CN108658090B - Method for preparing 13X type molecular sieve and high-silicon mordenite by extracting aluminum residue from fly ash through acid method and utilization method of fly ash - Google Patents
Method for preparing 13X type molecular sieve and high-silicon mordenite by extracting aluminum residue from fly ash through acid method and utilization method of fly ash Download PDFInfo
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- CN108658090B CN108658090B CN201710196375.3A CN201710196375A CN108658090B CN 108658090 B CN108658090 B CN 108658090B CN 201710196375 A CN201710196375 A CN 201710196375A CN 108658090 B CN108658090 B CN 108658090B
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- fly ash
- filtrate
- molecular sieve
- residue
- aluminum
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- 238000000034 method Methods 0.000 title claims abstract description 194
- 239000010881 fly ash Substances 0.000 title claims abstract description 175
- 239000002808 molecular sieve Substances 0.000 title claims abstract description 154
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 title claims abstract description 154
- 229910052710 silicon Inorganic materials 0.000 title claims abstract description 113
- 239000010703 silicon Substances 0.000 title claims abstract description 102
- 229910052680 mordenite Inorganic materials 0.000 title claims abstract description 72
- 239000002253 acid Substances 0.000 title claims abstract description 33
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical group [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 title claims description 7
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 192
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 179
- 239000000706 filtrate Substances 0.000 claims abstract description 152
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 138
- 238000000605 extraction Methods 0.000 claims abstract description 126
- 229910001868 water Inorganic materials 0.000 claims abstract description 118
- 239000002893 slag Substances 0.000 claims abstract description 111
- QPILZZVXGUNELN-UHFFFAOYSA-N sodium;4-amino-5-hydroxynaphthalene-2,7-disulfonic acid Chemical compound [Na+].OS(=O)(=O)C1=CC(O)=C2C(N)=CC(S(O)(=O)=O)=CC2=C1 QPILZZVXGUNELN-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000005216 hydrothermal crystallization Methods 0.000 claims abstract description 67
- PUZPDOWCWNUUKD-UHFFFAOYSA-M sodium fluoride Chemical compound [F-].[Na+] PUZPDOWCWNUUKD-UHFFFAOYSA-M 0.000 claims abstract description 60
- 238000001914 filtration Methods 0.000 claims abstract description 53
- 239000011775 sodium fluoride Substances 0.000 claims abstract description 30
- 235000013024 sodium fluoride Nutrition 0.000 claims abstract description 30
- 238000004321 preservation Methods 0.000 claims abstract description 13
- 238000007654 immersion Methods 0.000 claims abstract description 9
- 239000000047 product Substances 0.000 claims description 114
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 97
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 63
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 57
- 239000007787 solid Substances 0.000 claims description 57
- 238000002386 leaching Methods 0.000 claims description 50
- 238000005406 washing Methods 0.000 claims description 44
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 42
- 229910052593 corundum Inorganic materials 0.000 claims description 41
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 41
- 239000007788 liquid Substances 0.000 claims description 40
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 35
- 238000001035 drying Methods 0.000 claims description 33
- 238000004064 recycling Methods 0.000 claims description 30
- 239000000413 hydrolysate Substances 0.000 claims description 29
- 238000002156 mixing Methods 0.000 claims description 24
- 230000008569 process Effects 0.000 claims description 20
- 229910052742 iron Inorganic materials 0.000 claims description 18
- 238000003786 synthesis reaction Methods 0.000 claims description 16
- 230000015572 biosynthetic process Effects 0.000 claims description 13
- 239000013078 crystal Substances 0.000 claims description 13
- 238000000227 grinding Methods 0.000 claims description 12
- 238000007865 diluting Methods 0.000 claims description 11
- 230000007062 hydrolysis Effects 0.000 claims description 10
- 238000006460 hydrolysis reaction Methods 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 239000003513 alkali Substances 0.000 claims description 9
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims 1
- 230000029087 digestion Effects 0.000 abstract description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 72
- 239000000243 solution Substances 0.000 description 54
- 239000000203 mixture Substances 0.000 description 50
- 239000011734 sodium Substances 0.000 description 41
- 238000002441 X-ray diffraction Methods 0.000 description 39
- 239000000377 silicon dioxide Substances 0.000 description 36
- 229910001483 soda nepheline Inorganic materials 0.000 description 35
- 229910052681 coesite Inorganic materials 0.000 description 31
- 229910052906 cristobalite Inorganic materials 0.000 description 31
- 229910052682 stishovite Inorganic materials 0.000 description 31
- 229910052905 tridymite Inorganic materials 0.000 description 31
- 239000000126 substance Substances 0.000 description 26
- KKCBUQHMOMHUOY-UHFFFAOYSA-N Na2O Inorganic materials [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 24
- 229910020489 SiO3 Inorganic materials 0.000 description 24
- 230000002194 synthesizing effect Effects 0.000 description 21
- 239000008367 deionised water Substances 0.000 description 18
- 229910021641 deionized water Inorganic materials 0.000 description 18
- 239000000843 powder Substances 0.000 description 18
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 17
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 description 17
- 229910052911 sodium silicate Inorganic materials 0.000 description 16
- 238000003756 stirring Methods 0.000 description 16
- 239000012452 mother liquor Substances 0.000 description 12
- 238000002360 preparation method Methods 0.000 description 12
- 238000007885 magnetic separation Methods 0.000 description 11
- 238000000967 suction filtration Methods 0.000 description 11
- 238000001816 cooling Methods 0.000 description 10
- 238000009775 high-speed stirring Methods 0.000 description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 description 9
- 239000002994 raw material Substances 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 8
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 8
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000003763 carbonization Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000010790 dilution Methods 0.000 description 6
- 239000012895 dilution Substances 0.000 description 6
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 6
- 239000004115 Sodium Silicate Substances 0.000 description 5
- 229910021536 Zeolite Inorganic materials 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- 239000003245 coal Substances 0.000 description 5
- 229910052863 mullite Inorganic materials 0.000 description 5
- 235000012239 silicon dioxide Nutrition 0.000 description 5
- 239000010457 zeolite Substances 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- 239000004411 aluminium Substances 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 238000001027 hydrothermal synthesis Methods 0.000 description 4
- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 235000010755 mineral Nutrition 0.000 description 4
- 239000011707 mineral Substances 0.000 description 4
- 239000010453 quartz Substances 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- 239000010117 shenhua Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 238000004611 spectroscopical analysis Methods 0.000 description 4
- 238000001228 spectrum Methods 0.000 description 4
- 239000005995 Aluminium silicate Substances 0.000 description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 235000012211 aluminium silicate Nutrition 0.000 description 3
- 229910000323 aluminium silicate Inorganic materials 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 238000004090 dissolution Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 3
- 230000020477 pH reduction Effects 0.000 description 3
- 235000019353 potassium silicate Nutrition 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000010802 sludge Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 235000019795 sodium metasilicate Nutrition 0.000 description 3
- 239000012265 solid product Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- ROSDSFDQCJNGOL-UHFFFAOYSA-N Dimethylamine Chemical compound CNC ROSDSFDQCJNGOL-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 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 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 2
- 229910001570 bauxite Inorganic materials 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 238000010000 carbonizing Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000002149 energy-dispersive X-ray emission spectroscopy Methods 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 229910001388 sodium aluminate Inorganic materials 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 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
- OPIFSICVWOWJMJ-HAAGFXOZSA-N 5-bromo-4-chloro-3-indolyl alpha-D-mannoside Chemical compound O[C@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1OC1=CNC2=CC=C(Br)C(Cl)=C12 OPIFSICVWOWJMJ-HAAGFXOZSA-N 0.000 description 1
- 229910018125 Al-Si Inorganic materials 0.000 description 1
- 229910018520 Al—Si Inorganic materials 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- LZZYPRNAOMGNLH-UHFFFAOYSA-M Cetrimonium bromide Chemical compound [Br-].CCCCCCCCCCCCCCCC[N+](C)(C)C LZZYPRNAOMGNLH-UHFFFAOYSA-M 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 241000668854 Howardia biclavis Species 0.000 description 1
- 108010009736 Protein Hydrolysates Proteins 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 150000004645 aluminates Chemical class 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 159000000013 aluminium salts Chemical class 0.000 description 1
- 229910000329 aluminium sulfate Inorganic materials 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 229910021417 amorphous silicon Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- -1 firstly Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910001389 inorganic alkali salt Inorganic materials 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 150000007522 mineralic acids Chemical class 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- PHIQPXBZDGYJOG-UHFFFAOYSA-N sodium silicate nonahydrate Chemical compound O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-][Si]([O-])=O PHIQPXBZDGYJOG-UHFFFAOYSA-N 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
- C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
- C01B39/20—Faujasite type, e.g. type X or Y
- C01B39/22—Type X
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
- C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
- C01B39/26—Mordenite type
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/20—Preparation of aluminium oxide or hydroxide from aluminous ores using acids or salts
- C01F7/22—Preparation of aluminium oxide or hydroxide from aluminous ores using acids or salts with halides or halogen acids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2002/00—Crystal-structural characteristics
- C01P2002/70—Crystal-structural characteristics defined by measured X-ray, neutron or electron diffraction data
- C01P2002/72—Crystal-structural characteristics defined by measured X-ray, neutron or electron diffraction data by d-values or two theta-values, e.g. as X-ray diagram
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Organic Chemistry (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Geochemistry & Mineralogy (AREA)
- Silicates, Zeolites, And Molecular Sieves (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to the field of utilization of fly ash acid method aluminum extraction residues and fly ash, and discloses a method for preparing a 13X-type molecular sieve and high-silicon mordenite by using the fly ash acid method aluminum extraction residues and a utilization method of the fly ash. The method comprises the following steps: (1) carrying out alkaline roasting on the residue of the acid-method aluminum extraction of the fly ash to obtain roasted slag; sequentially carrying out high-temperature water immersion and heat preservation filtration on the roasted slag charge to obtain a first filtrate; (2) carrying out 13X type molecular sieve hydrothermal crystallization on the first filtrate to obtain a 13X type molecular sieve and a molecular sieve filtrate; (3) and carrying out hydrothermal crystallization on the molecular sieve filtrate and sodium fluoride to obtain high-silicon mordenite and a second filtrate. The method realizes the digestion of the residue of aluminum extraction by the acid method of fly ash, improves the utilization rate of the residue of aluminum extraction by the acid method of fly ash, and utilizes fly ash.
Description
Technical Field
The invention relates to the field of utilization of aluminum residue extracted by a fly ash acid method and fly ash, in particular to a method for preparing a 13X-type molecular sieve and high-silicon mordenite by extracting aluminum residue by a fly ash acid method and a utilization method of fly ash.
Background
The high-alumina fly ash is a novel aluminum resource peculiar to China, and the amount of prospect resources of the high-alumina fly ash is about 100 million tons of alumina. The bauxite resource reserves found in China are only 32 hundred million tons, the resource guarantee years are only about 20 years according to the estimation of the current mining scale, and the current external dependence of aluminum resources is as high as 55 percent. Therefore, the development and utilization of the high-alumina fly ash have practical significance for relieving the shortage of bauxite resources in China, ensuring the safety of the aluminum industry in China and enhancing the sustainable development capability of the aluminum industry.
The currently developed fly ash aluminum extraction process can be roughly divided into three major types, namely an acid method, an alkaline method and an acid-base combination method, and can produce qualified alumina products, but the process faces the problems of large emission amount of aluminum extraction residues and incapability of being effectively consumed to different degrees. Taking Shenhua group 'combined impurity removal one-step acid dissolution' process for extracting aluminum oxide as an example, each 100 tons of Al is produced2O3About 130 tons of aluminum extraction residue will be discharged. The residue discharge rate of the alkaline aluminum extraction process is higher. According to the relevant regulations of aluminum industry admission conditions issued by the Ministry of industry and belief in 2013, the comprehensive utilization rate of solid wastes of a newly-built system for producing alumina by using high-alumina fly ash is required to reach more than 96%. Therefore, the development of high-value and high-efficiency digestion technology for the residue of extracting aluminum from fly ash is urgently needed.
One of the obvious features of the residue after extracting aluminium from fly ash is rich in silicon (calcium) and poor in aluminium. At present, the utilization of the fly ash aluminum extraction residue mainly focuses on the preparation of silicon products (water glass, white carbon black, silicon micropowder and the like), the manufacture of basic building materials (cement, ceramic tiles, autoclaved bricks and the like), and the production of heat preservation, refractory materials and other fields. The application directions all have contradictions among the economic added value of products, the market capacity and the utilization rate of residues to different degrees, so that the overall utilization rate of the existing aluminum extraction residues from the fly ash is low, and the application and popularization of the high-alumina fly ash aluminum extraction technology are directly limited.
Molecular sieves are a class of materials having a uniform microporous structure. Due to the advantages of high adsorption capacity, strong thermal stability and the like which are not possessed by other adsorbents, the molecular sieve is important and widely applied to various application occasions such as catalysis, adsorption separation, ion exchange and the like.
The 13X type is a common molecular sieve, has the aperture of 1.0nm, can adsorb any molecule with the diameter of 0.364 nm-1.0 nm, can be used for catalyst co-carrier, co-adsorption of water and carbon dioxide and co-adsorption of water and hydrogen sulfide gas, is mainly applied to drying of medicine and air compression systems, and has the market price of more than 1 ten thousand yuan/ton. The ZSM-5 molecular sieve is a high-silicon molecular sieve with a special cross pore channel structure, has the pore channel diameter of about 0.5nm, has good thermal stability, hydrothermal stability and shape-selective catalytic efficiency, and is widely applied to the fields of petrochemical industry and the like at present.
Mordenite (Mordenite) is another commonly used aluminosilicate molecular sieve, which has a large number of five-membered ring structures and is connected in parallel in pairs, main channels are straight cylindrical twelve-membered rings, the cross section of each hole is oval, and the size of each hole is 0.65nm multiplied by 0.68 nm. The conventional mordenite has a silicon-aluminum ratio of 9-11 and has a chemical formula of Na [ Al [ [ Al ]8Si40O96]·24H2And O. The mordenite with higher silica-alumina ratio (more than 17) is called high-silica mordenite, and when the mordenite is used in the petrochemical fields of alkylation, alkane isomerization, hydrocracking, modification, dewaxing, dimethylamine synthesis reaction and the like, the catalytic activity, selectivity and thermal stability of the mordenite are obviously improved compared with those of the conventional MOR type molecular sieve, and the application prospect is wide.
The industrial synthesis of zeolite molecular sieves usually uses chemical raw materials such as water glass, sodium aluminate or aluminum hydroxide, and the cost is relatively high. Many researchers have conducted research on hydrothermal synthesis of molecular sieves from the same type of raw materials (including fly ash, coal gangue, kaolin, etc.).
CN101734683A discloses a method for preparing a 13X molecular sieve by using a high-alumina fly ash desilication liquid as a silicon source, which comprises the following steps: adding aluminum source such as aluminum sulfate or aluminum chloride into the desiliconized solution to form SiO2/Al2O3＝3～5，Na2O/SiO2＝1.0～1.5，H2O/Na2And aging and crystallizing under a system of 35-60O to synthesize the 13X molecular sieve with high crystallinity. The method needs additional aluminum source and does not completely and efficiently consume the fly ash.
Experimental research on synthesis of 13X zeolite molecular sieve from fly ash (chapter xi huan, china pilot plant of non-metal mining, phase 2 in 2003, 13x.23-35) uses fly ash as raw material, and is prepared by adding alkali to roast, adding a certain proportion of sodium silicate to adjust silica-alumina ratio, adding preformed amorphous 13X seed crystal, and adding a certain amount of sodium hydroxide and water to perform hydrothermal crystallization, thereby synthesizing 13X molecular sieve containing partial amorphous. The method utilizes the fly ash as a raw material, does not completely and efficiently consume the fly ash,
in the research on the preparation of 13X type zeolite molecular sieve from tailings of fly ash after calcium and iron extraction (Wangminghua, materials and metallurgy reports, No. 14, No. 1, 3 months in 2015, 13X.58-61), acid sludge obtained by removing iron and calcium by a fly ash acid method is used as a raw material, firstly, alkali is added for roasting, water is added for dissolution, then, a guiding agent and a template agent (CTAB) are added into slurry, and the 13X type zeolite molecular sieve is synthesized by hydrothermal crystallization for 20 hours at 100 ℃, wherein obvious amorphous silicon and aluminum exist. The method uses acid sludge obtained by removing iron and calcium by a fly ash acid method as a raw material, only can produce 13X type molecular sieve, generates waste materials, and cannot completely remove silicon and aluminum in the acid sludge obtained by removing iron and calcium by the fly ash acid method.
CN1230518A discloses a method for synthesizing high-silicon mordenite, SiO thereof2/Al2O3The molecular ratio is 15-30, water glass, inorganic acid, inorganic alkali and aluminium salt or aluminate are used as raw materials, and the molecular ratio in the reaction mixture is Na2O/Al2O3＝1-10；SiO2/Al2O3＝10-30；H2O/Al2O3200-.
CN101804995A discloses a method for preparing high-silicon mordenite by using mineral raw materials, which is characterized by comprising the following steps: 1) according to SiO in the silicon source2Al in the aluminum source2O3Inorganic alkali, fluoride, template agent: h2The molar ratio of O is (20 to 50):1, (2 to 5): 5 to 10): (1.5-6) 300-600), selecting an aluminum source, a silicon source, inorganic alkali, fluoride, a template agent and water; the aluminum source is coal gangue or kaolin; the silicon source is any one or mixture of more than two of kaolin, coal gangue, sodium metasilicate nonahydrate, activated silica powder and silica sol, and the mixture ratio of any two or more is arbitrary; 2) mixing a silicon source, an aluminum source, inorganic alkali, fluoride, a template agent and water, pulping, stirring and mixing at room temperature to 80 ℃ to form gel, and obtaining an initial gel mixture; adjusting the pH value of the initial gel mixture to 11-13, and performing hydrothermal crystallization synthesis reaction in a reaction kettle, wherein the hydrothermal crystallization synthesis reaction is performed under the condition of crystallization at 160-180 ℃ for 48-70 hours to obtain a crystallization product; and filtering and washing the crystallized product until the pH value is 7-8, drying, roasting at 500 ℃ for 5-10h, and demolding to obtain the high-silicon mordenite (the silica-alumina ratio is 12-20).
In the prior art, one of aluminum and silicon in the fly ash acid method aluminum extraction residue is excessive and needs to be prepared by adding a silicon source or an aluminum source, but the method is not favorable for efficiently dissolving the fly ash acid method aluminum extraction residue.
Therefore, the existing technology for preparing the molecular sieve by using the fly ash acid method aluminum extraction residue to realize the consumption of the fly ash acid method aluminum extraction residue cannot meet the requirement of fully utilizing the silicon and aluminum in the fly ash acid method aluminum extraction residue, and a method for more effectively preparing the molecular sieve by using the fly ash acid method aluminum extraction residue and realizing the high-efficiency consumption of the fly ash acid method aluminum extraction residue is needed.
Disclosure of Invention
The invention aims to solve the problems of how to improve the consumption efficiency of the acidified aluminum extraction residue of the fly ash by preparing a molecular sieve, co-producing high-silicon type and low-silicon type molecular sieves and how to utilize the fly ash, and provides a method for preparing a 13X type molecular sieve and high-silicon mordenite by extracting the aluminum extraction residue of the fly ash by an acid method and a utilization method of the fly ash.
The inventor of the invention finds in research that the material composition of the residue of aluminum extraction by the acid method of fly ash has specificity compared with fly ash: the silicon content is more enriched than that of common fly ash, the aluminum content is obviously reduced, and acid soluble elements such as Fe, Mg and the like are extracted from the fly ash in the process of extracting aluminum by an acid methodIs largely removed, wherein SiO2With Al2O3Molar ratio (which can be expressed as silicon to aluminum ratio, or SiO)2/Al2O3) About 10: 1. the mole ratio of silicon to aluminum in the fly ash acid method aluminum extraction residue can not be completely matched with a high-silicon molecular sieve and a low-silicon molecular sieve, if the fly ash acid method aluminum extraction residue is directly used for synthesizing a low-silicon molecular sieve (such as a 13X type molecular sieve, the silicon to aluminum ratio is about 2-3), the Si is obviously excessive, and an aluminum source needs to be added; when the Al-Si-Al-Si zeolite is used for synthesizing high-silicon molecular sieve (such as high-silicon mordenite with Si/Al ratio greater than 18), Al element is excessive, and a silicon source is required to be added. Obviously, an external aluminum source or silicon source is introduced, other resources are additionally consumed, and the utilization rate of the residue obtained by acidifying the fly ash and extracting aluminum cannot be effectively improved. On the other hand, in the acidified aluminum extraction residue of the fly ash, low-activity components such as mullite, quartz, anatase and the like are further enriched compared with the original fly ash, so that the utilization rate of the acidified aluminum extraction residue of the fly ash is restricted to be improved. Therefore, how to reasonably and better utilize silicon and aluminum resources in the fly ash acidification aluminum extraction residue needs not to add silicon or aluminum, and the factors need to be comprehensively considered. The inventor provides the invention to improve the consumption efficiency of the fly ash acidification aluminum extraction residue, realize the high-efficiency consumption of the fly ash acidification aluminum extraction residue and realize the joint production of the 13X-type molecular sieve and the high-silicon mordenite.
In order to achieve the purpose, the invention provides a method for preparing a 13X-type molecular sieve and high-silicon mordenite by extracting aluminum residues from fly ash by an acid method, which comprises the following steps:
(1) carrying out alkaline roasting on the residue of the acid-method aluminum extraction of the fly ash to obtain roasted slag; sequentially carrying out high-temperature water immersion and heat preservation filtration on the roasted slag charge to obtain a first filtrate;
(2) carrying out 13X type molecular sieve hydrothermal crystallization on the first filtrate to obtain a 13X type molecular sieve and a molecular sieve filtrate;
(3) and carrying out hydrothermal crystallization on the molecular sieve filtrate and sodium fluoride to obtain high-silicon mordenite and a second filtrate.
The invention also provides a utilization method of the fly ash, which comprises the following steps: carrying out acid method aluminum extraction on the fly ash to obtain fly ash acid method aluminum extraction residue and aluminum oxide; the 13X-type molecular sieve and the high-silicon mordenite are prepared from the residue of the acid-method aluminum extraction of the fly ash by the method.
Through the technical scheme, the method can better utilize silicon and aluminum resources in the fly ash acid method aluminum extraction residue, realizes effective consumption of the fly ash acid method aluminum extraction residue, and generates considerable environmental benefits; meanwhile, high-value and efficient resource utilization of the residue generated in the aluminum extraction by the fly ash acid method is realized.
The utilization method of the fly ash acid method aluminum extraction residue provided by the invention can utilize silicon and aluminum in the fly ash acid method to produce molecular sieve products without separating and extracting part of silicon, and can omit the operation of extraction and separation. In addition, the method provided by the invention can fully and efficiently consume the residue of aluminum extraction by the acid method of fly ash without additionally introducing an external aluminum source.
In order to realize better utilization of the fly ash acid method aluminum extraction residue, the method of the invention particularly limits the synthesis of the molecular sieve with low silica-alumina ratio, can obtain the 13X type molecular sieve, and can adjust the silica-alumina ratio in the filtrate generated by warping and synthesizing the 13X type molecular sieve, thereby being suitable for synthesizing the high silica-alumina ratio high silica mordenite, and fully utilizing the silica and alumina resources in the fly ash acid method aluminum extraction residue. The invention skillfully utilizes the fly ash acid method aluminum extraction residue to synthesize the molecular sieve for multiple times, and limits that the low silicon-aluminum ratio molecular sieve is synthesized firstly and then the high silicon-aluminum ratio molecular sieve is synthesized, thereby realizing the purposes of efficiently dissolving the fly ash acid method aluminum extraction residue and producing high value-added products.
The method provided by the invention can also utilize the fly ash to produce alumina, 13X-type molecular sieve and high-silicon mordenite, so that the fly ash is fully utilized and no waste residue is discharged.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
FIG. 1 is a flow chart of a method provided by the present invention;
FIG. 2 is an XRD spectrum of a 13X type molecular sieve prepared by the present invention;
FIG. 3 is an XRD spectrum of the high-silicon mordenite prepared by the present invention.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The first purpose of the invention is to provide a method for preparing 13X type molecular sieve and high-silicon mordenite by extracting aluminum residue from fly ash by an acid method, as shown in figure 1, comprising the following steps:
(1) carrying out alkaline roasting on the residue of the acid-method aluminum extraction of the fly ash to obtain roasted slag; sequentially carrying out high-temperature water immersion and heat preservation filtration on the roasted slag charge to obtain a first filtrate;
(2) carrying out 13X type molecular sieve hydrothermal crystallization on the first filtrate to obtain a 13X type molecular sieve and a molecular sieve filtrate;
(3) and carrying out hydrothermal crystallization on the molecular sieve filtrate and sodium fluoride to obtain high-silicon mordenite and a second filtrate.
In the invention, the residue of extracting aluminum from fly ash by acid method mainly comprises: SiO 22、Al2O3And TiO2，SiO2About 70 to 80 wt%, Al2O3In an amount of about 10 to 15 wt% and TiO2Is present in an amount of about 3 to 8 wt%. Such as Shenhua inner Mongolia quasi-Geer fly ash acid aluminum extraction residueIn, SiO2Is about 78.7 wt%, Al2O3In an amount of about 13.4% by weight and TiO2Is present in an amount of about 5.2 wt%. Further XRD analysis of the residue from acid extraction of aluminum from fly ash shows that Al is present2O3Substantially of mullite (3 Al)2O3·SiO2) In the form of TiO2The carrier is anatase and rutile; about 85% of the Si is present in amorphous form, the remainder being present in mullite and quartz. The low-activity components such as mullite, quartz, anatase and the like are further enriched compared with the original fly ash, and the activity of silicon and aluminum elements is poor, so that the utilization of the residue of extracting aluminum by acidifying the fly ash is not facilitated to produce the molecular sieve.
According to the invention, the step (1) is used for treating the fly ash acid method aluminum extraction residue, so that silicon and aluminum elements in the fly ash acid method aluminum extraction residue can be activated and can participate in the synthesis and utilization of the molecular sieve more effectively, and the content of the silicon and aluminum elements in the obtained first filtrate can be reasonably adjusted to meet the requirement of reaction raw materials for synthesizing the molecular sieve with low silicon-aluminum ratio. In the step (1), the alkaline roasting aims at fully decomposing mineral components with stable crystal structures, such as mullite, quartz and the like, at a lower roasting temperature so as to fully activate Si and Al elements in the mineral components. The activation of Si and Al elements can be realized by adding alkaline substances into the acidified aluminum extraction residues of the fly ash and roasting the residues together. Preferably, in step (1), the alkali roasting process comprises: mixing and grinding 100 parts by weight of the fly ash acid-process aluminum extraction residue and 100-130 parts by weight of a sodium carbonate-containing material, roasting the obtained ground product at 830-890 ℃ for 60-120 min, and then crushing to below 200 meshes to obtain the roasted slag material.
In the invention, in the step (1), after the roasting is completed, the roasted product can be rapidly cooled by air, and the roasted slag charge is obtained by cooling.
In the present invention, the sodium carbonate-containing material may be sodium carbonate solid powder directly used, or part of the second filtrate obtained in step (3) may be recycled as shown in fig. 1. The main component in the second filtrate is sodium carbonate, and sodium carbonate solid obtained by evaporating and crystallizing part of the second filtrate can be utilized. The fly ash acid method aluminum extraction residue can also be mixed with the first filter residue obtained from the heat preservation and filtration for recycling.
According to the invention, in the step (1), the high-temperature water leaching can further leach silicon and aluminum elements in the roasted slag, and specifically can dissolve Na in the roasted slag out by water2SiO3And NaAlSiO4. Preferably, in step (1), the high-temperature water leaching process comprises: removing iron from the roasted slag, mixing the roasted slag with water, and performing water leaching to obtain a water leaching product; the water immersion temperature is 95-105 ℃, and the water immersion time is 15-20 min; the amount of water is 150-200 ml relative to 100g of the roasted slag charge. Wherein the iron removal of the roasted slag can be realized by adopting a dry magnetic separation mode. The high temperature water leaching process may be carried out at atmospheric or autogenous pressure. The water leaching product is a solid-liquid mixture, and the solid is Na dissolved out by leaching the roasted slag charge with water2SiO3And NaAlSiO4The remaining product, the mineral phase composition of which is amorphous aluminosilicate and a small amount of crystalline NaAlSiO4(ii) a The liquid is Na-containing2SiO3And NaAlSiO4The solution of (1).
According to the invention, in the step (1), the water leaching product is subjected to solid-liquid separation through heat preservation and filtration, and the first filtrate is obtained. Preferably, in step (1), the filtration process comprises: diluting, filtering and washing the water leaching product by using part of the second filtrate to obtain slurry, and filtering the slurry to obtain first filter residue and the first filtrate; the filtering temperature is kept between 60 and 80 ℃.
According to the invention, the dosage of the second filtrate is 250-350 ml relative to 100g of the roasting slag charge;
in a preferred embodiment of the present invention, when the three processes of the alkaline roasting, the high-temperature water leaching and the heat-preservation dilution filtering involve condition parameters within the above-defined ranges, the first filter residue can be obtained with a minimum yield (i.e. the ratio of the dry basis weight of the first filter residue to the dry basis weight of the fly ash acid-extraction aluminum residue). Therefore, the fly ash acid method aluminum extraction residue has the highest one-time consumption efficiency mu when no external silica-aluminum source is introduced. The one-time consumption efficiency mu of the fly ash acid method aluminum extraction residue can be calculated by the following formula:
μ＝[(M-M1)/(M+Mout)]×100％；
mu is the one-time consumption efficiency of the residue of aluminum extraction by the acid method of the fly ash;
m is the dry basis weight of the fly ash acid method aluminum extraction residue for alkaline roasting in the step (1);
M1the dry basis weight of the first filter residue obtained in the step (1);
Moutis the dry basis mass of the external silica-alumina source introduced into the whole reaction system.
In the invention, no external silicon-aluminum source is introduced, so Mout＝0。
The first time consumption efficiency mu and the first filter residue M1Mass and external silico-aluminium source MoutThe mass is in inverse proportional relation, and is in direct proportional relation with the final consumption efficiency of the fly ash acid method aluminum extraction residue.
In the invention, silicon and aluminum elements in the residue of aluminum extraction by the acid method of fly ash can be converted into active components by the alkali method roasting, high-temperature water leaching and heat-preservation filtering, and Na is used2SiO3And NaAlSiO4The form of (A) is extracted, and the ratio of silicon to aluminum is adjusted to adapt to the needs of subsequent molecular sieve synthesis. Preferably, SiO in the first filtrate2With Al2O3The molar ratio of (10-25): 1. preferably SiO in the first filtrate2With Al2O3The molar ratio of (12-20): 1; more preferably (12-15): 1.
in the present invention, the chemical composition (molar ratio) of the first filtrate may be controlled to SiO2:Al2O3:Na2O:CO3 2-:H2O＝(10～25):1:(13～20):(3.5～11):(340～430)。
When synthesizing a 13X-type molecular sieve of a low-silicon molecular sieve in the prior art, the silicon-aluminum ratio in a hydrothermal crystallization mother liquor is usually regulated and limited to (3-5): 1 or so; when synthesizing high-silicon molecular sieve high-silicon mordenite, the ratio of silicon to aluminum in the hydrothermal crystallization mother liquor is generally limited to 20:1 or more. The pure 13X type molecular sieve or high silicon mordenite can be more easily synthesized under the condition of the silica-alumina ratio of the mother liquor.
But the method provided by the invention is used for improving the consumption efficiency of the residue of aluminum extraction by the acid method of the fly ash. Aiming at the material properties of the residue after the aluminum extraction by the acid method of the fly ash, if a 13X-type molecular sieve or high-silicon mordenite is produced according to the conventional technology, an external aluminum source is required to be respectively added to reduce the silicon-aluminum ratio to (3-5): 1, or adding an external silicon source to increase the silicon-aluminum ratio to be more than 20: 1. And an external silicon, aluminum source (i.e., M)out) The introduction of the method directly causes the reduction of the once consumption efficiency mu of the fly ash acid method aluminum extraction residue, and further influences the overall consumption efficiency of the fly ash acid method aluminum extraction residue, namely the quality of the fly ash acid method aluminum extraction residue consumed for preparing a unit mass product is reduced.
In the second filtrate obtained in the present invention, the concentration of sodium carbonate may be 15 to 25% by weight. The second filtrate is used for diluting, filtering and washing the water leaching product, so that the concentration of a filtering system can be reduced, the hydrolysis of sodium metasilicate in the water leaching product can be inhibited, the filtering efficiency can be improved, the filtering loss can be reduced, the yield of first filter residue can be reduced, and the one-time consumption efficiency of the fly ash acid method aluminum extraction residue can be improved. Meanwhile, the recycling of the sodium carbonate in the system is realized. The filtration can adopt a suction filtration or a filter pressing mode.
According to the present invention, preferably, the method further comprises: and (2) drying the first filter residue and then recycling the first filter residue in the step (1), and adding the first filter residue into the fly ash acid-method aluminum extraction residue in the alkali-method roasting.
According to the invention, the first filtrate obtained in the step (1) is utilized in the step (2) to synthesize the 13X type molecular sieve. And the synthesis conditions enable the composition of silicon and aluminum elements in the molecular sieve filtrate obtained after synthesis to be suitable for further synthesizing the high-silicon mordenite. Preferably, in step (ii)(2) In (3), the process of hydrothermal crystallization of the 13X type molecular sieve comprises: a) adding water into the filtrate for hydrolysis to obtain a hydrolysate; the adding amount of water is such that the total volume of the hydrolysate is 850-1000 ml relative to 100g of the roasting slag charge; b) introducing CO into the hydrolysate2Carrying out carbonation to enable the pH of the hydrolysate to be 13-15; c) adding or not adding 13X type molecular sieve seed crystals into the product obtained in the step b), and then carrying out hydrothermal crystallization for 15-30 h at 90-110 ℃ to obtain a 13X type molecular sieve hydrothermal crystallization product; the dosage of the 13X-type molecular sieve seed crystal is 0-10 wt% of the roasting slag charge; d) filtering the 13X type molecular sieve hydrothermal crystallization product to obtain a second filter residue and the molecular sieve filtrate; and drying the second filter residue to obtain the 13X-type molecular sieve. In the above synthesis process, the 13X type molecular sieve seed crystal is a known substance and can be synthesized by a laboratory according to a conventional method, the synthesis method is known and is not described any more, and SiO thereof is not described any more2With Al2O3The molar ratio of (2-3): 1. the XRD spectrum of the finally obtained solid product can be determined by XRD (X-ray diffraction) method, as shown in fig. 2, and compared with the standard spectrum, it is confirmed that 13X type molecular sieve is obtained.
According to the invention, by limiting the hydrothermal crystallization conditions of the 13X type molecular sieve in the step (2), pure 13X type molecular sieve and molecular sieve filtrate with chemical composition suitable for hydrothermal crystallization of the high-silicon mordenite in the step (3) can be obtained. The content of silicon and aluminum in the molecular sieve filtrate generated in the step (2) is obviously changed compared with that in the first filtrate, and preferably SiO in the molecular sieve filtrate2With Al2O3The molar ratio of (35-45): 1, more preferably (40 to 45): 1. the chemical composition (molar ratio) of the molecular sieve filtrate can be SiO2:Al2O3:Na2O:CO3 2-:H2O＝(35～45):1:(65～90):(60～85):(1900～2300)。
According to the present invention, preferably, in step (3), the hydrothermal crystallization of the high-silicon mordenite comprises: i) adding sodium fluoride solid into the molecular sieve filtrate to obtain synthetic liquid; ii) to saidIntroducing CO into the synthetic liquid2Performing carbonation to ensure that the pH of the synthetic liquid is 11.0-11.4; iii) carrying out hydrothermal crystallization on the product obtained in the step ii) at the temperature of 140-190 ℃ for 15-48 h to obtain a high-silicon mordenite hydrothermal crystallization product; iv) filtering the high-silicon mordenite hydrothermal crystallization product to obtain a third filter residue and the second filtrate; and washing, drying and roasting the third filter residue to obtain the high-silicon mordenite. The solid finally obtained can be confirmed to be high-silicon mordenite by an XRD (X-ray diffraction) method, as shown in fig. 3.
According to the invention, preferably, the sodium fluoride is added in an amount of SiO in the synthetic liquid210 to 20mol% of the amount of the catalyst. The sodium fluoride solid is high-grade pure NaF with the purity of more than or equal to 99 weight percent, and can be purchased from Shanghai Hu test company as high-grade pure NaF (more than or equal to 99 percent).
According to the invention, the second filtrate can be further utilized, and preferably, a part of the second filtrate is recycled to the heat preservation and filtration process in the step (1); and (3) evaporating and crystallizing the other part of the second filtrate to obtain sodium carbonate, and recycling the sodium carbonate to the alkali roasting process in the step (1). Therefore, the residue of aluminum extraction by the acid method of fly ash can be completely utilized, and no waste is generated.
The second object of the invention is to provide a utilization method of fly ash, which comprises the following steps: carrying out acid method aluminum extraction on the fly ash to obtain fly ash acid method aluminum extraction residue and aluminum oxide; the 13X-type molecular sieve and the high-silicon mordenite are prepared from the residue of the acid-method aluminum extraction of the fly ash by the method.
Wherein the fly ash can be fine ash collected from flue gas discharged from coal fired power plants after coal combustion. May be mainly composed of SiO2、Al2O3And TiO2。SiO2About 20 to 40 wt%, Al2O3In an amount of about 45 to 60 wt% and TiO2Is present in an amount of about 1.5 to about 4.5 wt%. For example fly ash from the power plant of Shenhua inner Mongolian China, where SiO is present2Is about 32.43 wt%, Al2O3In an amount of about 50.42 wt% and TiO2Is present in an amount of about 2.14 wt%.
The acid method for extracting aluminum in the invention can adopt a method known in the art, and is not described in detail herein.
In the present invention, the silica-alumina ratio of the high-silica mordenite obtained is 26 or more, preferably 28.8 to 34.2.
The present invention will be described in detail below by way of examples.
In the following examples, the substance obtained was determined to be 13X type molecular sieve by XRD (X-ray diffraction) using an X-ray diffractometer model D8 ADVANCE of Bruker, Germany, under the condition of 40Kv-40mA, scanning (2 theta) at 4-75 DEG, and comparing the scanning result with a standard card No. 38-0284 (PDF2004 edition);
the X-ray diffractometer was used to scan (2. theta.) at 4-75 deg. by XRD (X-ray diffraction) using D8 ADVANCE model X-ray diffractometer from Bruker, Germany, under the condition of 40Kv-40 mA. Scanning results the material obtained was determined to be Mordenite by comparison with standard card 29-1257 (PDF2004 edition).
Through an SEM-EDS (scanning electron microscope with an energy spectrometer), X-man 50 type EDS of Oxford company in UK is adopted and matched with Navo NanoSEM 450 type SEM of FEI company in America, chemical component signals of a mordenite sample are collected under the voltage of 15Kv, and the silicon-aluminum ratio of the high-silicon mordenite is calculated.
The calculation method of the one-time consumption efficiency mu of the fly ash acid method aluminum extraction residue is as described above.
The fly ash comes from Shenhua inner Mongolian China power plant, the specific composition content is shown in Table 1,
TABLE 1
| Composition of | Al2O3 | SiO2 | P2O5 | SO3 | K2O | CaO | TiO2 | Fe2O3 | MgO | Na2O |
| Content by weight% | 50.42 | 32.43 | 0.19 | 4.0 | 0.37 | 3.03 | 2.14 | 1.71 | 0.18 | 0.03 |
The fly ash acid method aluminum extraction residue comes from an alumina plant of the Niger energy Limited liability company, and the specific composition content is shown in Table 2.
TABLE 2
| Composition of | Al2O3 | SiO2 | P2O5 | SO3 | K2O | CaO | TiO2 | Fe2O3 | ZrO2 | Na2O |
| Content by weight% | 13.4 | 78.7 | 0.14 | 0.35 | 0.16 | 0.37 | 5.2 | 0.45 | 0.29 | - |
Preparation example 1
This preparation illustrates the preparation of fly ash to obtain fly ash acid process aluminum extraction residue.
Adding 5mol/L hydrochloric acid solution into 100g of fly ash, stirring and reacting for 30min at 150 ℃, filtering and washing to obtain an aluminum-rich solution and fly ash aluminum extraction residues by an acid method.
The chemical components of the residue from the acid extraction of aluminum from fly ash are shown in table 2.
Preparation example 2
This preparation illustrates the preparation of seeds of type 13X molecular sieve.
Sodium silicate is used as a silicon source, sodium aluminate is used as an aluminum source, water is added to prepare a 13X type molecular sieve hydrothermal crystallization mother liquor, and the composition (molar ratio) of the hydrothermal crystallization mother liquor is SiO2:Al2O3:Na2O:H2O＝5:1:1.5:50。
And transferring the mother liquor into a hydrothermal reaction kettle, and standing for hydrothermal reaction for 20 hours at the temperature of 95 ℃.
And filtering, washing and drying the product after the reaction to obtain pure 13X type molecular sieve solid powder which is used as the 13X type molecular sieve seed crystal in the invention. .
The average particle size of the 13X type molecular sieve seed crystal is 1-3 mu m, and the silicon-aluminum ratio is 3.
Example 1
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO360g of solid powder, mixing and grinding the solid powder, roasting the mixture for 90min at 860 ℃, quickly cooling the mixture in air after roasting is finished, and crushing the mixture to be below 200 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for iron removal, 70g of the roasted slag is taken and added with 140ml of deionized water (the amount of water is 200ml relative to 100g of the roasted slag), water leaching is carried out for 20min at 100 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved out2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid isHas Na2SiO3And NaAlSiO4The solution of (1);
(3) taking 100g (equivalent to 70g of roasting slag) of all water-leached products under the high-speed stirring state, adding 100ml of sodium carbonate solution (the concentration is 15 weight percent for the second filtrate recycled from the step (6)) to dilute, carrying out suction filtration at the temperature of 60 ℃, adding 100ml of the sodium carbonate solution to wash (corresponding to 286ml of the total dosage of the second filtrate relative to 100g of roasting slag); adding a certain amount of hot water (about 80 ℃) for washing to obtain a first filtrate with the volume of 400ml for synthesizing the 13X type molecular sieve; drying the obtained first filter residue to obtain 5.90g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝12:1:18:9.5:430。
(4) Taking 120ml of the first filtrate (21.0 g of the first filtrate in terms of roasting slag), adding 50ml of deionized water for hydrolysis (the total volume of the hydrolysate is 714ml relative to 100g of the roasting slag); introducing carbon dioxide into the obtained hydrolysate under stirring to perform carbonation until the pH is 13.455; then carrying out hydrothermal crystallization on the hydrolysate subjected to carbonization for 15.5 hours at 95 ℃, and filtering the obtained hydrothermal crystallization product to obtain second filter residue and molecular sieve filtrate; further washing and drying the second filter residue, and carrying out XRD (X-ray diffraction) analysis on the obtained product to obtain a spectrogram shown in figure 2, comparing the spectrogram with a standard card, and determining the spectrogram as the 13X-type molecular sieve;
the chemical composition (molar ratio) of the molecular sieve filtrate is SiO2:Al2O3:Na2O:CO3 2-:H2O＝37.2:1:72.7:68.2:1910；
(5) Adding 1.4g NaF solid (GR grade purity, not less than 99.0%, Shanghai Hu test) into 100ml of the obtained molecular sieve filtrate to obtain a synthetic solution (the addition of NaF is about SiO in the synthetic solution)220mol% of);
introducing CO into the synthetic liquid under the stirring state2Carrying out carbonation until the pH is 11.05; then hydrothermal crystallization is carried out at the temperature of 180 DEG CFiltering the obtained hydrothermal crystallization product for 50 hours to obtain third filter residue and second filtrate; further washing, drying and roasting the third filter residue, and analyzing an obtained product by XRD to obtain a spectrogram shown in figure 3, comparing the spectrogram with a standard card, and determining the high-silicon mordenite; EDS analysis shows that the mordenite has a silicon-aluminum ratio of 33.6;
(6) mixing the second filtrate (Na as main component)2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
The one-time consumption efficiency mu of the residue of the aluminum extraction by the acid method of the fly ash is 88.2 percent; after the first filter residue is recycled, the overall consumption efficiency of the residue generated in the aluminum extraction by the fly ash acid method is considered to be approximately 100 percent; na (Na)2CO3、CO2And the recycling of NaF is realized.
Example 2
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO3Mixing and grinding 65g of solid powder, roasting at 890 ℃ for 60min, quickly cooling with air after roasting is finished, and crushing to be less than about 180 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for iron removal, 70g of the roasted slag is added with 105ml of deionized water (the amount of water is 150ml relative to 100g of the roasted slag), water leaching is carried out for 18min at 95 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved out2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1).
(3) Taking 100g (equivalent to 70g of roasting slag) of all water-leached products under the high-speed stirring state, adding 100ml of sodium carbonate solution (the concentration of the second filtrate recycled from the step (6) is 20 weight percent) into the water-leached products for dilution, keeping the temperature and carrying out suction filtration at 80 ℃, adding 100ml of the sodium carbonate solution for washing (corresponding to 286ml of the total dosage of the second filtrate relative to 100g of roasting slag), adding a certain amount of hot water (about 90 ℃) for washing to obtain a first filtrate with the volume of 400ml, and using the first filtrate for synthesizing the 13X-type molecular sieve; drying the obtained first filter residue to obtain 6.42g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝13.4:1:18:9.5:420。
(4) Adding 120ml (equivalent to 21.0g of roasted slag) of the first filtrate into 50ml of deionized water for hydrolysis (the total volume of hydrolysate is 857ml relative to 100g of roasted slag); introducing CO into the obtained hydrolysate under stirring2Carbonation to pH 13.59; then adding 0.2g of 13X type molecular sieve seed crystal (preparation example 2) into the hydrolysate after carbonization, performing hydrothermal crystallization at 110 ℃ for 20 hours, and filtering the obtained hydrothermal crystallization product to obtain second filter residue and molecular sieve filtrate; further washing and drying the second filter residue, and analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, and determining the obtained spectrogram as a 13X-type molecular sieve;
the chemical composition (molar ratio) of the molecular sieve filtrate is SiO2:Al2O3:Na2O:CO3 2-:H2O＝38.1:1:77.5:66:1960；
(5) To 100ml of the obtained molecular sieve filtrate, 1.05g of sodium fluoride solid was added to obtain a synthetic solution (the amount of sodium fluoride solid added was SiO in the synthetic solution)215 mol%) of;
introducing CO into the synthetic liquid under the stirring state2Carbonizing to pH 12.0; then carrying out hydrothermal crystallization for 72h at the temperature of 150 ℃, and filtering the obtained hydrothermal crystallization product to obtain third filter residue and second filtrate; further washing, drying and roasting the third filter residue, analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, determining the obtained product as the high-silicon mordenite, and analyzing by EDS (electronic discharge spectroscopy) to obtain the mordenite with the silicon-aluminum ratio of 33.4;
(6) mixing the second filtrate (the main component isNa2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
The one-time consumption efficiency mu of the residue of the aluminum extraction by the fly ash acid method is 87.16%; after the first filter residue is recycled, the overall consumption efficiency of the residue generated in the aluminum extraction by the fly ash acid method is considered to be approximately 100 percent; na (Na)2CO3、CO2And the recycling of NaF is realized.
Example 3
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO350g of solid powder, mixing and grinding the solid powder, roasting the mixture for 120min at 830 ℃, quickly cooling the mixture by air after roasting is finished, and crushing the mixture to be less than about 150 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for removing iron, 70g of the roasted slag is added with 130ml of deionized water (the amount of water is 186ml relative to 100g of the roasted slag) to be subjected to water leaching for 15min at 105 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) under the high-speed stirring state, 100g of water leaching products (which are 70g of roasted slag), 100ml of sodium carbonate solution (the concentration is 25 weight percent and is recycled from the second filtrate in the step (6)) is added into the water leaching products for dilution, and the solution is subjected to suction filtration at the temperature of 70 ℃; adding 100ml of near-saturated sodium carbonate solution for washing (equivalent to the total dosage of 286ml of the second filtrate relative to 100g of roasted slag), and adding a certain amount of hot water (about 70 ℃) for washing to obtain a first filtrate with the volume of 400ml for synthesizing the 13X-type molecular sieve; drying the obtained first filter residue to obtain 6.26g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
conversion of the first filtrateChemical composition (mol ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝14.6:1:21.4:11.3:361。
(4) Adding 120ml (equivalent to 18.0g of roasting slag) of the first filtrate into 50ml of deionized water for hydrolysis (the total volume of the hydrolysate is 960ml relative to 100g of roasting slag); introducing CO into the obtained hydrolysate under stirring2Carrying out carbonation until the pH is 12.96; then adding 0.45g of 13X type molecular sieve seed crystal (preparation example 2) into the hydrolysate after carbonization, performing hydrothermal crystallization at 95 ℃ for 18h, and filtering the obtained hydrothermal crystallization product to obtain second filter residue and molecular sieve filtrate; further washing and drying the second filter residue, and analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, and determining the obtained spectrogram as a 13X-type molecular sieve;
the chemical composition (molar ratio) of the molecular sieve filtrate is SiO2:Al2O3:Na2O:CO3 2-:H2O＝43.3:1:66:83:2035；
(5) 0.7g of sodium fluoride solid was added to 100ml of the obtained molecular sieve filtrate to obtain a synthetic solution (the amount of sodium fluoride solid added was SiO in the synthetic solution)210 mol% of);
introducing CO into the synthetic liquid under the stirring state2Carbonation to pH 13.838; then carrying out hydrothermal crystallization for 15h at the temperature of 190 ℃, and filtering the obtained hydrothermal crystallization product to obtain third filter residue and second filtrate; further washing, drying and roasting the third filter residue, and analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, and determining the obtained spectrogram as the high-silicon mordenite; EDS analysis shows that the mordenite has a silicon-aluminum ratio of 34.2;
(6) mixing the second filtrate (Na as main component)2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
One-time elimination of residue from acid extraction of aluminium from fly ashThe nano efficiency mu is 87.48 percent; after the first filter residue is recycled, the overall consumption efficiency of the residue generated in the aluminum extraction by the fly ash acid method is considered to be approximately 100 percent; na (Na)2CO3、CO2And the recycling of NaF is realized.
Example 4
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO3Mixing and grinding 65g of solid powder, roasting at 890 ℃ for 60min, quickly cooling with air after roasting is finished, and crushing to be less than about 180 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation and iron removal, 70g of the roasted slag is added with 105ml of deionized water to be subjected to water leaching for 18min at 95 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) taking 100g (equivalent to 70g of roasting slag) of all water-leached products under the high-speed stirring state, adding 100ml of sodium carbonate solution (recycled from the second filtrate in the step (6) with the concentration of 20 weight percent) into the water-leached products for dilution, carrying out suction filtration at the temperature of 80 ℃, and adding 100ml of the sodium carbonate solution for washing; the total amount of the second filtrate used was 286ml relative to 100g of the roasted slag); adding a certain amount of hot water (about 90 ℃) for washing to obtain a first filtrate with the volume of 400ml for synthesizing the 13X type molecular sieve; drying the obtained first filter residue to obtain 6.60g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝13.6:1:17.8:9.75:426。
(4) Taking 120ml of the first filtrate (containing 21.0g of roasting slag), adding 80ml of deionized water for hydrolysis (the total volume of the hydrolysate is 952ml relative to 100g of roasting slag); introducing CO into the obtained hydrolysate under stirring2Carbonation to pH 13.59; then mixing the carbonAdding 0.2g of 13X type molecular sieve seed crystal (preparation example 2) into the separated hydrolysate, performing hydrothermal crystallization at 110 ℃ for 20 hours, and filtering the obtained hydrothermal crystallization product to obtain second filter residue and molecular sieve filtrate; further washing and drying the second filter residue, and analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, and determining the obtained spectrogram as a 13X-type molecular sieve;
the chemical composition (molar ratio) of the molecular sieve filtrate is SiO2:Al2O3:Na2O:CO3 2-:H2O＝40.4:1:89.7:72:2235；
(5) To 100ml of the obtained molecular sieve filtrate, 1.05g of NaF solid was added to obtain a synthetic solution (the amount of NaF added was about SiO in the synthetic solution)215 mol%) of;
introducing CO into the synthetic liquid under the stirring state2Carrying out carbonation until the pH is 11.05; then carrying out hydrothermal crystallization for 36 hours at 180 ℃, and filtering the obtained hydrothermal crystallization product to obtain third filter residue and second filtrate; further washing, drying and roasting the third filter residue, analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, determining the obtained product as high-silicon mordenite, determining the obtained product as mordenite, and analyzing the obtained product by EDS (electronic Desorption system) to obtain the mordenite with the silicon-aluminum ratio of 32.5;
(6) mixing the second filtrate (Na as main component)2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
The one-time consumption efficiency mu of the residue of the aluminum extraction by the fly ash acid method is 86.80%; after the first filter residue is recycled, the overall consumption efficiency of the residue generated in the aluminum extraction by the fly ash acid method is considered to be approximately 100 percent; na (Na)2CO3、CO2And the recycling of NaF is realized.
Example 5
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO360g of solid powder, mixing and grinding, roasting at 860 ℃ for 90min, and quickly emptying after roastingCooling and crushing to below 200 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for removing iron, 70g of the roasted slag is added into 140ml of deionized water to be subjected to water leaching for 20min at 100 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) taking 100g (equivalent to 70g of roasting slag) of all water-leached products under the high-speed stirring state, adding 100ml of sodium carbonate solution (the concentration is 25 weight percent for the second filtrate recycled from the step (6)) to dilute, carrying out suction filtration at the temperature of 60 ℃, adding 100ml of the sodium carbonate solution to wash (corresponding to 286ml of the total dosage of the second filtrate relative to 100g of roasting slag); adding a certain amount of hot water (about 80 ℃) for washing to obtain a first filtrate with the volume of 400ml for synthesizing the 13X type molecular sieve; drying the obtained first filter residue to obtain 6.11g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝12.5:1:17.5:9.2:428。
(4) Adding 120ml (equivalent to 21.0g of roasting slag) of the first filtrate into 60ml of deionized water for hydrolysis (the total volume of hydrolysate is 857ml relative to 100g of roasting slag); introducing carbon dioxide into the obtained hydrolysate under stirring to perform carbonation until the pH is 13.455; then carrying out hydrothermal crystallization on the hydrolysate subjected to carbonization for 15.5 hours at 95 ℃, and filtering the obtained hydrothermal crystallization product to obtain second filter residue and molecular sieve filtrate; further washing and drying the second filter residue, and carrying out XRD analysis on the obtained product to obtain a spectrogram which is compared with a standard card and determined as the 13X type molecular sieve;
the chemical composition (molar ratio) of the molecular sieve filtrate is SiO2:Al2O3:Na2O:CO3 2-:H2O＝35:1:86:71:2140。
(5) To 100ml of the obtained molecular sieve filtrate, 1.05g of sodium fluoride solid was added to obtain a synthetic solution (the amount of sodium fluoride solid added was SiO in the synthetic solution)215 mol%) of;
introducing CO into the synthetic liquid under the stirring state2Carrying out carbonation until the pH value is 11.03; then carrying out hydrothermal crystallization for 40h at the temperature of 180 ℃, and filtering the obtained hydrothermal crystallization product to obtain third filter residue and second filtrate; further washing, drying and roasting the third filter residue, analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, determining the obtained product as the high-silicon mordenite, and analyzing by EDS (electronic discharge spectroscopy) to obtain the mordenite with the silicon-aluminum ratio of 28.8;
(6) mixing the second filtrate (Na as main component)2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
The one-time consumption efficiency mu of the residue of the aluminum extraction by the fly ash acid method is 87.78%; after the first filter residue is recycled, the overall consumption efficiency of the residue generated in the aluminum extraction by the fly ash acid method is considered to be approximately 100 percent; na (Na)2CO3、CO2And the recycling of NaF is realized.
Example 6
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO3Mixing and grinding 65g of solid powder, roasting at 890 ℃ for 60min, quickly cooling with air after roasting is finished, and crushing to be below 200 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation and iron removal, 70g of the roasted slag is added into 105ml of deionized water to be soaked for 20min at the temperature of 95 ℃ and under the normal pressure, and Na in the roasted slag is dissolved out2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) under the high-speed stirring state, taking 93g (equivalent to 70g of roasting slag), adding 100ml of sodium carbonate solution (the concentration is 20 weight percent and is recycled from the second filtrate in the step (6)) to dilute, carrying out suction filtration at 80 ℃, adding 100ml of the sodium carbonate solution to wash (corresponding to 286ml of the total dosage of the second filtrate relative to 100g of roasting slag); adding a certain amount of hot water (about 90 ℃) for washing to obtain a first filtrate with the volume of 400ml for synthesizing the 13X type molecular sieve; drying the obtained first filter residue to obtain 7.22g, and recycling the first filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝13.6:1:18.6:10.5:441。
(4) Taking 120ml of the first filtrate (21.0 g of the first filtrate in terms of roasted slag), adding 60ml of deionized water for hydrolysis (the total volume of the hydrolysate is 857ml relative to 100g of the roasted slag); introducing CO into the obtained hydrolysate under stirring2Carbonation to pH 13.59; then adding 0.2g of 13X type molecular sieve seed crystal (preparation example 2) into the hydrolysate after carbonization, performing hydrothermal crystallization at 110 ℃ for 20 hours, and filtering the obtained hydrothermal crystallization product to obtain second filter residue and molecular sieve filtrate; further washing and drying the second filter residue, and analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, and determining the obtained spectrogram as a 13X-type molecular sieve;
the chemical composition (molar ratio) of the molecular sieve filtrate is SiO2:Al2O3:Na2O:CO3 2-:H2O＝37.7:1:86.5:63:1970；
(5) To 100ml of the obtained molecular sieve filtrate, 1.4g of NaF solid was added to obtain a synthetic solution (the amount of NaF added was about SiO in the synthetic solution)220mol% of);
introducing CO into the synthetic liquid under the stirring state2Carrying out carbonation until the pH is 11.84; then carrying out hydrothermal crystallization for 72h at the temperature of 140 ℃, and carrying out hydrothermal crystallization on the obtained productFiltering to obtain third filter residue and second filtrate; further washing, drying and roasting the third filter residue, analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, determining the obtained product as the high-silicon mordenite, and analyzing by EDS (electronic discharge spectroscopy) to obtain the mordenite with the silicon-aluminum ratio of 30.8;
(6) mixing the second filtrate (Na as main component)2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
The one-time consumption efficiency mu of the residue of the aluminum extraction by the fly ash acid method is 85.56%; after the first filter residue is recycled, the overall consumption efficiency of the residue generated in the aluminum extraction by the fly ash acid method is considered to be approximately 100 percent; na (Na)2CO3、CO2And the recycling of NaF is realized.
Comparative example 1
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO360g of solid powder, mixing and grinding the solid powder, roasting the mixture for 90min at 860 ℃, quickly cooling the mixture in air after roasting is finished, and crushing the mixture to be below 200 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for removing iron, 70g of the roasted slag is taken and added with 700ml of deionized water (the amount of water is 1000ml relative to 100g of the roasted slag), water leaching is carried out for 40min at 100 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved out2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) under the high-speed stirring state, taking 650g of all water-soaked products (which is 70g of roasted slag), carrying out suction filtration at the temperature of 60 ℃, and then adding 100ml of 15 weight percent sodium carbonate solution for washing (which is equivalent to the total dosage of 286ml of the sodium carbonate solution relative to 100g of roasted slag); and adding a certain amount of hot water (about 80 ℃) for washing, drying the obtained first filter residue to obtain 21.62g, wherein the one-time consumption efficiency mu of the residue for extracting the aluminum by the fly ash acid method is only 56.76% by calculation.
In the high-temperature water leaching process of the comparative example 1, the dosage of the added water is too much and exceeds the liquid-solid ratio range of 150-200 ml of water relative to 100g of the roasting slag defined by the invention, so that the alkalinity of a water leaching product is reduced, the dissolution rates of silicon and aluminum are seriously low, the yield of first filter residue is high, and the aim of efficiently dissolving the aluminum extraction residue by the fly ash acid method cannot be fulfilled.
Comparative example 2
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO360g of solid powder, mixing and grinding the solid powder, roasting the mixture for 90min at 860 ℃, quickly cooling the mixture in air after roasting is finished, and crushing the mixture to be below 200 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for iron removal, 70g of the roasted slag is taken and added with 140ml of deionized water (the amount of water is 200ml relative to 100g of the roasted slag), water leaching is carried out for 20min at 100 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved out2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) taking 100g of all water-immersed products (which is 70g of roasted slag) under the high-speed stirring state, adding 100ml of boiling water into the water-immersed products for dilution, carrying out suction filtration at the temperature of 60 ℃, and adding 100ml of boiling water for flushing (equivalent to 286ml of the total adding amount of the boiling water relative to 100g of the roasted slag); adding a certain amount of hot water (about 80 ℃) for washing to obtain a first filtrate with the volume of 400ml for synthesizing the 13X type molecular sieve; drying the obtained first filter residue to obtain 16.53g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝8.2:1:12.5:7.8:450。
(4) And directly synthesizing a 13X type molecular sieve by using the first filtrate, performing hydrothermal crystallization for 15.5 hours at 95 ℃, and filtering an obtained hydrothermal crystallization product to obtain a solid product.
The obtained solid product is detected by XRD to be a mixture of amorphous aluminosilicate and various molecular sieves, namely, the pure 13X type molecular sieve cannot be obtained.
In comparative example 2, the water leaching product is diluted and filtered and washed by using boiling water, and a sodium carbonate solution is not adopted, so that Si in a liquid phase of the water leaching product is highly hydrolyzed in the dilution and filtering processes to generate solid-phase hydrated silicon dioxide, so that serious filtering loss is generated, the yield of first filter residue is greatly increased, and the once-dissolving efficiency mu of the fly ash acid method aluminum extraction residue is reduced to 66.94%. Meanwhile, the first filtrate is directly used for hydrothermal crystallization according to the conventional hydrothermal crystallization conditions, and the pure 13X-type molecular sieve cannot be obtained.
In addition, the synthesis mother liquor suitable for synthesizing the high-silicon mordenite cannot be obtained in the steps (1) to (3), and pure high-silicon mordenite cannot be obtained. The tail liquid after synthesizing the 13X-type molecular sieve or the molecular sieve filtrate mainly contains sodium carbonate, only contains trace Si and Al, and cannot be used as a silicon source or an aluminum source to further synthesize any other type of molecular sieve.
Comparative example 3
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO360g of solid powder, mixing and grinding the solid powder, roasting the mixture for 90min at 860 ℃, quickly cooling the mixture in air after roasting is finished, and crushing the mixture to be below 200 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for iron removal, 70g of the roasted slag is taken and added with 140ml of deionized water (the amount of water is 200ml relative to 100g of the roasted slag), water leaching is carried out for 20min at 100 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved out2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) taking 100g (equivalent to 70g of roasting slag) of all water-leached products under the high-speed stirring state, adding 100ml of sodium carbonate solution (the concentration is 15 weight percent for the second filtrate recycled from the step (5)) to dilute, carrying out suction filtration at the temperature of 60 ℃, adding 100ml of the sodium carbonate solution to wash (corresponding to 286ml of the total dosage of the second filtrate relative to 100g of roasting slag); adding a certain amount of hot water (about 80 ℃) for washing to obtain a first filtrate with the volume of 400ml for synthesizing the 13X type molecular sieve; drying the obtained first filter residue to obtain 6.52g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝14.5:1:21.2:11.5:366。
(4) Taking 400ml of the whole first filtrate (70.0 g of the first filtrate in terms of roasting slag), adding 200ml of deionized water for hydrolysis (the total volume of hydrolysate is 857ml relative to 100g of the roasting slag); sodium metaaluminate (NaAlO) is also added2) 31.44g of solid is prepared into 13X type molecular sieve synthesis mother liquor, and the chemical composition (molar ratio) of the mother liquor is SiO2:Al2O3:Na2O:CO3 2-:H2O＝12:4:115.5:46:487。
Introducing CO into the obtained hydrolysate under stirring2Carbonation to pH 13.455; then carrying out hydrothermal crystallization on the hydrolysate subjected to carbonization for 15.5 hours at 95 ℃, and filtering the obtained hydrothermal crystallization product to obtain second filter residue and second filtrate; further washing and drying the second filter residue, and analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, and determining the obtained spectrogram as a 13X-type molecular sieve;
(5) second filtrate (main component is Na)2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
Comparative example 3 is prepared conventionally13X type molecular sieve synthesis mother liquor, but needs additional aluminum source sodium metaaluminate (M)out31.44g), the absorption efficiency mu of the fly ash acid method aluminum extraction residue is only 53.39 percent; and the obtained second filtrate can not be used for preparing the high-silicon mordenite continuously, and only the product 13X type molecular sieve is obtained.
Comparative example 4
(1) Adding 50g of residue of aluminum extraction by fly ash acid method into Na2CO3Mixing and grinding 65g of solid powder, roasting at 890 ℃ for 60min, quickly cooling with air after roasting is finished, and crushing to be below 200 meshes to obtain roasted slag;
(2) after the roasted slag is subjected to dry magnetic separation for iron removal, 70g of the roasted slag is taken and added with 140ml of deionized water (the amount of water is 200ml relative to 100g of the roasted slag), water leaching is carried out for 20min at 100 ℃ and normal pressure, and Na in the roasted slag is leached and dissolved out2SiO3And NaAlSiO4To obtain a solid-liquid mixed water leaching product; wherein the solid is dissolved Na2SiO3And NaAlSiO4The remaining product after that; the liquid is Na-containing2SiO3And NaAlSiO4The solution of (1);
(3) taking 100g (equivalent to 70g of roasting slag) of all water-leached products under the high-speed stirring state, adding 100ml of sodium carbonate solution (the concentration is 15 weight percent for the second filtrate recycled from the step (6)) to dilute, carrying out suction filtration at the temperature of 60 ℃, adding 100ml of the sodium carbonate solution to wash (corresponding to 286ml of the total dosage of the second filtrate relative to 100g of roasting slag); adding a certain amount of hot water (about 80 ℃) for washing to obtain a first filtrate with the volume of 400 ml; drying the obtained first filter residue to obtain 6.79g of filter residue, and recycling the filter residue to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1);
the first filtrate had a chemical composition (molar ratio) of SiO2:Al2O3:Na2O:CO3 2-:H2O＝14.2:1:17:8.6:462。
(4) The first filtrate (70.0 g in terms of roasted slag) was taken and added to 1500ml of deionized water to hydrolyze (total amount of hydrolysate per 100g of roasted slag)Volume is 2143 ml); sodium metasilicate (Na) is also added2SiO3) 179.44g of solid, which is used as the hydrothermal crystallization mother liquor of the high-silicon mordenite after being completely dissolved, and the chemical composition (molar ratio) of the solid is SiO2:Al2O3:Na2O:CO3 2-:H2O＝43.6:1:46.4:8.6:2129。
(5) Taking 100ml of the obtained hydrothermal crystallization mother liquor, adding 1.4g of sodium fluoride solid to obtain a synthetic liquid (the adding amount of the ammonium fluoride solid is SiO in the synthetic liquid)220mol% of);
introducing CO into the synthetic liquid under the stirring state2Carbonizing to pH 12.0; then carrying out hydrothermal crystallization for 48 hours at the temperature of 180 ℃, and filtering the obtained hydrothermal synthesis product to obtain third filter residue and second filtrate; further washing, drying and roasting the third filter residue, analyzing an obtained product by XRD (X-ray diffraction), comparing an obtained spectrogram with a standard card, determining the obtained product as the high-silicon mordenite, and analyzing by EDS (electronic discharge spectroscopy) to obtain the mordenite with the silicon-aluminum ratio of 33.6;
(6) mixing the second filtrate (Na as main component)2CO3Part containing a small amount of Si and Al) is recycled and added into the sodium carbonate solution in the step (3) for diluting, filtering and washing the water leaching product; the remaining part of the second filtrate is evaporated and crystallized to obtain Na2CO3And (4) recycling the solid to the alkaline roasting of the fly ash acid-process aluminum extraction residue in the step (1).
Adjusting the composition of the first filtrate for the synthesis of high-silicon mordenite in comparative example 4, additional silicon source of sodium metasilicate (M)out179.44g) results in the production of high-silicon mordenite only, and results in a once-through efficiency μ of only 18.83% in the fly ash acid-process aluminum extraction residue. The obtained second filtrate can not be used as a silicon source or an aluminum source to further prepare the 13X type or any other type of molecular sieve; namely, the obtained product only contains one high-silicon mordenite.
From the above examples, it can be seen that the method provided by the present invention can fully utilize the residue of the acid extraction of aluminum from fly ash without the need of adding additional silicon source or aluminum source. The 13X type molecular sieve and the high-silicon mordenite with high added values can be simultaneously produced and obtained while efficiently dissolving the residue of the aluminum extraction by the fly ash acid method.
In addition, the method provided by the invention can also realize the full utilization of the fly ash, and the conversion of the fly ash to produce alumina, 13X-type molecular sieve and high-silicon mordenite is realized without additionally adding a silicon source or an aluminum source.
Claims (8)
1. A method for preparing 13X type molecular sieve and high-silicon mordenite by extracting aluminum residue from fly ash by an acid method comprises the following steps:
(1) carrying out alkaline roasting on the residue of the acid-method aluminum extraction of the fly ash to obtain roasted slag; sequentially carrying out high-temperature water immersion and heat preservation filtration on the roasted slag charge to obtain a first filtrate;
(2) carrying out 13X type molecular sieve hydrothermal crystallization on the first filtrate to obtain a 13X type molecular sieve and a molecular sieve filtrate;
(3) carrying out hydrothermal crystallization on the molecular sieve filtrate and sodium fluoride to obtain high-silicon mordenite and a second filtrate;
wherein, in the step (1), the high-temperature water leaching process comprises the following steps: removing iron from the roasted slag, mixing the roasted slag with water, and performing water leaching to obtain a water leaching product; the using amount of water is 150-200 ml relative to 100g of the roasted slag charge; the process of heat preservation and filtration comprises the following steps: diluting, filtering and washing the water leaching product with partial second filtrate to obtain first filter residue and the first filtrate; the process of heat preservation and filtration comprises the following steps: the filtering temperature is kept between 60 and 80 ℃; the dosage of the second filtrate is 250-350 ml relative to 100g of the roasting slag charge; SiO in the first filtrate2With Al2O3The molar ratio of (10-25): 1
Wherein, in the step (2), the process of hydrothermal crystallization of the 13X-type molecular sieve comprises the following steps:
a) adding water into the first filtrate for hydrolysis to obtain a hydrolysate; the adding amount of water is such that the total volume of the hydrolysate is 850-1000 ml relative to 100g of the roasting slag charge;
b) introducing CO into the hydrolysate2Carrying out carbonation to enable the pH of the hydrolysate to be 13-15;
c) adding or not adding 13X type molecular sieve seed crystals into the product obtained in the step b), and then carrying out hydrothermal crystallization for 15-30 h at 90-110 ℃ to obtain a 13X type molecular sieve hydrothermal crystallization product; the dosage of the 13X-type molecular sieve seed crystal is 0-10 wt% of the roasting slag charge;
d) filtering the 13X type molecular sieve hydrothermal crystallization product to obtain a second filter residue and the molecular sieve filtrate; drying the second filter residue to obtain the 13X-type molecular sieve; SiO in the molecular sieve filtrate2With Al2O3The molar ratio of (35-45): 1.
2. the method of claim 1, wherein in step (1), the alkaline roasting comprises: mixing and grinding 100 parts by weight of the fly ash acid-process aluminum extraction residue and 100-130 parts by weight of a sodium carbonate-containing material, roasting the obtained ground product at 830-890 ℃ for 60-120 min, and then crushing to below 200 meshes to obtain the roasted slag material.
3. The method as claimed in claim 2, wherein, in the step (1), the high temperature water immersion process comprises: the water immersion temperature is 95-105 ℃, and the water immersion time is 15-20 min.
4. The method of claim 1, wherein the method further comprises: and (3) drying the first filter residue, and then recycling the first filter residue, adding the first filter residue into the fly ash acid method aluminum extraction residue in the step (1).
5. The method of claim 1, wherein in step (3), the hydrothermal crystallization of the high-silicon mordenite comprises:
i) adding sodium fluoride solid into the molecular sieve filtrate to obtain synthetic liquid;
ii) introducing CO into the synthetic fluid2Carrying out carbonation to ensure that the pH value of the synthetic liquid is 11-14;
iii) carrying out hydrothermal crystallization on the product obtained in the step ii) at the temperature of 140-190 ℃ for 15-72 h to obtain a high-silicon mordenite hydrothermal crystallization product;
iv) filtering the high-silicon mordenite hydrothermal crystallization product to obtain a third filter residue and the second filtrate; and washing, drying and roasting the third filter residue to obtain the high-silicon mordenite.
6. The method of claim 5, wherein the sodium fluoride solids are added in an amount of SiO in the synthesis solution210 to 20mol% of the amount of the catalyst.
7. The method of claim 1, wherein the method further comprises:
recycling a part of the second filtrate to the heat-preservation filtering process in the step (1); and (3) evaporating and crystallizing the other part of the second filtrate to obtain sodium carbonate, and recycling the sodium carbonate to the alkali roasting process in the step (1).
8. A method for utilizing fly ash, the method comprising: carrying out acid method aluminum extraction on the fly ash to obtain fly ash acid method aluminum extraction residue and aluminum oxide; 13X type molecular sieve and high silicon mordenite are prepared from fly ash acid method aluminum extraction residue by the method of any one of claims 1-7.
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| CN101804995A (en) * | 2010-04-13 | 2010-08-18 | 中国地质大学（武汉） | Method for preparing high-silicon mordenite by using raw mineral material |
| CN104743571A (en) * | 2013-12-27 | 2015-07-01 | 杨治平 | Method for preparing 13X type molecular sieve through coal ash |
| CN105217588A (en) * | 2015-09-16 | 2016-01-06 | 黄钰雪 | The circulation clean production method of yellow phosphorus coproduction sylvite, aluminum oxide, molecular sieve, slag cement and architectural shape |
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| CN101804995A (en) * | 2010-04-13 | 2010-08-18 | 中国地质大学（武汉） | Method for preparing high-silicon mordenite by using raw mineral material |
| CN104743571A (en) * | 2013-12-27 | 2015-07-01 | 杨治平 | Method for preparing 13X type molecular sieve through coal ash |
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