CN117385416A - Method for preparing electrodeposited nickel from high-nickel matte and electrodepositing device - Google Patents
Method for preparing electrodeposited nickel from high-nickel matte and electrodepositing device Download PDFInfo
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- CN117385416A CN117385416A CN202311316505.4A CN202311316505A CN117385416A CN 117385416 A CN117385416 A CN 117385416A CN 202311316505 A CN202311316505 A CN 202311316505A CN 117385416 A CN117385416 A CN 117385416A
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- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 132
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 51
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 41
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 41
- 238000002386 leaching Methods 0.000 claims abstract description 32
- 239000002994 raw material Substances 0.000 claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 230000008569 process Effects 0.000 claims abstract description 21
- 239000010949 copper Substances 0.000 claims abstract description 18
- 229910052802 copper Inorganic materials 0.000 claims abstract description 15
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000002002 slurry Substances 0.000 claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000001914 filtration Methods 0.000 claims abstract description 10
- 238000001035 drying Methods 0.000 claims abstract description 8
- 230000001590 oxidative effect Effects 0.000 claims abstract description 6
- 238000010298 pulverizing process Methods 0.000 claims abstract description 5
- WHBHBVVOGNECLV-OBQKJFGGSA-N 11-deoxycortisol Chemical compound O=C1CC[C@]2(C)[C@H]3CC[C@](C)([C@@](CC4)(O)C(=O)CO)[C@@H]4[C@@H]3CCC2=C1 WHBHBVVOGNECLV-OBQKJFGGSA-N 0.000 claims abstract description 4
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 4
- 238000004064 recycling Methods 0.000 claims abstract description 4
- 238000003756 stirring Methods 0.000 claims abstract description 4
- 238000002156 mixing Methods 0.000 claims abstract 10
- 239000000463 material Substances 0.000 claims abstract 2
- 239000007788 liquid Substances 0.000 claims description 176
- 239000007789 gas Substances 0.000 claims description 130
- 238000003411 electrode reaction Methods 0.000 claims description 124
- 239000001257 hydrogen Substances 0.000 claims description 38
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 37
- 239000004020 conductor Substances 0.000 claims description 27
- 239000002245 particle Substances 0.000 claims description 22
- 239000003792 electrolyte Substances 0.000 claims description 20
- 150000002500 ions Chemical class 0.000 claims description 20
- 238000004070 electrodeposition Methods 0.000 claims description 15
- 238000005868 electrolysis reaction Methods 0.000 claims description 13
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 230000005012 migration Effects 0.000 claims description 8
- 238000013508 migration Methods 0.000 claims description 8
- 230000009471 action Effects 0.000 claims description 7
- 239000011148 porous material Substances 0.000 claims description 7
- 230000005684 electric field Effects 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 239000002904 solvent Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- -1 hydrogen ions Chemical class 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims 1
- 239000007858 starting material Substances 0.000 claims 1
- 108091006146 Channels Proteins 0.000 description 82
- 238000003795 desorption Methods 0.000 description 24
- 239000012528 membrane Substances 0.000 description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 15
- 229910052760 oxygen Inorganic materials 0.000 description 15
- 239000001301 oxygen Substances 0.000 description 15
- 239000000446 fuel Substances 0.000 description 11
- 238000004519 manufacturing process Methods 0.000 description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 10
- 239000002253 acid Substances 0.000 description 10
- 238000006477 desulfuration reaction Methods 0.000 description 9
- 230000023556 desulfurization Effects 0.000 description 9
- 229910052751 metal Inorganic materials 0.000 description 9
- 239000002184 metal Substances 0.000 description 9
- 239000000460 chlorine Substances 0.000 description 8
- 238000001179 sorption measurement Methods 0.000 description 8
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 7
- 238000003487 electrochemical reaction Methods 0.000 description 7
- 238000005243 fluidization Methods 0.000 description 7
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 7
- 230000003647 oxidation Effects 0.000 description 7
- 238000007254 oxidation reaction Methods 0.000 description 7
- 230000027756 respiratory electron transport chain Effects 0.000 description 7
- 229920006395 saturated elastomer Polymers 0.000 description 7
- 238000000926 separation method Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 230000003009 desulfurizing effect Effects 0.000 description 5
- 238000004090 dissolution Methods 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- 238000001556 precipitation Methods 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 229910052801 chlorine Inorganic materials 0.000 description 4
- 230000005611 electricity Effects 0.000 description 4
- 239000012065 filter cake Substances 0.000 description 4
- 239000000706 filtrate Substances 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- 238000001223 reverse osmosis Methods 0.000 description 4
- 239000011343 solid material Substances 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 230000002776 aggregation Effects 0.000 description 3
- 238000004220 aggregation Methods 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- WWNBZGLDODTKEM-UHFFFAOYSA-N sulfanylidenenickel Chemical compound [Ni]=S WWNBZGLDODTKEM-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 108090000862 Ion Channels Proteins 0.000 description 2
- 102000004310 Ion Channels Human genes 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 239000012671 ceramic insulating material Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 229910000365 copper sulfate Inorganic materials 0.000 description 2
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 229910000765 intermetallic Inorganic materials 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 229910021586 Nickel(II) chloride Inorganic materials 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 230000002939 deleterious effect Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005518 electrochemistry Effects 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002105 nanoparticle Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 description 1
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 description 1
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007127 saponification reaction Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000011232 storage material Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/0423—Halogenated acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/08—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents with metals
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G53/00—Compounds of nickel
- C01G53/08—Halides
- C01G53/09—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
- C25B11/033—Liquid electrodes
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
- C25B15/083—Separating products
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
- C25B15/087—Recycling of electrolyte to electrochemical cell
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/30—Cells comprising movable electrodes, e.g. rotary electrodes; Assemblies of constructional parts thereof
- C25B9/305—Cells comprising movable electrodes, e.g. rotary electrodes; Assemblies of constructional parts thereof comprising vertical-type liquid electrode
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/60—Constructional parts of cells
- C25B9/63—Holders for electrodes; Positioning of the electrodes
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
- C25C1/06—Electrolytic production, recovery or refining of metals by electrolysis of solutions or iron group metals, refractory metals or manganese
- C25C1/08—Electrolytic production, recovery or refining of metals by electrolysis of solutions or iron group metals, refractory metals or manganese of nickel or cobalt
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
- C25C1/12—Electrolytic production, recovery or refining of metals by electrolysis of solutions of copper
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
- C25C7/007—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells of cells comprising at least a movable electrode
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
- C25C7/02—Electrodes; Connections thereof
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
- C25C7/06—Operating or servicing
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/02—Details
- H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
- H01M8/0258—Collectors; Separators, e.g. bipolar separators; Interconnectors characterised by the configuration of channels, e.g. by the flow field of the reactant or coolant
- H01M8/026—Collectors; Separators, e.g. bipolar separators; Interconnectors characterised by the configuration of channels, e.g. by the flow field of the reactant or coolant characterised by grooves, e.g. their pitch or depth
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/02—Details
- H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
- H01M8/0258—Collectors; Separators, e.g. bipolar separators; Interconnectors characterised by the configuration of channels, e.g. by the flow field of the reactant or coolant
- H01M8/0263—Collectors; Separators, e.g. bipolar separators; Interconnectors characterised by the configuration of channels, e.g. by the flow field of the reactant or coolant having meandering or serpentine paths
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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
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
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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
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
Abstract
The invention discloses a method for preparing electrodeposited nickel from high-nickel matte and an electrodepositing device. The method comprises the following steps: pulverizing high nickel matte, stirring with water to obtain slurry, and leaching the slurry with hydrochloric acid to obtain H-containing materials 2 S and H 2 Mixed gas of (2) leaching residue and NiCl 2 A solution; mixing the mixed gas with FeCl 3 Solution mixing reaction to make H in the mixed gas 2 S and FeCl 3 Reaction to produce FeCl 2 And elemental S from FeCl-containing 2 Filtering the solution to obtain simple substance S, and obtaining the FeCl-containing solution 2 FeCl in solution in (2) 2 Oxidizing to produce FeCl 3 The solution is reused for the mixing reaction, and the tail gas after the mixing reaction is further used for removing H 2 S, drying to obtain H 2 The method comprises the steps of carrying out a first treatment on the surface of the The leached residues are reduced by a flash furnace and refined by a converter according to an electrolytic copper process to prepare a copper plate for producing electrolytic copper, and the anode slime is used for recycling heavy metals; the NiCl is processed 2 The solution is used as a raw material to prepare electrodeposited nickel through an electrodepositing device.
Description
Technical Field
The embodiment of the disclosure relates to the technical field of electrochemistry, in particular to an electrode, an electrode assembly, an electrochemical reactor and an electrochemical reaction method. The embodiment of the disclosure also relates to a method for preparing electrodeposited nickel from the high-nickel matte and an electrodepositing device.
Background
An electrode for an electrochemical reaction refers to a site that provides electron transport for the electrode reaction (i.e., a reaction that loses or gains electrons occurring at the electrode), and in particular, the electrode is used to achieve the electron transport required for the electrode reaction. Currently, electrodes are made of solid materials and are fixedly installed inside an electrochemical reactor, so that undesirable problems occur when the electrode reaction requires gas participation or gas generation. For example, two electrodes (positive electrode and negative electrode respectively) in the hydrogen fuel cell adopt polar plates, oxygen and hydrogen are respectively sent into and adsorbed on the positive electrode polar plate and the negative electrode polar plate during operation, corresponding electrode reactions respectively occur on the positive electrode polar plate and the negative electrode polar plate, in the process, the surfaces of the positive electrode polar plate and the negative electrode polar plate are easily surrounded by a large number of bubbles, and the bubbles near the polar plates greatly increase the resistance between the polar plates and electrolyte due to poor gas conductivity, so that the resistance is increased, and the energy efficiency is reduced. For another example, two electrodes (respectively, an anode and a cathode) in the water electrolysis hydrogen production device are electrode plates, the anode electrode plate and the cathode electrode plate are respectively connected with the anode and the cathode of the power supply during working, corresponding electrode reactions are respectively generated on the anode electrode plate and the cathode electrode plate, oxygen (possibly other gases) can be generated on the anode electrode plate in the process, hydrogen can be generated on the cathode electrode plate, and if the oxygen and the hydrogen are required to be separately recovered, a diaphragm and a special air guide channel are usually arranged outside the anode electrode plate and the cathode electrode plate, so that the structure of the water electrolysis hydrogen production device is complicated, and the cost is increased.
Disclosure of Invention
Embodiments of the present disclosure provide an electrode, an electrode assembly, an electrochemical reactor, and an electrochemical reaction method, which solve the technical problem that the electrode is limited to be manufactured by a solid material.
In a first aspect, there is provided an electrode comprising: an electrode support having a pore structure permeable to an electrolyte; an electrode reaction channel formed by a separator provided in the electrode support body; the electrode input channel is arranged on the electrode support body and is communicated with the input end of the electrode reaction channel; the electrode output channel is arranged on the electrode support body and is communicated with the output end of the electrode reaction channel; an electrical external conductor arranged on the electrode support body and extending into the electrode reaction channel; in operation, the electrode input channel receives the electrode liquid before electrode reaction and guides the electrode liquid into the electrode reaction channel, the electrode output channel outputs the electrode liquid after electrode reaction from the electrode reaction channel, the electric external conductor is used for providing an electron migration external connection path required by electrode reaction for the electrode liquid in the electrode reaction channel, and the electrode liquid is used for forming a flowing electrode in the electrode reaction channel so as to realize electron migration required by the electrode reaction on the flowing electrode.
Optionally, the electrode reaction channel is a tubular diaphragm channel, and two ends of the tubular diaphragm channel are respectively an input end of the electrode reaction channel and an output end of the electrode reaction channel.
Alternatively, the cross-sectional shape of the tubular diaphragm passageway is circular, oval or rectangular.
Optionally, the length of the electrical external conductor extends along the axial direction of the tubular diaphragm channel.
Optionally, the electrical external conductor has a helical section located in the tubular diaphragm passage.
Optionally, the electrode support is a porous material, and the porous material is made of insulating plastic or ceramic insulating material.
Optionally, at least two electrode reaction channels are arranged in the electrode support body, the at least two electrode reaction channels are connected in parallel between the electrode input channel and the electrode output channel, and the electric external conductors in the at least two electrode reaction channels are used for being connected with the same pole of a power supply.
Optionally, the separator allows passage of a) ions and b) at least a) ions in the solvent in the electrode liquid, but does not allow passage of other components in the electrode liquid.
Optionally, the membrane adopts an ionic membrane or a reverse osmosis membrane for solution reverse osmosis treatment.
Alternatively, the electrode liquid can carry the raw gas required for the electrode reaction or the produced gas generated by the electrode reaction.
In a second aspect, there is provided an electrode assembly comprising: the electrode of the first aspect; and the electrode liquid circulation system is connected with the inlet of the electrode input channel and the outlet of the electrode output channel to form an electrode liquid circulation loop.
Optionally, the electrode liquid circulation system comprises: one end of the electrode liquid circulating pipeline is connected with the inlet of the electrode input channel, and the other end of the electrode liquid circulating pipeline is connected with the outlet of the electrode output channel; the circulating pump is arranged in the electrode liquid circulating pipeline in series; the regulating valve is arranged in the electrode liquid circulating pipeline in series; and the gas dissolving device is arranged in the electrode liquid circulating pipeline in series and is used for dissolving the raw material gas required by the electrode reaction in the electrode liquid.
Optionally, the gas dissolving device comprises: the gas dissolving bin is provided with a gas dissolving bin gas inlet end, a gas dissolving bin liquid inlet end and a gas dissolving bin liquid outlet end, the gas dissolving bin gas inlet end is connected with a compressed gas source, and the gas dissolving bin is connected in series in the electrode liquid circulating pipeline through the gas dissolving bin liquid inlet end and the gas dissolving bin liquid outlet end; and the electrode liquid cooler is arranged on the dissolved air bin and used for cooling the electrode liquid.
Optionally, the electrode liquid circulation system comprises: one end of the electrode liquid circulating pipeline is connected with the inlet of the electrode input channel, and the other end of the electrode liquid circulating pipeline is connected with the outlet of the electrode output channel; the circulating pump is arranged in the electrode liquid circulating pipeline in series; the regulating valve is arranged in the electrode liquid circulating pipeline in series; and the desorption device is arranged in the electrode liquid circulation pipeline in series and is used for desorbing the generated gas generated by the electrode reaction from the electrode liquid.
Optionally, the gas dissolving device comprises: the desorption bin is provided with a desorption bin exhaust end, a desorption bin liquid inlet end and a desorption bin liquid outlet end, the desorption bin exhaust end is connected with an air suction mechanism, and the desorption bin is connected in series in the electrode liquid circulation pipeline through the desorption bin liquid inlet end and the desorption bin liquid outlet end; and the electrode liquid heater is arranged on the desorption bin and used for heating the electrode liquid.
In a third aspect, there is provided an electrochemical reactor comprising: a main container; an electrolyte stored in the main container; a first electrode accommodated in the main container; a second electrode accommodated in the main container; the two poles of the power supply are respectively connected with the first electrode and the second electrode and are used for charging or supplying power; the first electrode and/or the second electrode adopts the electrode of the first aspect; alternatively, the first electrode and/or the second electrode employs the electrode assembly of the second aspect.
Optionally, the electrochemical reactor is a hydrogen fuel cell, the power supply is used for charging, oxygen is carried in the electrode liquid before the electrode reaction in the first electrode, and hydrogen is carried in the electrode liquid before the electrode reaction in the second electrode.
Optionally, the electrochemical reactor is a water electrolysis hydrogen production device, the power supply is used for supplying power, oxygen is carried in the electrode liquid after the electrode reaction in the first electrode, and hydrogen is carried in the electrode liquid after the electrode reaction in the second electrode.
In a fourth aspect, there is provided an electrochemical reaction method comprising: preparing electrode liquid; operating the electrochemical reactor of the third aspect; wherein the electrode liquid has at least the following characteristics: 1) The conductivity required for the electrode reaction is satisfied; 2) Can dissolve the raw gas required by the electrode reaction or the generated gas generated by the electrode reaction; 3) Contains conductive particles capable of adsorbing and dissolving the raw gas or the produced gas in the electrode liquid.
Optionally, the conductive particles are made of metal, intermetallic compound, metal oxide, ceramic, expanded graphite or conductive organic matter with adsorptivity.
Optionally, the particle size of the conductive particulate matter is 500 microns or less, 100 microns or less, or 50 microns or less.
The electrode, the electrode assembly, the electrochemical reactor and the electrochemical reaction method initially propose and apply the concept of a fluidized electrode. It should be noted that the electric external conductor serves to provide an external path for electron transfer required for the electrode reaction to the electrode liquid in the electrode reaction channel, and the electron transfer required for the electrode reaction occurs on the fluidization electrode, so that the fluidization electrode is a place for providing electron transfer for the electrode reaction, and the fluidization electrode is no longer a solid material. The electrode liquid can be set to be capable of carrying raw gas required by the electrode reaction or produced gas generated by the electrode reaction according to requirements, so that when the electrode reaction needs gas participation or needs gas generation, the fluidized electrode can avoid bubble aggregation on the surface of the solid electrode or can bring the produced gas of the electrode reaction out of the electrochemical reactor.
The disclosure is further described below with reference to the drawings and detailed description. Additional aspects and advantages of the disclosure will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice.
Drawings
The accompanying drawings, which form a part hereof, are included to provide an understanding of the disclosure, and are incorporated in and constitute a part of this specification.
Fig. 1 is a schematic structural view of an electrode according to an embodiment of the present disclosure.
Fig. 2 is a schematic structural view of an electrode assembly according to an embodiment of the present disclosure.
Fig. 3 is a schematic structural view of an electrode assembly according to an embodiment of the present disclosure.
Fig. 4 is a schematic view showing a structure of an electrochemical reactor according to an embodiment of the present disclosure.
Fig. 5 is a schematic view showing a structure of an electrochemical reactor according to an embodiment of the present disclosure.
Fig. 6 is a schematic view of an electrochemical reactor according to an embodiment of the present disclosure.
Fig. 7 is a process flow diagram of a method for preparing electrodeposited nickel from high nickel matte according to an embodiment of the present disclosure.
Marked in the figure as: electrode 1, electrode support 11, electrode reaction channel 12, membrane 121, electrode input channel 13, electrode output channel 14, electric external conductor 15, electrode liquid circulation pipe 21, circulation pump 22, regulating valve 23, gas dissolving device 24, gas dissolving tank 241, electrode liquid cooler 242, desorption device 25, desorption tank 251, electrode liquid heater 252, container 31, electrolyte 32, first electrode 33, second electrode 34, power supply 35, membrane 36.
Detailed Description
The present disclosure will now be described more fully hereinafter with reference to the accompanying drawings. Those of ordinary skill in the art will be able to implement the present disclosure based on these descriptions. Before explaining the present disclosure with reference to the drawings, it should be noted in particular that: an electrode, an electrode assembly, an electrochemical reactor and an electrochemical reaction method.
The technical solutions and technical features provided in the respective sections including the following description may be combined with each other without conflict. Furthermore, the described embodiments, features, and combinations of features can be combined as desired and claimed in any given application.
The embodiments of the present disclosure referred to in the following description are typically only a few, but not all, embodiments, based on which all other embodiments, as would be apparent to one of ordinary skill in the art without undue burden, are intended to be within the scope of patent protection.
With respect to terms and units in this specification: the terms "comprising," "including," "having," and any variations thereof, in this specification and the corresponding claims and related parts, are intended to cover a non-exclusive inclusion. Furthermore, other related terms and units may be reasonably construed based on the description provided herein.
Fig. 1 is a schematic structural view of an electrode according to an embodiment of the present disclosure. As shown in fig. 1, an electrode 1 includes: an electrode support 11, an electrode reaction channel 12, an electrode input channel 13, an electrode output channel 14 and an electrical external conductor 15.
Wherein the electrode support 11 has a pore structure permeable to the electrolyte so that the electrolyte can be in contact with a fluidized electrode described below.
Wherein the electrode reaction channel 12 is formed by a membrane 121 provided in the electrode support. Here, the separator 121 basically functions to constitute the electrode reaction channel 12, so that the fluidized electrode described below flows and performs an electrode reaction.
Wherein the electrode input channel 13 is provided on the electrode support and communicates with the input end of the electrode reaction channel 12.
Wherein an electrode output channel 14 is provided on the electrode support 11 and communicates with the output end of the electrode reaction channel 12.
Wherein an electrical external conductor 15 is arranged on the electrode support 11 and protrudes into the electrode reaction channel 12.
In operation, the electrode input channel 13 receives the electrode liquid before the electrode reaction and guides the electrode liquid into the electrode reaction channel 12, the electrode output channel 14 outputs the electrode liquid after the electrode reaction from the electrode reaction channel 12, the electric external conductor 15 is used for providing an external electron migration path (usually connected with one pole of a power supply) required by the electrode reaction for the electrode liquid in the electrode reaction channel 12, and the electrode liquid is used for forming a flowing electrode in the electrode reaction channel 12 so as to realize the electron migration required by the electrode reaction on the flowing electrode.
The electrode initiative described above proposes the concept of a "fluidising electrode". It should be noted that the electric external connection 15 is used to provide an external path for the electron transfer required for the electrode reaction to the electrode liquid in the electrode reaction channel 12, and the electron transfer required for the electrode reaction occurs on the fluidization electrode, so that the fluidization electrode is a place for providing the electron transfer for the electrode reaction, and the fluidization electrode is no longer a solid material.
Since the electrode liquid may form a fluidized electrode in the electrode reaction channel 12 so as to achieve electron transfer required for the electrode reaction on the fluidized electrode, the electrode liquid is necessarily conductive, and its specific composition may be configured according to the electrochemical reaction requirement.
In an alternative embodiment, the electrode liquid is capable of carrying a feed gas required for the electrode reaction or a product gas produced by the electrode reaction. Thus, when the electrode reaction needs gas to participate in or generate gas, the fluidized electrode can avoid bubble aggregation on the surface of the solid electrode or can bring the generated gas of the electrode reaction out of the electrochemical reactor.
Generally, the electrode liquid has at least the following characteristics: 1) The conductivity required for the electrode reaction is satisfied; 2) Can dissolve the raw gas required by the electrode reaction or the generated gas generated by the electrode reaction; 3) Contains conductive particles capable of adsorbing and dissolving the raw gas or the produced gas in the electrode liquid.
The conductive particles are disposed in the electrode liquid to improve the capability of the electrode liquid to carry the raw material gas. The conductive particles can be made of metal, intermetallic compound, metal oxide, ceramic, expanded graphite or conductive organic matter with adsorptivity. The conductive particles may have a particle size of 500 microns or less, 100 microns or less, or 50 microns or less. The particle size of the conductive particles may also be nano-sized,
in general, the electrode support 11 may be a porous material, which may be made of an insulating plastic or ceramic insulating material.
In general, the membrane 121 should allow passage of a) ions and b) at least a) ions in the solvent in the electrode liquid, but not other components in the electrode liquid. Thus, the membrane 121 may employ an ion membrane (allowing ions to pass through) or a reverse osmosis membrane for solution reverse osmosis treatment (i.e., allowing ions to pass through and allowing a solvent such as water in an electrode solution to pass through).
In an alternative embodiment, the electrode reaction channel 12 is a tubular membrane channel (as shown in fig. 1), and two ends of the tubular membrane channel are respectively an input end of the electrode reaction channel 12 and an output end of the electrode reaction channel. The cross-sectional shape of the tubular diaphragm passageway may be circular, oval, rectangular, or the like.
When the electrode reaction channels 12 are tubular diaphragm channels, at least two electrode reaction channels 12 may be disposed in the electrode support 11, the at least two electrode reaction channels 12 are connected in parallel between the electrode input channel 13 and the electrode output channel 14, and the electrical external conductors 15 in the at least two electrode reaction channels 12 are used for connecting with the same pole of the power supply. Thus, the contact area between the fluidized electrode and the electrolyte can be increased, and the electrode reaction efficiency can be improved.
When the electrode reaction channel 12 is a tubular diaphragm channel, the length of the electrical external conductor 15 may extend along the axial direction of the tubular diaphragm channel. Preferably, the electrical external conductor 15 may be configured to have a spiral section located in the tubular separator channel, for example, copper or other metal may be processed into a strip shape and further processed into a spiral shape, thereby forming the spiral section, and thus, when the electrode liquid flows axially in the tubular separator channel, the spiral section plays a role in stirring the electrode liquid, so that conductive particles are dispersed more uniformly, and thus, electrode reaction can be facilitated.
Fig. 2 is a schematic structural view of an electrode assembly according to an embodiment of the present disclosure. As shown in fig. 2, an electrode assembly includes: the electrode 1; and an electrode liquid circulation system connected with the inlet of the electrode input channel 13 and the outlet of the electrode output channel 14 to form an electrode liquid circulation loop.
Specifically, the electrode liquid circulation system includes: an electrode liquid circulation pipe 21 having one end connected to the inlet of the electrode input channel 13 and the other end connected to the outlet of the electrode output channel 14; a circulation pump 22 disposed in series in the electrode liquid circulation pipe 21; a regulating valve 23 disposed in series in the electrode liquid circulation pipe 21; and a gas dissolving device 24, which is arranged in the electrode liquid circulation pipeline in series, and is used for dissolving the raw material gas required by the electrode reaction in the electrode liquid.
In an alternative embodiment, the gas dissolving device 24 includes: the gas dissolving bin 241 is provided with a gas dissolving bin gas inlet end, a gas dissolving bin liquid inlet end and a gas dissolving bin liquid outlet end, the gas dissolving bin 241 gas inlet end is connected with a compressed gas source, and the gas dissolving bin is connected in series in the electrode liquid circulating pipeline 21 through the gas dissolving bin liquid inlet end and the gas dissolving bin liquid outlet end; an electrode liquid cooler 242 provided in the dissolved air chamber 241 for cooling the electrode liquid. The electrode liquid cooler 242 is typically a partition wall cooler.
The above-described electrode assembly may be referred to as a gas-consuming electrode assembly. In this embodiment, the operation principle of the gas-consuming electrode assembly is as follows.
The raw material gas is pressurized by a compressor and enters a gas dissolving bin 241, and is dissolved into the electrode liquid under the action of pressure, wherein one part of gas and conductive particles in the electrode liquid form adsorption, the other part of gas is dissolved in the electrode liquid in a molecular form, heat generated in the dissolving and adsorbing processes is taken away by an electrode liquid cooler 242, and the electrode liquid adsorbs and dissolves the raw material gas and flows out of the gas dissolving bin 241 after being nearly saturated, and is decompressed and enters the electrode 1 through a regulating valve 23.
In the electrode 1, the electrode liquid forms a fluidized electrode in the electrode reaction channel 12, and since the fluidized electrode is in contact with the electrical external conductor 15, charge transfer occurs in the fluidized electrode, and the raw gas adsorbed in the fluidized electrode becomes ions.
Specifically, when the raw material gas is a reducing gas and the electric external conductor 15 is connected to the positive electrode of the power source, the adsorbed raw material gas loses electrons and becomes cations, for example:
H 2 -2e - →2H +
when the raw material gas is an oxidizing gas and the electric external conductor 15 is connected to the negative electrode of the power supply, the adsorbed raw material gas gets electrons to become anions, for example:
2H 2 O+O 2 +4e - →4OH -
or Cl 2 +2e - →2Cl - 。
After the raw material gas is reacted into ions through the electrodes, the ions pass through the membrane 121 and the electrode support 11 to enter the electrolyte under the action of an electric field (the electric field is generated in an electrochemical reactor adopting a gas consumption electrode assembly), the conductive particles which are originally adsorbed with the raw material gas and saturated are not saturated, gas molecules dissolved in the electrode liquid are adsorbed to the conductive particles again to continue the reaction, the fluidized electrodes always flow to the electrode output channel 14 in the whole reaction process, the content of the raw material gas carried in the electrode liquid is gradually reduced, and finally the electrode liquid with poor content of the raw material gas returns to the dissolved gas bin 241 through the circulating pump 22 to absorb the raw material gas again.
Fig. 3 is a schematic structural view of an electrode assembly according to an embodiment of the present disclosure. As shown in fig. 3, an electrode assembly includes: the electrode 1; and an electrode liquid circulation system connected with the inlet of the electrode input channel 13 and the outlet of the electrode output channel 14 to form an electrode liquid circulation loop.
Specifically, the electrode liquid circulation system includes: an electrode liquid circulation pipe 21 having one end connected to the inlet of the electrode input channel 13 and the other end connected to the outlet of the electrode output channel 14; a circulation pump 22 disposed in series in the electrode liquid circulation pipe 21; a regulating valve 23 disposed in series in the electrode liquid circulation pipe 21; and a desorption device 25, which is arranged in series in the electrode liquid circulation pipeline 21, and is used for desorbing the generated gas generated by the electrode reaction from the electrode liquid.
In an alternative embodiment, the gas dissolving device 25 includes: the desorption bin 251 is provided with a desorption bin exhaust end, a desorption bin liquid inlet end and a desorption bin liquid outlet end, the desorption bin exhaust end is connected with an air extraction mechanism, and the desorption bin 251 is connected in series in the electrode liquid circulation pipeline 21 through the desorption bin liquid inlet end and the desorption bin liquid outlet end; an electrode liquid heater 252 is provided in the desorption chamber 251 to heat the electrode liquid. The electrode liquid heater 252 is typically a partition wall heater.
The above-described electrode assembly may be referred to as a gas-generating type electrode assembly. In this embodiment, the working principle of the gas-generating type electrode assembly is as follows.
Ions in the electrolyte migrate toward the fluidizing electrode under the action of an electric field generated in the electrochemical reactor employing the gas-consuming electrode assembly, pass through the electrode support 11 and the membrane 121, and then contact the fluidizing electrode, and as the fluidizing electrode is in contact with the electrical external conductor 15, charge transfer occurs in the fluidizing electrode, and charge is obtained or lost and an electrode reaction occurs to generate a simple substance and adsorb the simple substance on the surface of conductive particles of the fluidizing electrode.
Specifically, when the electrical external conductor 15 is connected to the negative electrode of the power source, the ions get electrons, for example:
2H + +2E - →H 2 ↑
when the electrical external conductor 15 is connected to the positive electrode of the power supply, the ions lose electrons, for example:
4OH - -2e - →2H 2 O+O 2 ↑
or Cl - -2e - →Cl 2 ↑。
As the electrode reaction proceeds, the adsorbed gas is saturated, the adsorbed gas is separated from the surface of the conductive particles and dissolved into the electrode liquid, the electrode liquid with dissolved gas flows out from the electrode output channel, is depressurized by the regulating valve 23 and enters the desorption bin 251, after the gas escapes from the depressurized electrode liquid, the heat absorbed by the desorption and the gas is supplemented by the electrode liquid heater 252, the generated gas is pumped away by the air pump, and the electrode liquid returns to the electrode through the circulating pump 22 to continue working.
In operation, the electrode and electrode assembly described above will be part of an electrochemical reactor. The electrochemical reactor is described below.
As shown in fig. 4 to 5, the present disclosure provides an electrochemical reactor including: a container 31 (for containing an electrolyte and first and second electrodes described below); an electrolyte 32 stored in the main container; a first electrode 33 accommodated in the main container; a second electrode 34 accommodated in the main container; a power supply 35, two poles of which are respectively connected with the first electrode and the second electrode and are used for charging or supplying power; the first electrode 33 and/or the second electrode 34 may be the above-described electrode or the above-described electrode assembly. The above-described electrochemical reactors will be further described below by way of a plurality of examples, respectively.
Fig. 4 is a schematic view showing a structure of an electrochemical reactor according to an embodiment of the present disclosure. As shown in fig. 4, an electrochemical reactor (here, specifically, a hydrogen fuel cell) includes: a main container 31; an electrolyte 32 stored in the main container; a first electrode 33 accommodated in the main container, the first electrode 33 employing the above-described gas-consuming electrode assembly, the raw material gas of the gas-consuming electrode assembly being oxygen; a second electrode 34 accommodated in the main container, the second electrode 34 also employing the above-described gas-consuming electrode assembly, the raw material gas of the gas-consuming electrode assembly being hydrogen gas; a power source 35, two poles of which are respectively connected to the first electrode 33 and the second electrode 34, for charging.
The working principle of the hydrogen fuel cell is as follows:
in the first electrode 33, oxygen is pressurized by a compressor and enters a gas dissolving bin 241, and is dissolved into electrode liquid under the action of pressure, wherein a part of oxygen and conductive particles in the electrode liquid form adsorption, and the other part of oxygen is dissolved in the electrode liquid in a molecular form, heat generated in the dissolving and adsorbing processes is taken away by an electrode liquid cooler 242, and the electrode liquid adsorbs and dissolves oxygen to flow out of the gas dissolving bin 241 after being nearly saturated, and is decompressed by a regulating valve 23 and enters an electrode reaction channel of the first electrode 33.
In the second electrode 34, hydrogen is pressurized by a compressor and enters a gas dissolving bin 241, and is dissolved into electrode liquid under the action of pressure, wherein a part of hydrogen and conductive particles in the electrode liquid form adsorption, and the other part of hydrogen is dissolved in the electrode liquid in a molecular form, heat generated in the dissolving and adsorbing processes is taken away by an electrode liquid cooler 242, and the electrode liquid adsorbs and dissolves oxygen and flows out of the gas dissolving bin 241 after being nearly saturated, and is decompressed by a regulating valve 23 and enters an electrode reaction channel of the second electrode 34.
In the electrode reaction channel of the second electrode 34, the hydrogen is oxidized into ions and electrons, the ions are transferred to the first electrode 33 through the electrolyte, and the electrons are transferred to the power supply through the electric external conductor 15 of the second electrode 34 to form electric current. In the electrode reaction channel of the first electrode 33, oxygen is reduced to water.
The conductive particles contained in the electrode liquid of the first electrode 33 may also serve as a catalyst for the reaction of the corresponding electrode (such as metal platinum in the present year), and the conductive particles contained in the electrode liquid of the second electrode 34 may also serve as a catalyst for the reaction of the corresponding electrode (such as metal iron, metal nickel, and metal platinum). Thus, the conductive particles play a role in adsorbing the raw material gas and also play a role in the catalyst.
The hydrogen fuel cell has no problem of increasing resistance between the motor and the electrolyte due to bubble aggregation on the surface of the solid electrode because the fluidized electrode is adopted.
Fig. 5 is a schematic view showing a structure of an electrochemical reactor according to an embodiment of the present disclosure. As shown in fig. 5, an electrochemical reactor (specifically, a water electrolysis hydrogen production apparatus herein) includes: a main container 31; an electrolyte 32 stored in the main container; a first electrode 33 accommodated in the main container, wherein the first electrode 33 employs the gas-generating electrode assembly, and the gas generated by the gas-generating electrode assembly is oxygen (or other gases); a second electrode 34 accommodated in the main container, the second electrode 34 also employing the above-described gas-generating electrode assembly, the gas-generating electrode assembly generating hydrogen gas; a power source 35, two poles of which are respectively connected to the first electrode 33 and the second electrode 34, for supplying power.
The water electrolysis hydrogen production device can carry produced gas through the fluidized electrode, and can separate and recycle the produced gas of the first electrode 33 and the produced gas of the second electrode 34.
Fig. 6 is a schematic view of an electrochemical reactor according to an embodiment of the present disclosure. As shown in fig. 6, an electrochemical reactor (herein, specifically, an electrodeposition device) includes: a main container 31 (in particular an electrolyzer); an electrolyte 32 stored in the main container; a first electrode 33 accommodated in the main container, the first electrode 33 employing the above-described gas-consuming electrode assembly, the raw material gas of the gas-consuming electrode assembly being hydrogen gas; a second electrode 34 housed in said main container, the second electrode 34 being a solid electrode (in particular a nickel plate) for depositing a target product (in particular electrodeposited nickel); a power source 35, two poles of which are respectively connected to the first electrode 33 and the second electrode 34, for supplying power.
The electro-deposition device is applied to a method for preparing electro-deposited nickel from high-nickel matte. The operation principle of the above-described electro-deposition apparatus will be described below with reference to the method for producing electro-deposited nickel from the high nickel matte.
In the existing process of preparing electrodeposited nickel by high nickel matte, the energy consumption has the largest proportion in the operation cost, mainly takes electric energy as a main component, has large power and poor peak regulation capability, is seriously influenced by the load of a power supply system, and is unfavorable for using new energy sources with low cost, such as wind energy, photovoltaic and the like, but the power supply capability has obvious time period. In addition, conventional sulfuric acid oxidative leach systems produce large amounts of spent acid, require the consumption of alkali to neutralize, and may produce deleterious salts containing heavy metal ions. The embodiment provides a method for preparing electrodeposited nickel by Gao Nieliu, which reduces the consumption of electric energy from a plurality of layers such as leaching, electrolysis and anolyte treatment modes, and organically combines the produced hydrogen with the used hydrogen in the production process, so that the electrodeposited nickel process has certain peak-shifting production capacity and is beneficial to using new energy.
Fig. 7 is a process flow diagram of a method for preparing electrodeposited nickel from high nickel matte according to an embodiment of the present disclosure. Referring to fig. 7, the process architecture of the method for preparing electrodeposited nickel from high nickel matte is as follows:
the classifying and pulverizing device (ball mill, raymond mill or jet mill) is provided with a high nickel matte inlet, a powder outlet and a water supplementing port, the slurry outlet of the classifying and pulverizing device is connected to a precipitation and filtration system, the filter cake outlet of the precipitation and filtration system is connected to a hydrochloric acid leaching tank, and the filtrate port of the precipitation and filtration system is connected back to the classifying and pulverizing device. The classifying and crushing device is used for crushing and classifying the high-nickel matte, and the precipitation and filtration system is used for carrying out precipitation and filtration on slurry output by the classifying and crushing device to obtain filtrate and a filter cake. The filtrate is returned to the classifying and crushing device, and the filter cake is used for subsequent treatment.
The hydrochloric acid leaching tank is closed, a gas collecting port above the hydrochloric acid leaching tank is connected to a gas inlet at the bottom of the ferric chloride desulfurization tower, and a clear liquid outlet of the hydrochloric acid leaching tank is connected to crude NiCl 2 The slag discharging port at the bottom of the hydrochloric acid leaching tank is connected to the filtering and drying device. The hydrochloric acid leaching tank is used for carrying out hydrochloric acid inlet and outlet on the filter cake.
The bottom desulfurization liquid circulation port of the ferric chloride desulfurization tower is connected to the circulation inlet of the air oxidation tank, the slag discharge port of the bottom of the ferric chloride desulfurization tower is connected to a filter (a plate-and-frame filter press or a belt filter press or a vacuum filter), the filtrate outlet of the filter is connected to the oxidation desulfurization tower, and the circulation outlet of the air oxidation tank is connected to the spray port of the top of the ferric chloride desulfurization tower.
The air inlet of the air oxidation tank is connected with a blower (Roots blower, a turbine or a vortex blower), the gas outlet at the top of the ferric chloride desulfurization tower is connected with the inlet of a copper sulfate desulfurization device, the outlet of the copper sulfate desulfurization device is connected with the inlet of an alkaline drying device, the outlet of the alkaline drying device is connected with a dissolved air chamber of a fluidization electrode, the slurry outlet of the dissolved air chamber is connected with the slurry inlet of a fluidized anode of the electrolytic tank, the slurry outlet of the fluidized anode of the electrolytic tank is connected back to a slurry return port of the dissolved air chamber, an exhaust pipe of the dissolved air chamber is connected with a pressure swing adsorption separation device, the H2 outlet of the pressure swing adsorption separation device is connected back to the dissolved air chamber, and the N2 outlet of the pressure swing adsorption separation device is communicated with the atmosphere;
crude NiCl 2 The storage tank is connected to a purification and impurity removal device, which is connected to the above-mentioned electrodeposition device (the main vessel 31 of the electrodeposition device is provided with a diaphragm 36 dividing the main vessel 31 into a cathode chamber accommodating the first electrode 33 and an anode chamber accommodating the second electrode 34), an anolyte outlet of the electrodeposition device is connected to a rectification dehydrohcl column, a deacidification anolyte outlet at the bottom of the rectification dehydrohcl column is connected to a deacidification anolyte inlet of the cathode chamber of the electrodeposition device, a vapor outlet at the top of the rectification deacidification column is connected to a condenser, and a hydrochloric acid outlet of the condenser is connected back to the hydrochloric acid leaching tank.
It should be noted that the electro-deposition device is provided with a membrane 36, which is an existing structure of the electro-deposition device (the membrane 36 mainly serves to avoid that suspended matter generated in the anode chamber during electrolysis enters the cathode chamber), so that the electro-deposition device is not described above, and the membrane 36 is mainly provided for distinguishing the cathode chamber from the anode chamber of the electro-deposition device. Similarly, in other embodiments of the present disclosure, such as the aforementioned hydrogen fuel cell, a proton exchange membrane may be provided in the hydrogen fuel cell, as required, and the proton exchange membrane is an existing structure of the hydrogen fuel cell, and therefore is not described in the aforementioned hydrogen fuel cell. The proton exchange membrane is not necessary in the aforementioned hydrogen fuel cell because of the presence of the membrane 121.
The leaching residue outlet of the hydrochloric acid leaching tank is connected to a filtering and drying device, the filtering and drying device is connected to a powder inlet of the flash furnace, the flash furnace copper liquid is cooled and then is sent to a crude copper inlet of the converter, and a copper liquid outlet of the refined copper of the converter is cooled and plated and then is arranged on an anode of the electrolytic cell.
The process of the Gao Nieliu method for preparing electrodeposited nickel can be described as:
after the high nickel matte is crushed and classified to be fine enough, water is used for stirring to form slurry (the high nickel matte can be directly ground into slurry by water immersion, the slurry reacts with nearly saturated hydrochloric acid in a hydrochloric acid leaching tank at the temperature of 60-70 ℃ as follows:
Ni+2HCl→NiCl 2 +H 2 ↑
Ni 3 S 2 +6HCl→3NiCl 2 +2H 2 S↑+H 2 ↑
The mixed gas (H) 2 S、H 2 Etc.) Fe in an iron chloride desulfurizing tower and in an acidic desulfurizing liquid 3+ Reaction and H removal 2 S to avoid it affecting subsequent H 2 The generated simple substance S is separated by a filter to be used as an industrial raw material:
H 2 S+FeCl 3 →FeCl 2 +HCl+S↓
containing FeCl after the reaction 2 Is oxidized by air in an air oxidation tank to regenerate FeCl 3 Oxidizing the formed FeCl 3 And returning the solution to the ferric chloride desulfurizing tower along with the solution:
2FeCl 2 +2HCl+1/2O 2 →2FeCl 3 +H 2 O
after passing through the ferric chloride desulfurizing tower, most of H 2 S has been removed and passed through CuSO 4 The desulfurizing tower further removes H 2 S, drying to obtain H 2 With a small amount of N 2 Is a mixed gas of (a) and (b).
The leaching residue of the hydrochloric acid leaching tank mainly comprises undissolved Cu and precious metal precipitate, and is reduced by a flash furnace and refined by a converter according to the traditional electrolytic copper process to prepare a copper plate for producing electrolytic copper, and the anode slime is used for recycling heavy metals.
NiCl leached by hydrochloric acid leaching tank 2 The solution was collected into crude NiCl 2 Purifying and removing impurities in the storage tank to obtain near-saturated NiCl 2 Purifying liquid.
NiCl 2 Adding the purifying liquid into the electro-depositionThe cathode chamber of the device keeps the liquid level of the cathode chamber slightly higher than that of the anode chamber to carry out electrolysis, and H is dissolved in the fluidized electrode at the first electrode during the electrolysis 2 The following reactions occur:
H 2 －2e － →2H +
generated H + Into the anolyte.
At the second electrode, ni 2+ The electrons are changed into Ni to be deposited on the nickel polar plate to form an electrodeposited nickel product:
Ni 2+ +2e － →Ni↓
part of the cathode chamber Cl － Migrate to the anode chamber under the action of an electric field and react with H in the anode chamber + Combined into hydrochloric acid.
Delivering the anode liquid in the anode chamber to a rectifying deacidification tower according to a certain proportion, rectifying to obtain H 2 O and HCl are condensed into hydrochloric acid at the top of the tower and sent to an acid salt leaching tank as raw materials, and the bottom of the tower contains less HCl and NiCl 2 The deacidified anolyte with increased concentration is sent back to the cathode chamber for continuous electrolysis.
The method for preparing electrodeposited nickel by Gao Nieliu has the technical advantages that:
1) S is not oxidized in the reduction leaching process, H 2 The existence of S inhibits Cu dissolution, so that the reaction has higher selectivity, the Ni dissolution rate is higher than 98%, and the Cu dissolution rate is only about 2%, compared with the process of simultaneously leaching Cu and Ni by oxygen pressure leaching, nitric acid leaching, chlorine leaching and the like, the difficulty of subsequent extraction and separation is reduced, and the consumption of extractant and acid and alkali consumption during saponification and back extraction of the extractant are saved.
2) Oxidizing leaching processes such as oxygen pressure leaching, nitric acid leaching, chlorine leaching and the like directly oxidize simple Ni metal, 2-valent S element and the like into Ni 2+ And SO4 2+ The chemical energy converted from low valence state to high valence state is released in the form of heat energy and is underutilized, and the scheme adopts the reduction leaching, namely, metal Ni and Ni 3 S 2 Transferring part of electrons to H during dissolution + On generation of H 2 Part of chemical energy is recovered, S 2－ Oxidized to elemental S rather than SO 4 2－ Simple substance S can be used as raw material for producing nickel matte by using a vulcanizing furnace, so that the subsequent production neutralization H is reduced 2 SO 4 The amount of alkali required for the spent acid.
3) Compared with an insoluble anode electrolytic method, the electrolytic tank adopts the hydrogen electrode, hydrogen in an adsorption state is converted into hydrogen ions in an electrolytic process to be directly dissolved in anode liquid, gas is not generated by the anode, anode current is not uniform due to the fact that the anode plate is shielded by bubbles, and extra energy consumption is not generated due to the fact that floating bubbles exist in the solution and resistance is increased.
4) Compared with insoluble anodic electrolytic method, H atom in adsorption state is oriented to H + The overvoltage required for conversion is higher than that of OH － To O 2 The overvoltage of the conversion is lower, and the electrochemical efficiency is higher.
5) Compared with a nickel sulfide anode, the fluidized hydrogen anode cannot dissolve, and the increase of resistance caused by the change of the polar distance due to the change of the thickness of the anode plate is avoided.
5) Compared with a nickel sulfide anode, the anode solution has the advantages that impurities are not introduced due to anode dissolution, the purity of the anode solution is stable, the impurity content is low, and the quality of the produced electrodeposited nickel is improved.
6) Compared with a nickel sulfide anode, the anode does not introduce impurities, so that the anode liquid treatment difficulty is low, the recycling rate is high, and the equipment cost and the operation cost of the anode liquid treatment are reduced.
7) Compared with a nickel sulfate system, the nickel chloride has higher solubility, higher ion concentration of the catholyte and the anolyte, lower resistivity and higher energy efficiency.
8) SO when the pH is reduced in sulfuric acid system 4 2－ Hydrolysis consumes conductive ions in the solution, so that the conductivity of the solution is reduced, and the resistance is increased: SO (SO) 4 2－ +H + →HSO 4 － 。
In the chloride system, because HCl is monobasic strong acid, higher ionization degree can be maintained when the pH value is reduced, and the conductivity and stability of the solution are better than those of a sulfuric acid system.
9) In the scheme, the hydrogen electrode of the anode is isolated from the anolyte through the proton membrane and is not in direct contact with chloride ions, so that the separation of chlorine at the anode is avoided and the problems of energy loss and pollution caused by chlorine separation are solved compared with the process of directly contacting the anolyte with the polar plate.
10 Compared with the oxidation leaching process, the S element is recovered in the form of simple substance, the acid circulation is completely balanced theoretically, no extra alkali is needed to neutralize the waste acid, and in the oxidation leaching process, the over-S element is oxidized into SO 4 2- Excess sulfuric acid is generated in the anolyte after electrolysis, and is not consumed even if the anolyte is recycled to a leaching tank, and the excess acid in the anolyte is mixed with nickel, so that the sulfuric acid is high-boiling-point acid and is not easy to separate by a rectification method, and the cost for recovering the acid is high.
11 The hydrogen electrode is used as the anode, so that the reaction at the anode is equivalent to the reaction of a hydrogen fuel cell, partial electric energy is replaced by chemical energy, and hydrogen can be produced by wind power, electric voltage and other low-cost energy sources, thereby improving the energy structure of the production process of electrodeposited nickel, reducing the energy cost, realizing a certain energy peak regulation function by taking hydrogen as an energy storage material, staggering the high electricity price of the electricity consumption peak period, reducing the electricity consumption when limiting electricity and maintaining the production.
The above description has been made regarding the content of the present disclosure. Those of ordinary skill in the art will be able to implement the present disclosure based on these descriptions. Based on the foregoing specification, all other embodiments that may be obtained by one of ordinary skill in the art without making any inventive effort are intended to be within the scope of patent protection.
Claims (10)
1. A method for preparing electrodeposited nickel from high nickel matte is characterized by comprising the following steps: comprising the following steps:
pulverizing high nickel matte, stirring with water to obtain slurry, and leaching the slurry with hydrochloric acid to obtain H-containing materials 2 S and H 2 Mixed gas of (2) leaching residue and NiCl 2 A solution;
mixing the mixed gas with FeCl 3 Solution mixing reaction to make H in the mixed gas 2 S and FeCl 3 Reaction to produce FeCl 2 And elemental S from FeCl-containing 2 Filtering the solution to obtain simple substance S, and obtaining the FeCl-containing solution 2 FeCl in solution in (2) 2 Oxidizing to produce FeCl 3 The solution is reused for the mixing reaction, and the tail gas after the mixing reaction is further used for removing H 2 S, drying to obtain H 2 ；
The leached residues are reduced by a flash furnace and refined by a converter according to an electrolytic copper process to prepare a copper plate for producing electrolytic copper, and the anode slime is used for recycling heavy metals;
the NiCl is processed 2 The solution is used as a raw material to prepare electrodeposited nickel through an electrodepositing device.
2. A method for preparing electrodeposited nickel from high nickel matte according to claim 1, wherein: h is further removed from the tail gas after the mixed reaction 2 S comprises: mixing the tail gas after the mixing reaction with CuSO 4 The solution is mixed and reacted.
3. A method for preparing electrodeposited nickel from high nickel matte according to claim 1, wherein:
the electrodeposition device includes: a main container; an electrolyte stored in the main container; a first electrode accommodated in the main container, the first electrode adopting a gas-consuming electrode assembly, the raw gas of the gas-consuming electrode assembly being hydrogen; a second electrode accommodated in the main container, the second electrode being a nickel plate; the two poles of the power supply are respectively connected with the first electrode and the second electrode and are used for supplying power; a separator disposed between the first electrode and the second electrode, dividing the main container into a cathode chamber accommodating the first electrode and an anode chamber accommodating the second electrode;
Wherein the gas-consuming electrode assembly comprises an electrode and an electrode liquid circulation system;
wherein the electrode comprises: an electrode support having a pore structure permeable to an electrolyte; an electrode reaction channel formed by a separator provided in the electrode support body; the electrode input channel is arranged on the electrode support body and is communicated with the input end of the electrode reaction channel; the electrode output channel is arranged on the electrode support body and is communicated with the output end of the electrode reaction channel; an electrical external conductor arranged on the electrode support body and extending into the electrode reaction channel; in operation, the electrode input channel receives electrode liquid before electrode reaction and guides the electrode liquid into the electrode reaction channel, the electrode output channel outputs electrode liquid after electrode reaction from the electrode reaction channel, the electric external conductor is used for providing an electron migration external connection path required by electrode reaction for the electrode liquid in the electrode reaction channel, and the electrode liquid is used for forming a flowing electrode in the electrode reaction channel so as to realize electron migration required by the electrode reaction on the flowing electrode;
wherein, the electrode liquid circulation system includes: one end of the electrode liquid circulating pipeline is connected with the inlet of the electrode input channel, and the other end of the electrode liquid circulating pipeline is connected with the outlet of the electrode output channel; the circulating pump is arranged in the electrode liquid circulating pipeline in series; the regulating valve is arranged in the electrode liquid circulating pipeline in series; the gas dissolving device is arranged in the electrode liquid circulating pipeline in series and is used for dissolving the raw material gas required by the electrode reaction in the electrode liquid;
The NiCl is processed 2 The preparation of electrodeposited nickel from a solution as a starting material by an electrodeposition apparatus comprises: niCl is added 2 The solution is added into a cathode chamber of the electro-deposition device, the liquid level of the cathode chamber is kept slightly higher than that of an anode chamber to carry out electrolysis, and the first electrode is dissolved in H in the fluidized electrode during the electrolysis 2 The lost electrons are converted into hydrogen ions, the hydrogen ions enter into the anode liquid, and Ni in the second electrode 2+ The electrons are changed into Ni to deposit on the nickel polar plate to form electrodeposited nickel product, and part of Cl in the cathode chamber － Migrate to the anode chamber under the action of an electric field and react with H in the anode chamber + Combined into hydrochloric acid.
4. A method for preparing electrodeposited nickel from high nickel matte according to claim 3, wherein: the gas dissolving device comprises: the gas dissolving bin is provided with a gas dissolving bin gas inlet end, a gas dissolving bin liquid inlet end and a gas dissolving bin liquid outlet end, the gas dissolving bin gas inlet end is connected with a compressed gas source, and the gas dissolving bin is connected in series in the electrode liquid circulating pipeline through the gas dissolving bin liquid inlet end and the gas dissolving bin liquid outlet end; and the electrode liquid cooler is arranged on the dissolved air bin and used for cooling the electrode liquid.
5. A method for preparing electrodeposited nickel from high nickel matte according to claim 3, wherein: the electrode reaction channel is a tubular diaphragm channel, and the two ends of the tubular diaphragm channel are respectively an input end of the electrode reaction channel and an output end of the electrode reaction channel.
6. A method for preparing electrodeposited nickel from high nickel matte according to claim 3, wherein: the length of the electrical external conductor extends along the axial direction of the tubular diaphragm channel; the electrical external conductor has a helical section located in the tubular diaphragm passage.
7. A method for preparing electrodeposited nickel from high nickel matte according to claim 3, wherein: the electrode support body is internally provided with at least two electrode reaction channels, the at least two electrode reaction channels are connected in parallel between the electrode input channel and the electrode output channel, and the electric external conductors in the at least two electrode reaction channels are used for being connected with the same pole of a power supply.
8. A method for preparing electrodeposited nickel from high nickel matte according to claim 3, wherein: the separator allows passage of a) ions and b) at least a) ions in the solvent in the electrode liquid, but does not allow passage of other components in the electrode liquid.
9. A method for preparing electrodeposited nickel from high nickel matte according to claim 3, wherein: the electrode liquid has at least the following characteristics: 1) The conductivity required for the electrode reaction is satisfied; 2) Is capable of dissolving the feed gas required for the electrode reaction; 3) Contains the conductive particles capable of adsorbing and dissolving the raw material gas in the electrode liquid.
10. An electrodeposition apparatus characterized in that: comprising the following steps:
a main container;
an electrolyte stored in the main container;
a first electrode accommodated in the main container, the first electrode employing a gas-consuming electrode assembly;
a second electrode accommodated in the main container, the second electrode being a solid plate;
the two poles of the power supply are respectively connected with the first electrode and the second electrode and are used for supplying power;
a separator disposed between the first electrode and the second electrode, dividing the main container into a cathode chamber accommodating the first electrode and an anode chamber accommodating the second electrode;
wherein the gas-consuming electrode assembly comprises an electrode and an electrode liquid circulation system;
wherein the electrode comprises:
an electrode support having a pore structure permeable to an electrolyte;
an electrode reaction channel formed by a separator provided in the electrode support body;
the electrode input channel is arranged on the electrode support body and is communicated with the input end of the electrode reaction channel;
the electrode output channel is arranged on the electrode support body and is communicated with the output end of the electrode reaction channel;
an electrical external conductor arranged on the electrode support body and extending into the electrode reaction channel;
In operation, the electrode input channel receives electrode liquid before electrode reaction and guides the electrode liquid into the electrode reaction channel, the electrode output channel outputs electrode liquid after electrode reaction from the electrode reaction channel, the electric external conductor is used for providing an electron migration external connection path required by electrode reaction for the electrode liquid in the electrode reaction channel, and the electrode liquid is used for forming a flowing electrode in the electrode reaction channel so as to realize electron migration required by the electrode reaction on the flowing electrode;
the electrode liquid circulation system comprises:
one end of the electrode liquid circulating pipeline is connected with the inlet of the electrode input channel, and the other end of the electrode liquid circulating pipeline is connected with the outlet of the electrode output channel;
the circulating pump is arranged in the electrode liquid circulating pipeline in series;
the regulating valve is arranged in the electrode liquid circulating pipeline in series;
and the gas dissolving device is arranged in the electrode liquid circulating pipeline in series and is used for dissolving the raw material gas required by the electrode reaction in the electrode liquid.
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