porous film, wherein the seepage rate of the porous film is 30%, the electro-reduction current density is 2000A/m 2, the electro-reduction temperature is 100 ℃, the current efficiency is 99%, the purity of cathode iron is 99.9%, and the direct current consumption of each ton of iron is lower than 3210kWh; the anode is a lead alloy or titanium-based ruthenium iridium tantalum coating electrode, and the cathode is made of iron, copper, titanium or stainless steel; the membrane separation device 3-3 is ultrafiltration. Solar furnace 2-5 converts solar energy into heat energy, and the solar energy heats a medium, wherein the medium is a mixed gas of nitrogen and argon.
The invention is not described in detail in part as being well known in the art.
There are, of course, many embodiments of the invention that can be varied and modified from the teachings of this invention by those skilled in the art, and that such variations and modifications are within the scope of the appended claims without departing from the spirit and the substance of the invention.
Claims (10)
1. A system for preparing iron by hydrogen electro-reduction of iron ore, which is characterized by comprising a hydrogen reduction process (1), an acidolysis purification process (2) and an electro-reduction iron preparation process (3);
the hydrogen reduction process (1) comprises a fluidized hydrogen reduction device (1-1) and an electrolytic water hydrogen production device (1-2);
The acidolysis purification process (2) comprises an acidolysis filtering device (2-1), a purification device (2-2), a high-temperature desulfurization device (2-3), a sulfuric acid heat exchanger (2-4), a solar furnace (2-5) and a sulfur dioxide heat exchanger (2-6);
The electroreduction iron making process (3) comprises a valence state control device (3-1), an electroreduction device (3-2), a membrane separation device (3-3), a catholyte heat exchange device (3-4) and an anolyte heat exchange device (3-5);
The feed inlet of the fluidized hydrogen reduction device (1-1) is connected with an iron concentrate feeding pipeline; the discharge port of the fluidized hydrogen reduction device (1-1) is connected with the solid feed port of the acidolysis filtering device (2-1) through a pipeline; the liquid inlet of the electrolytic water hydrogen production device (1-2) is connected with an aqueous solution pipeline; the anode of the water electrolysis hydrogen production device (1-2) is connected with the anode of the direct current green electricity through a conductive copper beam; the cathode of the water electrolysis hydrogen production device (1-2) is connected with the cathode of the direct current green electricity through a conductive copper beam; the cathode hydrogen outlet of the electrolytic water hydrogen production device (1-2) is connected with the gas inlet of the fluidization hydrogen reduction device (1-1) and the gas inlet of the high-temperature desulfurization device (2-3) through a pipeline; the anode oxygen outlet of the electrolytic water hydrogen production device (1-2) is connected with an oxygen product pipeline; the fluidized hydrogen reduction device (1-1) is provided with a heat exchange jacket, and an inlet of the heat exchange jacket is connected with a solar furnace high-temperature medium through a pipeline; the outlet of the heat exchange jacket is connected with a solar furnace low-temperature medium through a pipeline;
The gas-liquid feed inlet of the acidolysis filtering device (2-1) is connected with the liquid outlet of the sulfuric acid heat exchanger (2-4), the sulfur dioxide gas outlet of the sulfur dioxide heat exchanger (2-6) and the liquid outlet of the sulfuric acid solution main pipe through pipelines; the solid discharge port of the acidolysis filtering device (2-1) is connected with the solid feed port of the high-temperature desulfurizing device (2-3) through a pipeline; the liquid outlet of the acidolysis filtering device (2-1) is connected with the liquid inlet of the purifying device (2-2) through a pipeline; the liquid outlet of the purification device (2-2) is connected with the liquid inlet of the catholyte heat exchange device (3-4) through a pipeline, and the solid discharge port of the purification device (2-2) is connected with the solid feed port of the high-temperature desulfurization device (2-3) through a pipeline; the solid discharge port of the high-temperature desulfurization device (2-3) is connected with a cement clinker pipeline; the air outlet of the high-temperature desulfurization device (2-3) is connected with the air inlet of the sulfur dioxide heat exchanger (2-6) through a pipeline; a heat exchange jacket is arranged in the high-temperature desulfurization device (2-3), and a high-temperature medium inlet of the heat exchange jacket is connected with a high-temperature medium outlet of the solar furnace (2-5); the low-temperature medium outlet of the heat exchange jacket is connected with the low-temperature medium inlet of the solar furnace (2-5); the liquid inlet of the sulfuric acid heat exchanger (2-4) is connected with the liquid outlet of the anode of the electric reduction device (3-2); the air outlet of the sulfuric acid heat exchanger (2-4) is connected with a low-temperature air evacuation port; the solar furnace (2-5) is provided with a receiving window for receiving solar energy; an air inlet of the sulfur dioxide heat exchanger (2-6) is connected with an air main pipe; the high-temperature air outlet of the sulfur dioxide heat exchanger (2-6) is connected with the air inlet of the sulfuric acid heat exchanger (2-4), the air inlet (3-4) of the catholyte heat exchange device and the air inlet (3-5) of the anolyte heat exchange device through pipelines;
the cathode liquid inlet of the valence state control device (3-1) is connected with the liquid outlet of the cathode liquid heat exchange device (3-4); the anode liquid inlet of the valence state control device (3-1) is connected with the liquid outlet of the anode liquid heat exchange device (3-5); the anode liquid outlet of the valence state control device (3-1) is connected with the anode liquid inlet of the electric reduction device (3-2) and the liquid inlet of the anolyte heat exchange device (3-5) through a pipeline; the anode gas outlet of the valence state control device (3-1) is connected with an oxygen product pipeline; the cathode liquid outlet of the valence state control device (3-1) is connected with the cathode liquid inlet of the electric reduction device (3-2) through a pipeline; the anode of the valence state control device (3-1) is connected with the anode of the direct current green electricity through a conductive copper beam; the cathode of the valence state control device (3-1) is connected with the cathode of the direct current green electricity through a conductive copper beam; the cathode liquid inlet of the electro-reduction device (3-2) is connected with the ferrous sulfate solution discharge port of the membrane separation device (3-3) through a pipeline; the anode of the electric reduction device (3-2) is connected with the anode of the direct-current green electricity through a conductive copper beam; the cathode of the electric reduction device (3-2) is connected with the cathode of the direct-current green electricity through a conductive copper beam; the anode gas outlet of the electric reduction device (3-2) is connected with an oxygen product pipeline; the cathode liquid outlet of the electro-reduction device (3-2) is connected with the liquid inlet of the membrane separation device (3-3) through a pipeline; the cathode air outlet of the electric reduction device (3-2) is connected with the hydrogen outlet and the hydrogen product inlet of the electrolytic water hydrogen production device (1-2) through pipelines; the pure iron outlet of the electric reduction device (3-2) is designed to be open; the regenerated water outlet of the membrane separation device (3-3) is connected with the liquid inlet of the anolyte heat exchange device (3-5); the air outlet of the catholyte heat exchange device (3-4) is connected with a low-temperature air evacuation pipe; the air outlet of the anolyte heat exchange device (3-5) is connected with a low-temperature air evacuation pipe.
2. A method for producing iron by hydro-electro-reduction of iron ore based on the system of claim 1, comprising the steps of:
The iron concentrate is sent into the fluidized hydrogen reduction device (1-1) to undergo a reduction reaction with green hydrogen from the electrolytic water hydrogen production device (1-2) and the electric reduction device (3-2) to obtain low-valence iron oxide; delivering the low-valence iron oxide to the acidolysis filtering device (2-1); in the fluidized hydrogen reduction device (1-1), a solar furnace high-temperature medium is adopted to circularly provide reaction heat;
In the acidolysis filtering device (2-1), the low-valence iron oxide reacts with concentrated sulfuric acid from a liquid outlet of the sulfuric acid heat exchanger (2-4), sulfur dioxide from a gas outlet of the sulfur dioxide heat exchanger (2-6) and sulfuric acid in a sulfuric acid solution main pipe to obtain acidolysis slurry; the sulfuric acid solution is used for starting the system for the first time; filtering acidolysis slurry to obtain acidolysis slag and acidolysis solution; delivering acidolysis slag to a high-temperature desulfurization device (2-3) for treatment; delivering acidolysis solution to a purifying device (2-2) for treatment; in the high-temperature desulfurization device (2-3), acidolysis slag and purified slag from the purification device (2-2) are subjected to high-temperature desulfurization reaction in the presence of hydrogen to obtain sulfur dioxide gas and cement clinker; delivering and utilizing cement clinker; the solar furnace (2-5) converts solar energy into heat energy, a medium is preheated, and a high-temperature medium is circulated to provide reaction heat for the high-temperature desulfurization device (2-3); in the purifying device (2-2), the purified ferric sulfate solution is preheated by a catholyte heat exchange device (3-4) and then sent to the valence state control (3-1); the high-temperature sulfur dioxide discharged from the high-temperature desulfurization device (2-3) exchanges heat with air through the sulfur dioxide heat exchanger (2-6), and the cooled sulfur dioxide is sent to the acidolysis filtering device (2-1); the preheated high-temperature air enters a catholyte heat exchange device (3-4), an anolyte heat exchange device (3-5) and a sulfuric acid heat exchanger (2-4) respectively, and heat is provided for the preheated high-temperature air through heat exchange;
In the valence state control device (3-1), the cathode chamber ferric salt solution is electrically reduced into ferrous sulfate under the action of direct current; the valence state control device (3-1) separates out oxygen and generates sulfuric acid under the action of direct current in the anode chamber solution; an oxygen product delivery pipe; mixing 1% -20% of the sulfuric acid solution with the regenerated water generated by the membrane separation device (3-3), circulating to the anolyte heat exchange device (3-5), entering an anolyte inlet of the valence state control device (3-1), and delivering the rest sulfuric acid solution into an anode chamber of the electroreduction device (3-2); in the electroreduction device (3-2), ferrous sulfate solution from a cathode chamber of the valence control device (3-1) and the membrane separation device (3-3) is reduced into pure iron and byproducts of hydrogen and residual dilute ferrous sulfate solution under the action of direct current; hydrogen is sent to the fluidized hydrogen reduction device (1-1) and the high-temperature desulfurization device (2-3) for utilization or used as a hydrogen product; and delivering the dilute ferrous sulfate solution to the membrane separation device (3-3) for treatment.
3. The method for producing iron by hydrogen electro-reduction of iron ore according to claim 2, wherein the fluidized hydrogen reduction device (1-1) adopts a fluidized bed reactor, green hydrogen is a reducing agent, the reaction temperature is 300 ℃ to 800 ℃, and the residence time is: 10min-50min.
4. The method for producing iron by hydro-electric reduction of iron ore according to claim 2, wherein the iron concentrate is hematite and/or magnetite, and the iron oxide grade is not lower than 90%.
5. The method for producing iron by hydrogen electro-reduction of iron ore according to claim 2, wherein in the acidolysis filtering device (2-1), sulfuric acid solution is used for the first start-up of the system, the concentration of the concentrated sulfuric acid solution is not lower than 100g/L, and the acidolysis temperature is 50-100 ℃;
Ferric ions generated in the acidolysis process are reduced into ferrous ions under the action of sulfur dioxide, so that the reduction acidolysis is realized, the acidolysis efficiency is improved, and the acidolysis rate is more than 98%.
6. The method for producing iron by hydrogen electro-reduction of iron ore according to claim 2, wherein the high temperature desulfurization device (2-3) adopts a fluidized bed or rotary kiln reactor, the reaction temperature is 1000 ℃ to 1500 ℃, and the desulfurization rate is more than 99%.
7. The method for producing iron by hydrogen electro-reduction of iron ore according to claim 2, wherein in the valence control device (3-1), the diaphragm material is an ionic membrane or a porous membrane, wherein the porous membrane has a seepage rate of 1% -30%, a current density of 50A/m 2-1000A/m2, the anode is a lead alloy or titanium-based ruthenium iridium tantalum coated electrode, the cathode comprises one or more of iron, copper, titanium and stainless steel, and the reaction temperature is 20 ℃ -100 ℃.
8. The method for producing iron by hydrogen electro-reduction of iron ore according to claim 2, wherein in the electro-reduction device (3-2), the diaphragm is made of an ionic membrane or a porous membrane, wherein the porous membrane has a seepage rate of 1% -30%, a current density of 50A/m 2-2000A/m2, the anode is a lead alloy and/or titanium-based ruthenium iridium tantalum coated electrode, the cathode comprises one or more of iron, copper, titanium and stainless steel, and the reaction temperature is 60 ℃ -100 ℃.
9. The method for producing iron by hydro-electro-reduction of iron ore according to claim 2, characterized in that the membrane separation device (3-3) comprises one or several of reverse osmosis, ultrafiltration, nanofiltration and electrodialysis.
10. The method of low carbon electrometallurgical of iron ore according to claim 2, characterized in that the solar furnace (2-5) converts solar energy into heat energy, the solar heating medium being molten salt and/or gas, the molten salt comprising molten salt composed of one or several of the elements silicon, sodium, oxygen, calcium and aluminum, the gas comprising nitrogen and/or argon.
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