WO2016119722A1 - 一种提纯制备高纯五氧化二钒粉体的系统及方法 - Google Patents
一种提纯制备高纯五氧化二钒粉体的系统及方法 Download PDFInfo
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- WO2016119722A1 WO2016119722A1 PCT/CN2016/072524 CN2016072524W WO2016119722A1 WO 2016119722 A1 WO2016119722 A1 WO 2016119722A1 CN 2016072524 W CN2016072524 W CN 2016072524W WO 2016119722 A1 WO2016119722 A1 WO 2016119722A1
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- vanadium
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- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 title claims abstract description 194
- 239000000843 powder Substances 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 37
- 239000007789 gas Substances 0.000 claims abstract description 203
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 108
- ZHXZNKNQUHUIGN-UHFFFAOYSA-N chloro hypochlorite;vanadium Chemical compound [V].ClOCl ZHXZNKNQUHUIGN-UHFFFAOYSA-N 0.000 claims abstract description 61
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical class [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 60
- UNTBPXHCXVWYOI-UHFFFAOYSA-O azanium;oxido(dioxo)vanadium Chemical compound [NH4+].[O-][V](=O)=O UNTBPXHCXVWYOI-UHFFFAOYSA-O 0.000 claims abstract description 55
- 238000001354 calcination Methods 0.000 claims abstract description 47
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 41
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000000460 chlorine Substances 0.000 claims abstract description 4
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 4
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims description 111
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 72
- 235000019270 ammonium chloride Nutrition 0.000 claims description 55
- 239000003546 flue gas Substances 0.000 claims description 50
- 239000007788 liquid Substances 0.000 claims description 48
- CGFLRDJQEKNAGT-UHFFFAOYSA-N [V].O(Cl)Cl.[V] Chemical compound [V].O(Cl)Cl.[V] CGFLRDJQEKNAGT-UHFFFAOYSA-N 0.000 claims description 38
- 229910052720 vanadium Inorganic materials 0.000 claims description 37
- 238000010992 reflux Methods 0.000 claims description 32
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 30
- 238000003860 storage Methods 0.000 claims description 30
- 239000002253 acid Substances 0.000 claims description 28
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 24
- 229910052710 silicon Inorganic materials 0.000 claims description 24
- 239000010703 silicon Substances 0.000 claims description 24
- 239000006096 absorbing agent Substances 0.000 claims description 22
- 238000007789 sealing Methods 0.000 claims description 22
- 238000004821 distillation Methods 0.000 claims description 21
- 239000002893 slag Substances 0.000 claims description 18
- 239000012535 impurity Substances 0.000 claims description 17
- 238000009835 boiling Methods 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 13
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 13
- 239000000446 fuel Substances 0.000 claims description 12
- 229910021529 ammonia Inorganic materials 0.000 claims description 11
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 11
- 238000000746 purification Methods 0.000 claims description 11
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 10
- 238000002386 leaching Methods 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000002360 preparation method Methods 0.000 claims description 6
- 229910021642 ultra pure water Inorganic materials 0.000 claims description 6
- 239000012498 ultrapure water Substances 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 239000000779 smoke Substances 0.000 claims description 5
- 238000000354 decomposition reaction Methods 0.000 claims description 4
- 238000005243 fluidization Methods 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 2
- 239000012071 phase Substances 0.000 claims 10
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims 3
- RCJVRSBWZCNNQT-UHFFFAOYSA-N dichloridooxygen Chemical compound ClOCl RCJVRSBWZCNNQT-UHFFFAOYSA-N 0.000 claims 1
- 239000007791 liquid phase Substances 0.000 claims 1
- MXXWOMGUGJBKIW-YPCIICBESA-N piperine Chemical compound C=1C=C2OCOC2=CC=1/C=C/C=C/C(=O)N1CCCCC1 MXXWOMGUGJBKIW-YPCIICBESA-N 0.000 claims 1
- 229940075559 piperine Drugs 0.000 claims 1
- 235000019100 piperine Nutrition 0.000 claims 1
- 239000012808 vapor phase Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000002351 wastewater Substances 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000005576 amination reaction Methods 0.000 abstract 1
- 230000002349 favourable effect Effects 0.000 abstract 1
- 239000007858 starting material Substances 0.000 abstract 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 34
- 239000000243 solution Substances 0.000 description 15
- 238000001556 precipitation Methods 0.000 description 13
- 239000002994 raw material Substances 0.000 description 13
- 239000000047 product Substances 0.000 description 12
- 150000003863 ammonium salts Chemical class 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 7
- 239000003153 chemical reaction reagent Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- -1 ammonium ions Chemical class 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000007062 hydrolysis Effects 0.000 description 4
- 238000006460 hydrolysis reaction Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 230000033228 biological regulation Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229910021550 Vanadium Chloride Inorganic materials 0.000 description 2
- XHCLAFWTIXFWPH-UHFFFAOYSA-N [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] XHCLAFWTIXFWPH-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 229910045601 alloy Inorganic materials 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 229910001510 metal chloride Inorganic materials 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- RPESBQCJGHJMTK-UHFFFAOYSA-I pentachlorovanadium Chemical compound [Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[V+5] RPESBQCJGHJMTK-UHFFFAOYSA-I 0.000 description 2
- 239000012629 purifying agent Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229910001935 vanadium oxide Inorganic materials 0.000 description 2
- NGNBDVOYPDDBFK-UHFFFAOYSA-N 2-[2,4-di(pentan-2-yl)phenoxy]acetyl chloride Chemical compound CCCC(C)C1=CC=C(OCC(Cl)=O)C(C(C)CCC)=C1 NGNBDVOYPDDBFK-UHFFFAOYSA-N 0.000 description 1
- DDFHBQSCUXNBSA-UHFFFAOYSA-N 5-(5-carboxythiophen-2-yl)thiophene-2-carboxylic acid Chemical compound S1C(C(=O)O)=CC=C1C1=CC=C(C(O)=O)S1 DDFHBQSCUXNBSA-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical group [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 1
- 206010024769 Local reaction Diseases 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 229910021552 Vanadium(IV) chloride Inorganic materials 0.000 description 1
- GDQJRIJQPNLZBK-UHFFFAOYSA-A [V+5].O(Cl)Cl.[V+5].[Cl-].[V+5].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-] Chemical compound [V+5].O(Cl)Cl.[V+5].[Cl-].[V+5].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-] GDQJRIJQPNLZBK-UHFFFAOYSA-A 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- SKKMWRVAJNPLFY-UHFFFAOYSA-N azanylidynevanadium Chemical compound [V]#N SKKMWRVAJNPLFY-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000009388 chemical precipitation Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003086 colorant Substances 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- PNXOJQQRXBVKEX-UHFFFAOYSA-N iron vanadium Chemical compound [V].[Fe] PNXOJQQRXBVKEX-UHFFFAOYSA-N 0.000 description 1
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 1
- 229910001416 lithium ion Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 1
- 229920005591 polysilicon Polymers 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 229910001456 vanadium ion Inorganic materials 0.000 description 1
- IBYSTTGVDIFUAY-UHFFFAOYSA-N vanadium monoxide Chemical compound [V]=O IBYSTTGVDIFUAY-UHFFFAOYSA-N 0.000 description 1
- JTJFQBNJBPPZRI-UHFFFAOYSA-J vanadium tetrachloride Chemical compound Cl[V](Cl)(Cl)Cl JTJFQBNJBPPZRI-UHFFFAOYSA-J 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G31/00—Compounds of vanadium
- C01G31/02—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/71—Feed mechanisms
- B01F35/717—Feed mechanisms characterised by the means for feeding the components to the mixer
- B01F35/7173—Feed mechanisms characterised by the means for feeding the components to the mixer using gravity, e.g. from a hopper
- B01F35/71731—Feed mechanisms characterised by the means for feeding the components to the mixer using gravity, e.g. from a hopper using a hopper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
- B01J6/001—Calcining
- B01J6/004—Calcining using hot gas streams in which the material is moved
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01L—CHEMICAL OR PHYSICAL LABORATORY APPARATUS FOR GENERAL USE
- B01L5/00—Gas handling apparatus
- B01L5/04—Gas washing apparatus, e.g. by bubbling
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/06—Binary compounds of nitrogen with metals, with silicon, or with boron, or with carbon, i.e. nitrides; Compounds of nitrogen with more than one metal, silicon or boron
- C01B21/0615—Binary compounds of nitrogen with metals, with silicon, or with boron, or with carbon, i.e. nitrides; Compounds of nitrogen with more than one metal, silicon or boron with transition metals other than titanium, zirconium or hafnium
- C01B21/0617—Binary compounds of nitrogen with metals, with silicon, or with boron, or with carbon, i.e. nitrides; Compounds of nitrogen with more than one metal, silicon or boron with transition metals other than titanium, zirconium or hafnium with vanadium, niobium or tantalum
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G31/00—Compounds of vanadium
- C01G31/04—Halides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00164—Controlling or regulating processes controlling the flow
- B01J2219/00166—Controlling or regulating processes controlling the flow controlling the residence time inside the reactor vessel
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Definitions
- the invention belongs to the field of chemical industry and material, and particularly relates to a system and a method for purifying and preparing high-purity vanadium pentoxide powder.
- Vanadium pentoxide is one of the important industrial vanadium products, widely used in the production of alloy additives such as vanadium iron and vanadium nitride, as well as catalysts, colorants, and hard alloy additives. With the continuous development of new energy technologies, the battery industry is increasingly demanding high-purity vanadium pentoxide (purity of more than 3N5), including all-vanadium flow batteries (VRB) with good large-scale energy storage performance and vanadium for electric vehicles.
- the acid salt is a lithium ion battery or the like.
- the vanadium solution is usually obtained by leaching a vanadium solution or a vanadium-rich material (such as ammonium polyvanadate, ammonium metavanadate, industrial grade vanadium pentoxide, etc.), and is purified by chemical precipitation or (and) solvent extraction/ion.
- a vanadium-rich material such as ammonium polyvanadate, ammonium metavanadate, industrial grade vanadium pentoxide, etc.
- the impurity removal process parameters are closely related to the impurity content of the raw materials, so the adaptability to the raw materials is poor; the calcium salt, magnesium salt purifying agent or extractant used in the purification process, the acid-base reagent, and the ammonium salt for vanadium precipitation are also It is easy to introduce impurities.
- it is generally required to use an expensive reagent with a high purity, so that the cost is too high, the scale cannot be produced, and the purity of the product is difficult to be stabilized at 3N5 or more.
- the related institution also proposes to adopt the repeated precipitation method to purify and remove the vanadium solution, that is, to utilize the ammonium salt precipitation property of the vanadium-containing solution to selectively select vanadium.
- the raw material chlorination-rectification purification-subsequent treatment is a common preparation process for high-purity materials, such as high purity. Silicon (polysilicon), high purity silica, and the like.
- vanadium chloride vanadium oxychloride vanadium has a large difference from the boiling points of common impurities such as iron, calcium, magnesium, aluminum, sodium, potassium, etc., it is easy to obtain high purity vanadium oxychloride by rectification, and from high purity three High-purity vanadium pentoxide can be prepared by hydrolysis of vanadium oxychloride by hydrolysis and precipitation of ammonium salts, followed by calcination. Therefore, the preparation of high-purity vanadium pentoxide by the chlorination method has a great advantage in principle.
- the patent has the following deficiencies: (1) Similar to the aforementioned Iowa State University study, the patent actually only gives the principle of chlorination, lacking specific operational solutions, such as chlorination including both boiling chlorine And include molten salt chlorination, and molten salt chlorination and boiling chlorination are completely different chlorination methods; for example, for chlorination reactors, "rotary kiln, fluidized furnace, boiling furnace, shaft furnace, Reactors such as multi-hearth furnaces actually cover almost all common mainstream reactors in the metallurgical industry, but different reactors have very different requirements for raw materials. Shaft furnaces can only handle "coarse" particles larger than 8 mm.
- fine particles need to be treated with pellets and pre-sintering, while boiling chlorination is generally suitable for processing fine particles, so for a specific vanadium raw material, it cannot be directly applied to rotary kiln, fluidized furnace, boiling furnace, shaft furnace, and more.
- the reactor such as a crucible furnace; and the "fluidizer” and the “boiling furnace” are essentially the same, but the name is different; thus, it can be seen that the operation modes and conditions of these reactors are very different.
- vanadium raw material chlorination technology still has the following two problems: (1) vanadium raw material chlorination roasting is a strong exothermic process, and the heat generated by the chlorination reaction can satisfy the solid and gas. In addition to the preheating of the reaction material, it is still necessary to remove the heat through the furnace wall to stabilize the chlorination temperature. Therefore, the solid and the gas usually enter the reactor at a near room temperature, and the chlorination reaction generates heat to preheat before participating in the reaction.
- the local reaction efficiency of the chlorination reactor is too low; (2) due to the need to remove the heat generated by the chlorination reaction by a large amount of heat dissipation to maintain the operating temperature, the operating conditions and environmental climate changes are liable to cause chlorination temperature fluctuations, resulting in chlorination selection. Reduced sex and efficiency require a reasonable heat balance supply and temperature regulation. Therefore, it is necessary to provide a reasonable heat supply and temperature control to effectively increase the chlorination efficiency and obtain a stable chlorination temperature to ensure the selectivity of chlorination to effectively suppress the chlorination of impurities.
- the regulation of the chlorination process the improvement of the direct yield of vanadium, the avoidance of a large amount of ammonia nitrogen wastewater, and the improvement of the vanadium pentoxide purification efficiency are the techniques for improving the purity of vanadium pentoxide by chlorination.
- the present invention provides a system and method for purifying and preparing high-purity vanadium pentoxide powder to ensure good selectivity of low-temperature chlorination, avoiding generation of a large amount of ammonia-nitrogen wastewater, and reducing production of high-purity vanadium pentoxide. Energy consumption and operating costs.
- the present invention adopts the following technical solutions:
- the system for purifying and preparing high-purity vanadium pentoxide powder of the invention comprises the feeding device 1, the low-temperature chlorination fluidized bed 2, the rectification and purification device 3, the gas-vaporized ammonium fluidized bed 4, the ammonium metavanadate Feeding device 5, calcining fluidized bed 6, exhaust gas leaching absorber 7, induced draft fan 8 and chimney 9;
- the feeding device 1 comprises an industrial grade vanadium pentoxide silo 1-1, an industrial grade vanadium pentoxide screw feeder 1-2, a carbon powder silo 1-3 and a carbon powder screw feeder 1-4;
- the low temperature chlorination fluidized bed 2 comprises a chlorination bed feeder 2-1, a chlorinated fluidized bed main body 2-2, a chlorinated bed cyclone 2-3, a flue gas heat exchanger 2-4, a smoke Gas condenser 2-5, chlorinated bed acid sealed tank 2-6 and chlorination Bed spiral slag remover 2-7;
- the rectification and purification device 3 includes a distillation still 3-1, a rectification column 3-2, a distillate condenser 3-3, a reflux liquid collection tank 3-4, a silicon-containing vanadium oxychloride vanadium storage tank 3-5, Distillation section acid sealing tank 3-6, high purity vanadium oxychloride vanadium condenser 3-7 and high purity vanadium oxychloride vanadium storage tank 3-8;
- the gas phase ammonium chloride fluidized bed 4 comprises an ammonium bed air purifier 4-1, an ammonium bed gas heater 4-2, a vanadium oxychloride nozzle 4-3, a gas phase ammonium chloride fluidized bed body 4-4, Ammonium bed cyclone 4-5 and ammonium bed discharger 4-6;
- the ammonium metavanadate feeding device 5 comprises ammonium metavanadate silo 5-1 and ammonium metavanadate screw feeder 5-2;
- the calcined fluidized bed 6 comprises a calcined bed air purifier 6-1, a calcined bed gas heater 6-2, a calcined bed feeder 6-3, a calcined fluidized bed main body 6-4, a calcined bed cyclone 6 -5 and high purity vanadium pentoxide silo 6-6;
- the outlet of the bottom of the industrial grade vanadium pentoxide silo 1-1 is connected to the inlet of the industrial grade vanadium pentoxide screw feeder 1-2; the bottom of the carbon powder silo 1-3
- the discharge port is connected to the feed port of the carbon powder screw feeder 1-4; the discharge port of the industrial grade vanadium pentoxide screw feeder 1-2, the carbon powder screw feeder 1-
- the discharge ports of 4 are connected to the feed port of the chlorination bed feeder 2-1 through a pipe;
- the discharge port of the chlorination bed feeder 2-1 is connected to the inlet of the upper portion of the chlorinated fluidized bed main body 2-2 through a pipe; the bottom of the chlorination bed feeder 2-1
- the inlet port is connected to the nitrogen gas source manifold through a pipe;
- the chlorination bed cyclone separator 2-3 is disposed at the top center of the enlarged section of the chlorination fluidized bed main body 2-2;
- the chlorination bed cyclone separation The gas outlet at the top of the 2-3 is connected to the hot flue gas inlet of the flue gas heat exchanger 2-4 through a pipe; the cold flue gas outlet of the flue gas heat exchanger 2-4 passes through the pipe and the smoke a gas inlet of the gas condenser 2-5 is connected;
- a gas outlet of the flue gas condenser 2-5 is connected to a gas inlet of the chlorinated bed acid sealing tank 2-6 through a pipe;
- the chlorinated bed acid The gas outlet of the sealing tank 2-6 is connected
- the liquid outlet at the bottom of the flue gas condenser 2-5 is connected to the feed port of the rectification column 3-2 through a pipe; the vapor outlet of the distillation still 3-1 passes through the pipe and the rectification column 3 a vapor inlet of -2 is connected; a reflux port of the distillation pot 3-1 is connected to a liquid reflux outlet at the bottom of the rectification column 3-2 through a pipe;
- the gas outlet at the top of the rectification column 3-2 is connected to the gas inlet of the distillate condenser 3-3 through a conduit; the liquid outlet of the distillate condenser 3-3 is passed through the conduit and the reflux a liquid inlet of the liquid collection tank 3-4 is connected; a reflux liquid outlet of the reflux liquid collection tank 3-4 is connected to a reflux liquid inlet at the top of the rectification column 3-2 through a conduit; the reflux liquid collection tank
- the discharge opening of 3-4 is connected to the inlet of the silicon-containing vanadium oxychloride vanadium storage tank
- the inlet of the ammonium bed air purifier 4-1 is connected to the compressed air manifold through a pipeline; the outlet of the ammonium bed air purifier 4-1 is separately connected to the ammonium bed gas heater through a pipeline
- the inlet of 4-2, the gas inlet of vanadium oxychloride nozzle 4-3 and the inlet of the bottom of the ammonium bed discharger 4-6 are connected; the inlet of the ammonium bed gas heater 4-2
- the gas port is connected to the ultrapure water and the purified liquid ammonia main pipe through a pipeline; the combustion air inlet and the fuel inlet of the burner of the ammonium bed gas heater 4-2 are respectively connected to the compressed air main pipe and the fuel main pipe through the pipeline;
- the gas outlet of the ammonium bed gas heater 4-2 is connected to the gas inlet of the bottom of the gas phase ammonium chloride fluidized bed main body 4-4 through a pipe; the high purity vanadium oxychloride vanadium storage tank 3-8 The liquid outlet is connected to the
- the discharge port at the bottom of the ammonium metavanadate silo 5-1 is connected to the feed port of the ammonium metavanadate screw feeder 5-2; the row of the ammonium metavanadate screw feeder 5-2
- the feed port is connected to the feed port of the calcined bed feeder 6-3 through a pipe through a pipe;
- the intake port of the calcining bed air purifier 6-1 is connected to the compressed air manifold through a pipe; the gas outlet of the calcining bed air purifier 6-1 is respectively connected to the calcined bed gas heater 6-2 through a pipe
- the air inlet is connected to the air inlet at the bottom of the calcined bed feeder 6-3; the combustion air inlet and the fuel inlet of the calcining bed gas heater 6-2 are respectively passed through the pipeline and the compressed air main pipe and the fuel main pipe Connected; the gas outlet of the calcined bed gas heater 6-2 passes through the pipe and the bottom of the calcined fluidized bed main body 6-4
- the gas discharge port is connected; the discharge port of the calcined bed feeder 6-3 is connected to the feed port of the lower portion of the calcined bed fluidized bed main body 6-4 through a pipe; the calcined fluidized bed main body 6-4
- the top air outlet is connected to the inlet of the calcining bed cyclone 6-5 through
- the gas outlet of the exhaust gas rinsing absorber 7 is connected to the gas inlet of the draft fan 8 through a pipe; the gas outlet of the draft fan 8 is connected to the gas inlet at the bottom of the chimney 9 through a pipe.
- the method for purifying and preparing high-purity vanadium pentoxide powder based on the above system of the present invention comprises the following steps:
- the industrial grade vanadium pentoxide powder in the industrial grade vanadium pentoxide silo 1-1 and the carbon powder of the carbon powder silo 1-3 are respectively passed through the industrial grade vanadium pentoxide spiral feeder 1 -2 and the carbon powder screw feeder 1-4 simultaneously enter the chlorination bed feeder 2-1 and then enter the chlorination fluidized bed main body 2-2; chlorine gas and nitrogen gas from the chlorine gas source main pipe
- the nitrogen of the gas source main pipe and the air of the compressed air main pipe are preheated by heat exchange between the flue gas heat exchanger 2-4 and the chlorinated flue gas, and then enter the chlorinated fluidized bed main body 2-2 to make vanadium pentoxide.
- the powder material such as carbon powder maintains fluidization and chemical reaction with it.
- the air causes some of the carbon powder to burn to provide heat to maintain the fluidized bed temperature.
- the chlorine gas and the carbon powder work together to chlorinate vanadium pentoxide and a small amount of impurities.
- the crude vanadium oxychloride vapor formed by the flue gas condenser 2-5 enters the rectification column 3-2 and the distillation still 3-1, and is subjected to a rectification operation to obtain a vanadium-rich scrap rich in high-boiling impurities.
- the vanadium-rich waste is used for subsequent recovery of vanadium
- the silicon-containing vanadium oxychloride vapor is passed through the distillate condenser 3-3 After condensing to the liquid, part of the reflux liquid collection tank 3-4 is refluxed to the rectification column 3-2, and the rest is introduced into the silicon-containing vanadium oxychloride vanadium storage tank 3-5; the silicon-containing vanadium oxychloride vanadium storage
- the spent gas generated in the tank 3-5 is sent to the exhaust gas leaching absorber 7 through the acid sealing tank 3-6 of the rectifying section, and the silicon-containing vanadium oxychloride can be used for catalysis and other chemical fields;
- the vanadium oxychloride vapor is condensed into the liquid through the high-purity vanadium oxychloride condenser
- the high purity vanadium oxychloride vanadium of the high purity vanadium oxychloride vanadium storage tank 3-8 is produced by the vanadium oxychloride vanadium nozzle 4-3
- Purified air from the ammonium bed air purifier 4-1 is loaded into the gas phase ammonium chloride fluidized bed main body 4-4; ultrapure water, purified liquid ammonia and purified air are passed through the ammonium bed gas heater 4 -2 is preheated and sent to the gas phase ammonium chloride fluidized bed main body 4-4 to maintain fluidization of the powder in the bed, and hydrolyze and ammoniumlate vanadium oxychloride to form vanadium oxide containing ammonium chloride.
- ammonium acid powder, the ammonium ammonium metaphosphate-containing ammonium metavanadate powder is discharged into the ammonium metavanadate silo 5-1 through the ammonium bed discharger 4-6, and the ammonia is produced.
- the ammonium fluoride is removed from the dust by the ammonium bed cyclone 4-5 and sent to the tail gas treatment unit for treatment;
- the ammonium chloride-containing ammonium metavanadate powder in the ammonium metavanadate silo 5-1 is sequentially passed through the ammonium metavanadate screw feeder 5-2 and the calcined bed feeder 6-3. Calcining the fluidized bed main body 6-4; the compressed air is sequentially preheated by the calcining bed air purifier 6-1 and the calcined bed gas heater 6-2, and then introduced into the calcined fluidized bed main body 6-4. The powder in the bed is maintained fluidized, and the ammonium meta-vanadate material containing ammonium chloride is thermally decomposed to obtain a high-purity vanadium pentoxide powder product, and the upper row of the fluidized bed main body 6-4 is calcined.
- the feed port enters the high-purity vanadium pentoxide bin 6-6; the calcined flue gas generated by the calcination decomposition enters the calcining bed cyclone separator 6-5, and the ammonium chloride is separated and the dust is removed to be sent to the tail gas treatment unit. Processing; the ammonium chloride powder collected by the calcined bed cyclone 6-5 is sent to an ammonium chloride silo;
- the gas discharged from the exhaust gas eluting absorber 7 after being absorbed by the alkali solution is sent to the chimney 9 through the induced draft fan 8 and then emptied.
- One of the features of the present invention is that in the chlorinated fluidized bed main body 2-2, the chlorination process carbon powder is added in an amount of 10% to 20% by mass of the industrial grade vanadium pentoxide powder, and chlorinated.
- the operating temperature is 300-500 ° C, and the average residence time of the powder is 30-80 min.
- the second feature of the present invention is that in the rectification column 3-2, the number of trays in the rectification operation rectification section is 5 to 10, and the number of trays in the stripping section is 10 to 20; During the distillation operation, the reflux ratio (ie, the ratio of the reflux flow at the top of the column to the discharge amount) is maintained at 15 to 40.
- the third feature of the present invention is that, in the gas phase ammonium chloride fluidized bed main body 4-4, ammonium metavanadate is prepared by gas phase ammonium crystallization of high-purity vanadium oxychloride, and the operating temperature of the gas phase ammonium is 130-250. °C, the molar ratio of water vapor to ammonia is 0.5 to 0.8, and the molar ratio of ammonia to vanadium oxychloride is 3.5 to 4.5.
- the fourth feature of the present invention is that in the calcined fluidized bed main body 6-4, thermal decomposition of ammonium ammonium metaphosphate containing ammonium metavanadate is achieved by fluidized calcination, the calcination operation temperature is 400 to 650 ° C, powder The average residence time of the material is 60-180 min.
- the purity of the high-purity vanadium pentoxide powder obtained by the invention is above 4N. Compared with the prior art, the present invention has the following outstanding advantages:
- the chlorination gas is preheated by the heat exchange between the chlorinated gas and the chlorinated flue gas while cooling the flue gas. Heat, the temperature distribution of the chlorination reactor is more uniform, and the low-temperature chlorination efficiency of the vanadium raw material is effectively improved;
- a part of the carbon powder is burned by appropriate amount of air to achieve heat balance supply and temperature regulation of the chlorination process, stabilize the chlorination operation temperature, improve the chlorination reaction efficiency and ensure good selectivity of chlorination, and avoid the formation of tetrachlorination.
- side reactions such as vanadium;
- Ammonium metavanadate containing ammonium chloride is fluidized and calcined, ammonium metavanadate is decomposed to high-purity vanadium pentoxide product, and ammonium chloride is also decomposed and discharged with flue gas. After cooling, ammonium chloride can be obtained.
- the product effectively realizes the preparation of high-purity products and the recovery of ammonium chloride.
- the invention has the advantages of strong adaptability of raw materials, good selectivity of low-temperature chlorination, non-polluting wastewater discharge, low production energy consumption and low operation cost, stable product quality, and the like, and is suitable for large-scale high-purity vanadium pentoxide powder of 4N or more.
- Industrial production has good economic efficiency and social benefits.
- Figure 1 is a schematic view showing the configuration of a high purity vanadium pentoxide powder system of the present invention.
- FIG. 1 is a schematic view of a system for purifying and preparing high-purity vanadium pentoxide powder according to the present invention.
- the system for purifying high-purity vanadium pentoxide powder used in the present embodiment comprises a feeding device 1, a low-temperature chlorination fluidized bed 2, a rectification purification device 3, a gas-phase ammonium chloride fluidized bed 4, Ammonium metavanadate feeding device 5, calcining fluidized bed 6, exhaust gas leaching absorber 7, induced draft fan 8 and chimney 9;
- the feeding device 1 comprises an industrial grade vanadium pentoxide silo 1-1, an industrial grade vanadium pentoxide spiral feeder 1-2, a carbon powder silo 1-3 and a carbon powder screw feeder 1-4;
- the low temperature chlorination fluidized bed 2 comprises a chlorination bed feeder 2-1, a chlorinated fluidized bed main body 2-2, a chlorinated bed cyclone 2-3, a flue gas heat exchanger 2-4, a flue gas condensation 2-5, chlorinated bed acid sealed tank 2-6 and chlorinated bed spiral slag remover 2-7;
- the rectification and purification device 3 includes a distillation still 3-1, a rectification column 3-2, a distillate condenser 3-3, a reflux liquid collection tank 3-4, a silicon-containing vanadium oxychloride vanadium storage tank 3-5, and a rectification Segment acid sealing tank 3-6, high purity vanadium oxychloride vanadium condenser 3-7 and high purity vanadium oxychloride vanadium storage tank 3-8;
- the gas phase ammonium chloride fluidized bed 4 comprises an ammonium bed air purifier 4-1, an ammonium bed gas heater 4-2, a vanadium oxychloride nozzle 4-3, a gas phase ammonium chloride fluidized bed body 4-4, and an ammonium chloride.
- Ammonium metavanadate feeding device 5 comprises ammonium metavanadate silo 5-1 and ammonium metavanadate screw feeder 5-2;
- the calcined fluidized bed 6 comprises a calcined bed air purifier 6-1, a calcined bed gas heater 6-2, a calcined bed feeder 6-3, a calcined fluidized bed main body 6-4, a calcined bed cyclone separator 6-5 And high purity vanadium pentoxide silo 6-6;
- the outlet of the bottom of the industrial grade vanadium pentoxide silo 1-1 is connected with the inlet of the industrial grade vanadium pentoxide screw feeder 1-2; the outlet of the carbon powder silo 1-3 and the charcoal
- the feed ports of the powder auger feeders 1-4 are connected; the discharge ports of the industrial grade vanadium pentoxide screw feeder 1-2, the discharge ports of the carbon powder screw feeders 1-4 are all fed with the chlorination bed
- the feed ports of the 2-1 are connected by pipes;
- the discharge port of the chlorination bed feeder 2-1 is connected to the inlet of the upper part of the chlorination fluidized bed main body 2-2 through a pipe; the inlet of the bottom of the chlorination bed feeder 2-1 is piped and The nitrogen gas source manifold is connected; the chlorination bed cyclone separator 2-3 is disposed at the top center of the enlarged section of the chlorination fluidized bed main body 2-2; the gas outlet of the chlorinated bed cyclone separator 2-3 passes through the pipeline and the smoke
- the hot flue gas inlets of the gas heat exchangers 2-4 are connected; the cold flue gas outlets of the flue gas heat exchangers 2-4 are connected to the gas inlets of the flue gas condensers 2-5 through pipes; the flue gas condensers 2 -
- the gas outlet of 5 is connected to the gas inlet of the chlorinated bed acid sealing tank 2-6 through a pipe; the gas outlet of the chlorinated bed acid sealing tank 2-6 is connected to the gas inlet of the exhaust gas leaching absorb
- the liquid outlet at the bottom of the flue gas condenser 2-5 is connected to the feed port of the rectification column 3-2 through a pipe; the vapor outlet of the distillation still 3-1 is connected to the vapor inlet of the rectification column 3-2 through a pipe; The reflux port of the still 3-1 is connected to the liquid reflux outlet at the bottom of the rectification column 3-2 through a pipe; the gas outlet at the top of the rectification column 3-2 is passed through the gas inlet of the distillate condenser 3-3 through the pipe.
- the liquid outlet of the distillate condenser 3-3 is connected to the liquid inlet of the reflux liquid collection tank 3-4 through a pipe; the reflux liquid outlet of the reflux liquid collection tank 3-4 is passed through the pipe and the top of the rectification column 3-2
- the reflux liquid inlet is connected;
- the discharge port of the reflux liquid collection tank 3-4 is connected to the inlet of the silicon-containing vanadium oxychloride vanadium storage tank 3-5 through the pipeline;
- the silicon-containing vanadium oxychloride vanadium storage tank 3-5 is lacking
- the gas outlet is connected to the gas inlet of the acid sealing tank 3-6 of the rectifying section through a pipeline;
- the gas outlet of the rectifying acid sealing tank 3-6 is connected to the gas inlet of the exhaust gas eluting absorber 7 through a pipeline;
- the rectification tower 3 -2 of the distillate outlet is connected to the gas inlet of the high purity vanadium oxychloride condenser 3-7 through a pipe;
- the inlet of the ammonium bed air purifier 4-1 is connected to the compressed air manifold through a pipeline; the outlet of the ammonium bed air purifier 4-1 is separately connected to the inlet of the ammonium bed gas heater 4-2 through a pipeline. Mouth, trichloroox
- the gas inlet of the vanadium nozzle 4-3 and the inlet of the bottom of the ammonium bed discharger 4-6 are connected; the inlet of the ammonium bed gas heater 4-2 passes through the pipeline and the ultrapure water, the purified liquid ammonia manifold
- the gasification inlet and the fuel inlet of the burner of the ammonium bed gas heater 4-2 are respectively connected to the compressed air main pipe and the fuel main pipe through the pipeline; the gas outlet of the ammonium gasifier 4-2 passes through the pipeline and the gas phase
- the inlet ports at the bottom of the ammonium fluidized bed main body 4-4 are connected; the liquid outlet of the high purity vanadium oxychloride vanadium storage tank 3-8 is connected through
- the ammonium bed cyclone 4-5 is disposed at the top center of the enlarged section of the gas phase ammonium chloride fluidized bed main body 4-4; the top gas outlet of the ammonium bed cyclone 4-5 is connected to the exhaust gas treatment unit through a pipe;
- the discharge port of the upper portion of the gas phase ammonium chloride fluidized bed main body 4-4 is connected to the feed port of the ammonium bed discharger 4-6 through a pipe;
- the discharge port of the ammonium bed discharger 4-6 is piped and The feed ports of the ammonium metavanadate silo 5-1 are connected;
- the discharge port at the bottom of the ammonium metavanadate silo 5-1 is connected with the feed port of the ammonium metavanadate screw feeder 5-2; the discharge port of the ammonium metavanadate screw feeder 5-2 is piped and calcined.
- the feed ports of the bed feeder 6-3 are connected by pipes;
- the intake port of the calcining bed air purifier 6-1 is connected to the compressed air manifold through a pipe; the gas outlet of the calcining bed air purifier 6-1 is respectively passed through the pipe to the inlet and the calcination of the calcining bed gas heater 6-2.
- the air inlets at the bottom of the bed feeder 6-3 are connected; the combustion air inlet and the fuel inlet of the burner of the calcining bed gas heater 6-2 are respectively connected to the compressed air main pipe and the fuel main pipe through a pipe; the calcining bed gas heater
- the gas outlet of 6-2 is connected to the inlet of the bottom of the calcined fluidized bed main body 6-4 through a pipe; the discharge port of the calcined bed feeder 6-3 passes through the pipe and the lower part of the fluidized bed main body 6-4 of the calcined bed.
- the feed ports are connected; the gas outlet at the top of the calcined fluidized bed main body 6-4 is connected to the inlet of the calcination bed cyclone 6-5 through a pipe; the powder outlet at the bottom of the calcination bed cyclone 6-5 Connected to the inlet of the ammonium chloride silo through a pipeline; the top outlet of the calciner cyclone separator 6-5 is connected to the tail gas treatment unit through a pipe; the discharge port of the upper portion of the main body 6-4 of the calcined fluidized bed passes through the pipeline Connected to the feed port of the high purity vanadium pentoxide silo 6-6;
- the gas outlet of the exhaust gas rinsing absorber 7 is connected to the gas inlet of the draft fan 8 through a pipe; the gas outlet of the draft fan 8 is connected to the gas inlet at the bottom of the chimney 9 through a pipe.
- the high-purity vanadium pentoxide powder is purified by the above system, and the specific method comprises: industrial grade vanadium pentoxide powder and carbon powder silo in the industrial grade vanadium pentoxide silo 1-1
- the carbon powder of 3 is respectively mixed into the chlorinated fluidized bed main body 2-2 by the industrial grade vanadium pentoxide screw feeder 1-2 and the carbon powder screw feeder 1-4 simultaneously entering the chlorination bed feeder 2-1.
- the chlorine gas from the chlorine gas source main pipe, the nitrogen gas of the nitrogen gas source main pipe and the air of the compressed air main pipe are heated and preheated by the flue gas heat exchanger 2-4 and the chlorinated flue gas, and then enter the chlorinated fluidized bed main body 2-2
- the powder materials such as vanadium pentoxide and carbon powder are maintained fluidized and chemicalized. Learning reaction, air causes some carbon powder to burn to provide heat to maintain fluidized bed temperature.
- Chlorine gas and carbon powder work together to chlorinate vanadium pentoxide and a small amount of impurities to form chlorinated residue and chlorination of vanadium oxychloride.
- the crude vanadium oxychloride vapor formed by the flue gas condenser 2-5 enters the rectification column 3-2 and the distillation still 3-1, and is subjected to a rectification operation to obtain a vanadium-rich scrap rich in high-boiling impurities and rich in low-boiling impurities.
- the liquid collection tank 3-4 is refluxed to the rectification column 3-2, and the remaining portion is introduced into the silicon-containing vanadium oxychloride vanadium storage tank 3-5; the spent gas generated in the silicon-containing vanadium oxychloride vanadium storage tank 3-5 is rectified
- the segment acid is sealed 3-6 and sent to the exhaust gas leaching absorber 7.
- the silicon-containing vanadium oxychloride can be used in the chemical industry; the high-purity vanadium oxychloride vapor is passed through the high-purity vanadium oxychloride condenser 3-7 After condensing to liquid, enter the high purity vanadium oxychloride vanadium storage tank 3-8;
- ammonium ammonium metavanadate powder is passed through an ammonium bed discharger 4- 6 is discharged into the ammonium metavanadate silo 5-1, and the ammonia-containing ammonium fumed flue gas is removed by the ammonium bed cyclone 4-5 and sent to the tail gas treatment unit for treatment;
- ammonium chloride-containing ammonium metavanadate powder in the ammonium metavanadate silo 5-1 is sequentially introduced into the calcined fluidized bed main body through the ammonium metavanadate screw feeder 5-2 and the calcined bed feeder 6-3.
- the compressed air is sequentially pre-heated by the calcining bed air purifier 6-1 and the calcined bed gas heater 6-2, and then enters the calcined fluidized bed main body 6-4 to maintain the fluidization in the bed, and
- the ammonium metavanadate material containing ammonium chloride is thermally decomposed to obtain a high-purity vanadium pentoxide powder product, and the high-purity vanadium pentoxide silo 6 is obtained by calcining the discharge port of the upper part of the fluidized bed main body 6-4.
- the gas discharged from the exhaust gas absorbing absorber 7 after being absorbed by the alkali solution is sent to the chimney 9 through the draft fan 8 and then emptied.
- This embodiment uses powdered industrial grade vanadium pentoxide as raw material, and its chemical composition is listed in Table 1.
- the treatment amount is 70kg/h, which is prepared by low temperature chlorination, vanadium oxychloride rectification, gas phase ammoniumation and calcination. A high purity vanadium pentoxide product is obtained.
- the amount of carbon powder added in the low-temperature chlorination process is 10% of the quality of the industrial grade vanadium pentoxide powder, the chlorination operation temperature is 500 ° C, and the average residence time of the powder is 30 min;
- the rectification column 3-2 the number of trays in the rectification section of the rectification section is 5, the number of trays in the stripping section is 10, and the reflux ratio of the rectification operation is 40;
- the gas phase ammonium chloride fluidized bed main body 4-4 The operating temperature of the gas phase ammonium is 130 ° C, the molar ratio of water vapor to ammonia is 0.5, the molar ratio of ammonia to vanadium oxychloride is 4.5; in the calcined fluidized bed main body 6-4, the calcination operation temperature is 400 ° C Under the operating conditions of the average residence time of the powder of 180 min, the direct yield of vanadium is 80%, and the purity of the high-
- the amount of carbon powder added in the low-temperature chlorination process is 20% of the quality of the industrial grade vanadium pentoxide powder, the chlorination operation temperature is 300 ° C, and the average residence time of the powder is 80 min;
- the rectification column 3-2 the number of trays in the rectification section of the rectification section is 10, the number of trays in the stripping section is 20, and the reflux ratio of the rectification operation is 15;
- in the gas phase ammonium chloride fluidized bed main body 4-4 The operating temperature of the gas phase ammonium is 250 ° C, the molar ratio of water vapor to ammonia is 0.8, the molar ratio of ammonia to vanadium oxychloride is 3.5; in the calcined fluidized bed main body 6-4, the calcination operation temperature is 650 °C, under the operating conditions of the average residence time of the powder for 60 min, the direct yield of vanadium is 81%, and the purity of the
Abstract
Description
V2O5 | Si | Ca | Al | Ti | Fe | Mn | Na | K | S |
98.8 | 0.0150 | 0.0275 | 0.0099 | 0.0260 | 0.0971 | 0.0293 | 0.1385 | 0.0714 | 0.1274 |
Claims (8)
- 一种提纯制备高纯五氧化二钒粉体的系统,其特征在于,所述系统包括加料装置(1)、低温氯化流化床(2)、精馏提纯装置(3)、气相铵化流化床(4)、偏钒酸铵加料装置(5)、煅烧流化床(6)、尾气淋洗吸收器(7)、引风机(8)和烟囱(9);所述加料装置(1)包括工业级五氧化二钒料仓(1-1)、工业级五氧化二钒螺旋加料器(1-2)、炭粉料仓(1-3)和炭粉螺旋加料器(1-4);所述低温氯化流化床(2)包括氯化床进料器(2-1)、氯化流化床主体(2-2)、氯化床旋风分离器(2-3)、烟气换热器(2-4)、烟气冷凝器(2-5)、氯化床酸封罐(2-6)和氯化床螺旋排渣器(2-7);所述精馏提纯装置(3)包括蒸馏釜(3-1)、精馏塔(3-2)、馏出物冷凝器(3-3)、回流液收集罐(3-4)、含硅三氯氧钒储罐(3-5)、精馏段酸封罐(3-6)、高纯三氯氧钒冷凝器(3-7)和高纯三氯氧钒储罐(3-8);所述气相铵化流化床(4)包括铵化床空气净化器(4-1)、铵化床气体加热器(4-2)、三氯氧钒喷嘴(4-3)、气相铵化流化床主体(4-4)、铵化床旋风分离器(4-5)和铵化床排料器(4-6);所述偏钒酸铵加料装置(5)包括偏钒酸铵料仓(5-1)和偏钒酸铵螺旋加料器(5-2);所述煅烧流化床(6)包括煅烧床空气净化器(6-1)、煅烧床气体加热器(6-2)、煅烧床进料器(6-3)、煅烧流化床主体(6-4)、煅烧床旋风分离器(6-5)和高纯五氧化二钒料仓(6-6);所述工业级五氧化二钒料仓(1-1)底部的出料口与所述工业级五氧化二钒螺旋加料器(1-2)的进料口相连接;所述炭粉料仓(1-3)底部的出料口与所述炭粉螺旋加料器(1-4)的进料口相连接;所述工业级五氧化二钒螺旋加料器(1-2)的出料口、所述炭粉螺旋加料器(1-4)的出料口均与所述氯化床进料器(2-1)的进料口通过管道相连接;所述氯化床进料器(2-1)的排料口与所述氯化流化床主体(2-2)上部的进料口通过管道相连接;所述氯化床进料器(2-1)底部的进气口通过管道与氮气气源总管相连接;所述氯化床旋风分离器(2-3)设置于所述氯化流化床主体(2-2)的扩大段顶部中心;所述氯化床旋风分离器(2-3)顶部的出气口通过管道与所述烟气换热器(2-4)的热烟气入口相连接;所述烟气换热器(2-4)的冷烟气出 口通过管道与所述烟气冷凝器(2-5)的气体入口相连接;所述烟气冷凝器(2-5)的气体出口通过管道与所述氯化床酸封罐(2-6)的气体入口相连接;所述氯化床酸封罐(2-6)的气体出口通过管道与所述尾气淋洗吸收器(7)的气体入口相连接;所述氯化流化床主体(2-2)下部的排渣口与所述氯化床螺旋排渣器(2-7)的进料口通过管道相连接;所述氯化流化床主体(2-2)底部的进气口通过管道与所述烟气换热器(2-4)的热气体出口相连接;所述烟气换热器(2-4)的冷气体入口通过管道分别与氯气气源总管、氮气气源总管及压缩空气总管相连接;所述烟气冷凝器(2-5)底部的液体出口通过管道与所述精馏塔(3-2)的进料口相连接;所述蒸馏釜(3-1)的蒸气出口通过管道与所述精馏塔(3-2)的蒸气入口相连接;所述蒸馏釜(3-1)的回流口通过管道与所述精馏塔(3-2)底部的液体回流出口相连接;所述精馏塔(3-2)顶部的气体出口通过管道与所述馏出物冷凝器(3-3)的气体入口相连接;所述馏出物冷凝器(3-3)的液体出口通过管道与所述回流液收集罐(3-4)的液体入口相连接;所述回流液收集罐(3-4)的回流液体出口通过管道与所述精馏塔(3-2)顶部的回流液体入口相连接;所述回流液收集罐(3-4)的排料口与所述含硅三氯氧钒储罐(3-5)的入口通过管道相连接;所述含硅三氯氧钒储罐(3-5)的乏气出口通过管道与所述精馏段酸封罐(3-6)的气体入口相连接;所述精馏酸封罐(3-6)的气体出口通过管道与所述尾气淋洗吸收器(7)的气体入口相连接;所述精馏塔(3-2)的精馏物出口通过管道与所述高纯三氯氧钒冷凝器(3-7)的气体入口相连接;所述高纯三氯氧钒冷凝器(3-7)的液体出口与所述高纯三氯氧钒储罐(3-8)的液体入口通过管道相连接;所述蒸馏釜(3-1)底部设置了底流出口;所述铵化床空气净化器(4-1)的进气口与压缩空气总管通过管道相连接;所述铵化床空气净化器(4-1)的出气口通过管道分别与所述铵化床气体加热器(4-2)的进气口、三氯氧钒喷嘴(4-3)的气体入口及铵化床排料器(4-6)底部的进气口相连接;所述铵化床气体加热器(4-2)的进气口通过管道与超纯水、纯化液氨总管相连接;所述铵化床气体加热器(4-2)燃烧嘴的助燃风入口和燃料入口分别通过管道与压缩空气总管和燃料总管相连接;所述铵化床气体加热器(4-2)的出气口通过管道与所述气相铵化流化床主体(4-4)底部的进气口相连接;所述高纯三氯氧钒储罐(3-8)的液体出口通过管道与所述三氯氧钒喷嘴(4-3)的三氯氧钒入口相连接;所述铵化床旋风分离器(4-5)设置于所述气相铵化流化床主体(4-4)扩大段顶部中心处;所述铵化床旋风分离器(4-5)的顶部出气 口通过管道与尾气处理单元相连接;所述气相铵化流化床主体(4-4)上部的排料口通过管道与所述铵化床排料器(4-6)的进料口相连接;所述铵化床排料器(4-6)的排料口通过管道与所述偏钒酸铵料仓(5-1)的进料口相连接;所述偏钒酸铵料仓(5-1)底部的出料口与所述偏钒酸铵螺旋加料器(5-2)的进料口相连接;所述偏钒酸铵螺旋加料器(5-2)的排料口通过管道与所述煅烧床进料器(6-3)的进料口通过管道相连接;所述煅烧床空气净化器(6-1)的进气口与压缩空气总管通过管道相连接;所述煅烧床空气净化器(6-1)的出气口通过管道分别与所述煅烧床气体加热器(6-2)的进气口和煅烧床进料器(6-3)底部的进气口相连接;所述煅烧床气体加热器(6-2)燃烧嘴的助燃风入口和燃料入口分别通过管道与压缩空气总管和燃料总管相连接;所述煅烧床气体加热器(6-2)的出气口通过管道与所述煅烧流化床主体(6-4)底部的进气口相连接;所述煅烧床进料器(6-3)的排料口通过管道与所述煅烧床流化床主体(6-4)下部的进料口相连接;所述煅烧流化床主体(6-4)顶部的出气口通过管道与所述煅烧床旋风分离器(6-5)的进气口相连接;所述煅烧床旋风分离器(6-5)底部的粉料出口通过管道与氯化铵料仓进料口相连接;所述煅烧床旋风分离器(6-5)的顶部出气口通过管道与尾气处理单元相连接;所述煅烧流化床主体(6-4)上部的排料口通过管道与所述高纯五氧化二钒料仓(6-6)的进料口相连接;所述尾气淋洗吸收器(7)的气体出口通过管道与所述引风机(8)的气体入口相连接;所述引风机(8)的气体出口通过管道与所述烟囱(9)底部的气体入口相连接。
- 一种基于权利要求1所述系统的提纯制备高纯五氧化二钒粉体的方法,包括以下步骤:所述工业级五氧化二钒料仓(1-1)中的工业级五氧化二钒粉料和所述炭粉料仓(1-3)的炭粉分别经所述工业级五氧化二钒螺旋加料器(1-2)和所述炭粉螺旋加料器(1-4)同时进入所述氯化床进料器(2-1)混合后进入所述氯化流化床主体(2-2);来自氯气气源总管的氯气、氮气气源总管的氮气及压缩空气总管的空气经所述烟气换热器(2-4)与氯化烟气换热预热后进入所述氯化流化床主体(2-2)中使五氧化二钒和炭粉维持流态化并与之发生化学反应,空气使部分炭粉发生燃烧提供热量维持流化床温度,氯气与炭粉共同作用使五氧化二钒和少量杂质发生氯化,形成氯化残渣和富含三氯氧钒的氯化烟气;氯化残渣依次经所 述氯化流化床主体(2-2)下部的排渣口和所述氯化床螺旋排渣器(2-7)排出;氯化烟气经所述氯化床旋风分离器(2-3)将粉尘脱除并落回氯化流化床主体(2-2)后,再经所述烟气换热器(2-4)预冷却并进入烟气冷凝器(2-5)中使其中的三氯氧钒冷凝形成粗三氯氧钒液体,剩余尾气经所述氯化床酸封罐(2-6)后进入所述尾气淋洗吸收器(7)中;所述烟气冷凝器(2-5)形成的粗三氯氧钒液体进入所述精馏塔(3-2)和所述蒸馏釜(3-1)后进行精馏操作,得到富含高沸点杂质的富钒废料、富含低沸点杂质的含硅三氯氧钒蒸气和高纯三氯氧钒蒸气;含硅三氯氧钒蒸气经所述馏出物冷凝器(3-3)冷凝至液体后,部分经回流液收集罐(3-4)回流至所述精馏塔(3-2),其余部分进入所述含硅三氯氧钒储罐(3-5)中;含硅三氯氧钒储罐(3-5)中产生的乏气经所述精馏段酸封罐(3-6)后送往所述尾气淋洗吸收器(7)中;高纯三氯氧钒蒸气经所述高纯三氯氧钒冷凝器(3-7)冷凝至液体后进入所述高纯三氯氧钒储罐(3-8)中;所述高纯三氯氧钒储罐(3-8)的高纯三氯氧钒经所述三氯氧钒喷嘴(4-3),由来自铵化床空气净化器(4-1)的净化空气气载进入所述气相铵化流化床主体(4-4)中;超纯水、纯化液氨和净化空气经所述铵化床气体加热器(4-2)预热后送入所述气相铵化流化床主体(4-4)中使床内粉料维持流态化,并使三氯氧钒发生水解和铵化,生成含氯化铵的偏钒酸铵粉体,所述含氯化铵的偏钒酸铵粉体经铵化床排料器(4-6)排出后进入所述偏钒酸铵料仓(5-1)中,产生的含氨的铵化烟气经铵化床旋风分离器(4-5)脱除粉尘后送尾气处理单元处理;所述偏钒酸铵料仓(5-1)中的含氯化铵的偏钒酸铵粉料依次经所述偏钒酸铵螺旋加料器(5-2)和煅烧床进料器(6-3)进入所述煅烧流化床主体(6-4)中;压缩空气依次经煅烧床空气净化器(6-1)净化和煅烧床气体加热器(6-2)预热后进入所述煅烧流化床主体(6-4)中使床内粉料维持流态化,并使含氯化铵的偏钒酸铵物料发生热分解,得到高纯五氧化二钒粉体产品,经所述煅烧流化床主体(6-4)上部的排料口进入所述高纯五氧化二钒料仓(6-6)中;煅烧分解产生的煅烧烟气进入所述煅烧床旋风分离器(6-5)降温析出氯化铵并脱除粉尘后送尾气处理单元处理;所述煅烧床旋风分离器(6-5)收集到的氯化铵粉料送往氯化铵料仓中;所述尾气淋洗吸收器(7)经碱溶液吸收处理后排出的气体经所述引风机(8)送入所述烟囱(9)后排空。
- 根据权利要求2所述的提纯制备高纯五氧化二钒粉体的方法,其特征在于,在所述氯化流化床主体(2-2)内,所述氯化过程炭粉添加量为工业级五氧化二钒粉料质量的10%~20%。
- 根据权利要求2所述的提纯制备高纯五氧化二钒粉体的方法,其特征在于,在所述氯化流化床主体(2-2)内,氯化操作温度为300~500℃,粉料的平均停留时间为30~80min。
- 根据权利要求2所述的提纯制备高纯五氧化二钒粉体的方法,其特征在于,在所述精馏塔(3-2)内,所述精馏操作精馏段的塔板数为5~10块,提馏段的塔板数为10~20块。
- 根据权利要求2所述的提纯制备高纯五氧化二钒粉体的方法,其特征在于,所述精馏操作的回流比为15~40。
- 根据权利要求2所述的提纯制备高纯五氧化二钒粉体的方法,其特征在于,在所述气相铵化流化床主体(4-4)内,通过高纯三氯氧钒气相铵化制备得到偏钒酸铵,所述气相铵化的操作温度为130~250℃,水蒸气与氨气的摩尔比为0.5~0.8,氨气与三氯氧钒的摩尔比为3.5~4.5。
- 根据权利要求2所述的提纯制备高纯五氧化二钒粉体的方法,其特征在于,在所述煅烧流化床主体(6-4)内,通过流态化煅烧实现含氯化铵的偏钒酸铵的热分解,所述煅烧操作温度为400~650℃,粉料的平均停留时间为60~180min。
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