CN110201975A - A kind of abraum salt recycling treatment disposal system and application - Google Patents
A kind of abraum salt recycling treatment disposal system and application Download PDFInfo
- Publication number
- CN110201975A CN110201975A CN201910461209.0A CN201910461209A CN110201975A CN 110201975 A CN110201975 A CN 110201975A CN 201910461209 A CN201910461209 A CN 201910461209A CN 110201975 A CN110201975 A CN 110201975A
- Authority
- CN
- China
- Prior art keywords
- output end
- input terminal
- salt
- flue gas
- abraum
- Prior art date
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- Pending
Links
- 150000003839 salts Chemical class 0.000 title claims abstract description 276
- 238000004064 recycling Methods 0.000 title claims abstract description 34
- 238000000197 pyrolysis Methods 0.000 claims abstract description 113
- 239000003546 flue gas Substances 0.000 claims abstract description 111
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 107
- 238000001704 evaporation Methods 0.000 claims abstract description 59
- 230000008020 evaporation Effects 0.000 claims abstract description 58
- 239000007789 gas Substances 0.000 claims abstract description 49
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 43
- 238000004090 dissolution Methods 0.000 claims abstract description 36
- 239000002893 slag Substances 0.000 claims abstract description 34
- 239000003610 charcoal Substances 0.000 claims abstract description 33
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 30
- 239000012267 brine Substances 0.000 claims abstract description 28
- 238000012545 processing Methods 0.000 claims abstract description 28
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 28
- 239000011780 sodium chloride Substances 0.000 claims abstract description 20
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 13
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 13
- 238000001035 drying Methods 0.000 claims abstract description 12
- 238000001640 fractional crystallisation Methods 0.000 claims abstract description 7
- 239000000178 monomer Substances 0.000 claims abstract description 6
- 230000009977 dual effect Effects 0.000 claims description 57
- 238000010304 firing Methods 0.000 claims description 54
- 238000000034 method Methods 0.000 claims description 53
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 44
- 238000000108 ultra-filtration Methods 0.000 claims description 39
- 230000001376 precipitating effect Effects 0.000 claims description 36
- 238000002425 crystallisation Methods 0.000 claims description 35
- 230000008025 crystallization Effects 0.000 claims description 34
- 239000003153 chemical reaction reagent Substances 0.000 claims description 33
- 230000008569 process Effects 0.000 claims description 32
- 239000000047 product Substances 0.000 claims description 32
- 239000002918 waste heat Substances 0.000 claims description 32
- 238000005201 scrubbing Methods 0.000 claims description 29
- UIIMBOGNXHQVGW-UHFFFAOYSA-M sodium bicarbonate Substances [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 29
- 239000002253 acid Substances 0.000 claims description 25
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Substances [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 22
- 230000007717 exclusion Effects 0.000 claims description 21
- 239000003345 natural gas Substances 0.000 claims description 21
- 238000002485 combustion reaction Methods 0.000 claims description 20
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 20
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 19
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 17
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 16
- 239000000908 ammonium hydroxide Substances 0.000 claims description 16
- 229910052799 carbon Inorganic materials 0.000 claims description 16
- 239000005416 organic matter Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 15
- 239000008234 soft water Substances 0.000 claims description 15
- 239000003638 chemical reducing agent Substances 0.000 claims description 14
- 239000007787 solid Substances 0.000 claims description 14
- 239000000243 solution Substances 0.000 claims description 14
- 239000012535 impurity Substances 0.000 claims description 12
- 239000002351 wastewater Substances 0.000 claims description 12
- 239000002562 thickening agent Substances 0.000 claims description 11
- 239000000706 filtrate Substances 0.000 claims description 10
- 239000000446 fuel Substances 0.000 claims description 9
- 239000000571 coke Substances 0.000 claims description 8
- 239000004744 fabric Substances 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 7
- 239000012043 crude product Substances 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000007254 oxidation reaction Methods 0.000 claims description 6
- 206010002660 Anoxia Diseases 0.000 claims description 5
- 241000976983 Anoxia Species 0.000 claims description 5
- 206010021143 Hypoxia Diseases 0.000 claims description 5
- 230000007953 anoxia Effects 0.000 claims description 5
- 239000002738 chelating agent Substances 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 238000004806 packaging method and process Methods 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 5
- 235000019504 cigarettes Nutrition 0.000 claims description 4
- 239000000356 contaminant Substances 0.000 claims description 4
- 238000012797 qualification Methods 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 4
- 238000012546 transfer Methods 0.000 claims description 4
- 239000004568 cement Substances 0.000 claims description 3
- 238000006555 catalytic reaction Methods 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 6
- 239000002440 industrial waste Substances 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract description 3
- 235000002639 sodium chloride Nutrition 0.000 description 227
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 18
- 239000000428 dust Substances 0.000 description 16
- 239000007788 liquid Substances 0.000 description 16
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 16
- 230000000694 effects Effects 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 14
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 13
- 229910002092 carbon dioxide Inorganic materials 0.000 description 13
- 239000000126 substance Substances 0.000 description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 9
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 9
- 238000001816 cooling Methods 0.000 description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 description 9
- 239000002699 waste material Substances 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 8
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- 235000017557 sodium bicarbonate Nutrition 0.000 description 7
- 235000017550 sodium carbonate Nutrition 0.000 description 7
- 239000003500 flue dust Substances 0.000 description 6
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 239000011734 sodium Substances 0.000 description 6
- 238000005406 washing Methods 0.000 description 6
- 229910019142 PO4 Inorganic materials 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 239000013078 crystal Substances 0.000 description 5
- 238000013461 design Methods 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 229910001385 heavy metal Inorganic materials 0.000 description 5
- 238000007654 immersion Methods 0.000 description 5
- 239000012528 membrane Substances 0.000 description 5
- 239000010452 phosphate Substances 0.000 description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 5
- 238000009938 salting Methods 0.000 description 5
- 239000007921 spray Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 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 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 229910017053 inorganic salt Inorganic materials 0.000 description 4
- 229910052753 mercury Inorganic materials 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 239000004615 ingredient Substances 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 230000006641 stabilisation Effects 0.000 description 3
- 238000011105 stabilization Methods 0.000 description 3
- 229910052815 sulfur oxide Inorganic materials 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 229910002089 NOx Inorganic materials 0.000 description 2
- 239000007832 Na2SO4 Substances 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 2
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000001351 cycling effect Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 230000013011 mating Effects 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 150000003384 small molecules Chemical class 0.000 description 2
- 229940079827 sodium hydrogen sulfite Drugs 0.000 description 2
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000002341 toxic gas Substances 0.000 description 2
- 239000012855 volatile organic compound Substances 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 229910020933 NaCl—Na2SO4 Inorganic materials 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- 241001529739 Prunella <angiosperm> Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 150000001721 carbon Chemical class 0.000 description 1
- 229910021386 carbon form Inorganic materials 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000185 dioxinlike effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- BNIILDVGGAEEIG-UHFFFAOYSA-L disodium hydrogen phosphate Chemical compound [Na+].[Na+].OP([O-])([O-])=O BNIILDVGGAEEIG-UHFFFAOYSA-L 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000001754 furnace pyrolysis Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000009931 harmful effect Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910000403 monosodium phosphate Inorganic materials 0.000 description 1
- 235000019799 monosodium phosphate Nutrition 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 238000000643 oven drying Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000002296 pyrolytic carbon Substances 0.000 description 1
- 238000001953 recrystallisation Methods 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 150000003385 sodium Chemical class 0.000 description 1
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 description 1
- 239000001488 sodium phosphate Substances 0.000 description 1
- 229910000162 sodium phosphate Inorganic materials 0.000 description 1
- 235000011008 sodium phosphates Nutrition 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000003019 stabilising effect Effects 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- RYFMWSXOAZQYPI-UHFFFAOYSA-K trisodium phosphate Chemical compound [Na+].[Na+].[Na+].[O-]P([O-])([O-])=O RYFMWSXOAZQYPI-UHFFFAOYSA-K 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B2101/00—Type of solid waste
- B09B2101/02—Gases or liquids enclosed in discarded articles, e.g. aerosol cans or cooling systems of refrigerators
Abstract
The present invention relates to a kind of abraum salt recycling treatment disposal systems, the system comprises be sequentially connected the charing pyrolysis system for the abraum salt for connecing setting, the dissolution filter system and evaporation point salt system of the slag of salt containing charcoal, the charing pyrolysis system of the abraum salt can carry out charing pyrolysis processing to the abraum salt I being made of sodium chloride, sodium sulphate monomer salt or mixed abraum salt, and can handle tail gas；The dissolution filter system of the slag of salt containing charcoal can charing pyrolysis system to abraum salt treated that the slag of salt containing charcoal dissolved, filter operation；The evaporation point salt system can dissolution filter system to the slag of salt containing charcoal treated that strong brine is evaporated concentration, fractional crystallization and drying process, obtain product salt.This system carries out removing organic pollutant, mixed inorganic point salt treatment using industrial waste salt as raw material, to abraum salt, and final output industry second level product salt realizes the recycling of abraum salt, and can be realized the flue gas qualified discharge generated in production process.
Description
Technical field
The invention belongs to environmental technology field, it is related to a kind of abraum salt recycling treatment disposal system and application.
Background technique
Industrial waste salt is mainly from industries such as coal chemical industry, pesticide, chemical fertilizer, biochemical industries, these industrial waste salts Chang Yin is wherein
It can not be reused in industrial production containing a certain amount of organic matter, these abraum salts are also classified as danger by national relevant legal documents
Dangerous waste.Often complicated component, poisonous and harmful property are big for abraum salt, are the difficult points of dangerous waste industry processing, and processing cost is high, at ton
For reason expense at 3500 yuan or more, this often brings very big burden to enterprise, while also resulting in the wasting of resources.
Currently, the Technical comparing both at home and abroad about abraum salt processing is limited, main disposal technology has:
(1) direct incineration method
This method is added directly waste salt dregs to incinerator, and material from top to bottom, about 900 degree of heating temperature, gives up
Salt melting flows into furnace bottom, recycles after cooling, the organic pollutant that abraum salt includes gasifies at high temperature, decomposes, tail gas from incinerator
It further burns into dual firing chamber or is directly discharged after physical chemistry processing.But this method needs to carry out predrying simultaneously to waste salt dregs
It is required that the particle of waste salt dregs is uniform and partial size is as small as possible, in order to particle internal temperature gradient minimum, but with air blast
Into, be easy to furnace roof portion formed fused salt rain, melting, ring formation, knot occur with successively decreasing for temperature in subsequent each unit
The severe phenomenon such as block, and assemble in its equipment pipe inner wall, easily device is caused to block, industrialization stabilising arrangement not yet appears in the newspapers
Road.
(2) removal of impurities+evaporative crystallization processing is dissolved
This method is that abraum salt is redissolved in clear water, by physical-chemical process remove impurity (organic matter, heavy metal from
Son etc.) after again by evaporative crystallization recycle inorganic salts.But this method processing cost is high, and has secondary waste water and sludge to generate,
Particularly with the highly concentrated salt containing organic matter, the effect that physical chemistry is disposed after dissolution is difficult to ensure.
(3) innoxious landfill stabilization
This method is mixed all kinds of abraum salts and after the solidification of the curing agent such as concrete, according to National Hazard waste management and
The relevant laws and regulations and technical specification of disposition carry out special landfill stabilization.The method of disposal not only occupies a large amount of soil, while easily
Cause secondary pollution.
(4) pyrolysismethod
Pyrolysismethod is under 550 DEG C~600 DEG C, anoxia condition, the organic matter in abraum salt to occur endless using pyrolysis oven
It is oxidized, it is decomposed into CH4、H2, CO and coke process.And the coke formed after the organic matter pyrolysis in abraum salt remain in it is inorganic
Salt surface need to further be dissolved, be filtered, evaporative crystallization processing, separating inorganic salts with coke, and finally obtained purity is higher
Inorganic salt product.
Therefore, one or more of relevant processing equipments are needed.
By retrieval, following two patent publication us relevant to present patent application are found:
1, phosphatic abraum salt recycling processing method (CN109607503A), the method first will be phosphatic
Abraum salt mixes after 300 DEG C~500 DEG C pyrolysis with water, and phosphate is made sufficiently to dissolve and add under 80 DEG C~100 DEG C heating conditions
Enter active carbon stirring, the phosphate solution containing a small amount of sodium chloride is obtained by filtration, adjusts the pH value of salting liquid to 4~12, then
Phosphate solid, solid-liquid point is precipitated with the rate of temperature fall crystallisation by cooling of 15~30 DEG C/h in 70 DEG C~90 DEG C of hot phosphoric acid salting liquid
From rear recycling filtrate, phosphate is obtained.The present invention recycles phosphoric acid in the form of sodium dihydrogen phosphate, disodium hydrogen phosphate and sodium phosphate etc.
Salt, the resource utilization for realizing abraum salt utilize, and the phosphate purity is high and grain size of recycling are preferable, avoid recrystallization process
The middle too fast problem for leading to crystallization effect difference of cooling, meanwhile, isolated active carbon and filtrate can be repeated by regeneration
It utilizes, ensure that the zero-emission of waste water.
2, sodium chloride abraum salt recycling processing method (CN108929708A) during a kind of DYE PRODUCTION, the present invention is first led to
It crosses the moisture removed under condition of different temperatures in abraum salt in oxygen-free environment, split small organic molecule gasification, aromatic ring substance
The condensed ring substance charing such as solution, naphthalene and anthracene, then by the dissolution of gained salt, except obtaining purification of chlorinated sodium solution, gained after charing particle
Sodium chloride solution is electrolysed by Bipolar Membrane, prepares sodium hydroxide solution and dilute hydrochloric acid.Entire treatment process is simple and efficient, economy can
Row, while realizing the resource utilization and utilization of the product of sodium chloride abraum salt, the small organic molecule of cracking and charing.
By comparison, there is essential difference in present patent application and above-mentioned patent publication us.
Summary of the invention
It is an object of the invention to overcome the shortcoming of existing abraum salt processing technique, a kind of abraum salt recycling treatment is provided
Disposal system and application, which carries out removing organic pollutant using industrial waste salt as raw material, to abraum salt, mixed inorganic divides salt
Processing, final output industry second level product salt, such as anhydrous sodium sulfate, sodium chloride, sodium bicarbonate finished product salt, realize the money of abraum salt
Source has preferable economic benefit and good social benefit, and can be realized the flue gas generated in production process row up to standard
It puts, which can apply in terms of the abraum salt recycling treatment.
The present invention solves its technical problem and adopts the following technical solutions to achieve:
A kind of abraum salt recycling treatment disposal system, the system comprises be sequentially connected the charing pyrolysis for connecing the abraum salt of setting
System, the dissolution filter system of the slag of salt containing charcoal and evaporation divide salt system, and the charing pyrolysis system of the abraum salt can be to by chlorination
The abraum salt I of sodium, sodium sulphate monomer salt or mixed abraum salt composition carries out charing pyrolysis processing, and can be handled simultaneously tail gas
Qualified discharge；The dissolution filter system of the slag of salt containing charcoal can charing pyrolysis system to abraum salt treated the slag of salt containing charcoal into
Row dissolution, filter operation；The evaporation divide salt system can dissolution filter system to the slag of salt containing charcoal treated strong brine into
Row evaporation and concentration, fractional crystallization and drying process, obtain product salt.
Moreover, the charing pyrolysis system of the abraum salt includes at conveying system, rotary pyrolysis oven, combustion system and tail gas
Reason system, the input terminal of the conveying system can input abraum salt I to be processed, the output end of the conveying system and rotary heat
The input terminal of solution furnace is connected setting, and the output end of the rotary pyrolysis oven includes the slag output end of salt containing charcoal and pyrolysis gas output
End, the slag output end of salt containing charcoal are connected setting, the pyrolysis gas output end and tail with the dissolution filter system of the slag of salt containing charcoal
Gas processing system is connected setting；The input terminal of the combustion system is connected setting with natural gas, the output of the combustion system
Hold the setting that is also connected with the input terminal of rotary pyrolysis oven；
The exhaust treatment system includes dual firing chamber, waste heat boiler, chilling tower, bag filter, forecooler, two-stage washing
Tower, flue gas disappear white device, chimney and circulating water chennel, and the dual firing chamber includes input terminal and flue gas output end, the dual firing chamber it is defeated
Entering end includes natural gas input, pyrolysis gas input terminal and ammonium hydroxide input terminal, and the natural gas input is connected with natural gas
Setting can input natural gas by the natural gas input into dual firing chamber, the pyrolysis gas input terminal of the dual firing chamber with return
The pyrolysis gas output end of rotatable pyrolysis oven is connected setting, and the ammonium hydroxide input terminal is connected setting with ammonium hydroxide, passes through the ammonium hydroxide
Input terminal can input ammonium hydroxide into dual firing chamber；
The input terminal of the waste heat boiler includes soft water input terminal and flue gas input terminal, and the output end of the waste heat boiler includes
Steam output end and flue gas output end, the flue gas input terminal of the waste heat boiler is connected with the flue gas output end of dual firing chamber to be set
Set, the soft water input terminal of the waste heat boiler is connected setting with soft water, by the soft water input terminal can into waste heat boiler it is defeated
Enter soft water, the steam output end of the waste heat boiler and evaporation point salt system, the flue gas white device that disappears are connected setting；
The input terminal of the chilling tower includes flue gas input terminal and quencher input terminal, the flue gas input terminal of chilling tower with it is remaining
The flue gas output end of heat boiler is connected setting, and the quencher input terminal is connected setting with quencher, passes through the quencher
Input terminal can input quencher into chilling tower, and the output end of the chilling tower is connected with the input terminal of bag filter to be set
It sets, is provided with active carbon input terminal on the pipeline between the output end of chilling tower, bag filter, passes through the active carbon input terminal
Active carbon, the output end of the bag filter can be inputted into the pipeline between the output end, bag filter of chilling tower
Be connected setting with the input terminal of forecooler, and the output end of the forecooler is connected setting with the input terminal of two-stage scrubbing tower；
The output end of the two-stage scrubbing tower includes waste water output end and flue gas output end, the waste water of the two-stage scrubbing tower
Output end and the input terminal of evaporation point salt system, circulating water chennel are respectively connected with setting, the flue gas output end of the two-stage scrubbing tower
It is connected setting with the disappear input terminal of white device of flue gas, the flue gas output end of white device that disappears is connected with the input terminal of chimney and sets
It sets, the output end of the chimney can export the flue gas of qualified discharge；
The output end of the circulating water chennel is connected setting with the input terminal of two-stage scrubbing tower, which can be to two
Lye is inputted in grade scrubbing tower, which can reach discharge standard for the contaminant removal in flue gas.
Moreover, the conveying system uses screw feeding structure, matching setting frequency control motor, discharge system is equally adopted
With screw feeding structure；
Alternatively, the combustion system is combustor, fuel uses natural gas；
Alternatively, the scrubbing tower is wet scrubber tower, which can remove sour gas.
Moreover, the pyrolytic process of abraum salt is to make to give up under 550 DEG C~600 DEG C, anoxia condition in the rotary pyrolysis oven
Organic matter in salt generates incomplete oxidation, is decomposed into CH4/CO/H2And coke.
Moreover, dual firing chamber is heated up to 1100 DEG C after the pyrolysis smoke generated in the rotary pyrolysis oven is passed through dual firing chamber
More than, and stopped 2 seconds or more in dual firing chamber；Alternatively, the chilling tower is atomizing chilling tower, quencher uses limewash, cigarette
Residence time of the gas in chilling tower is less than 1s.
Moreover, the bag filter selects high temperature resistant material, the exhaust temperature into cloth bag is controlled at 220 ± 5 DEG C；
Alternatively, the chilling tower is half dry type chilling tower；Alternatively, mixing is provided in the cleaning solution of the two-stage scrubbing tower
Catalyst and chelating agent.
Moreover, the dissolution filter system of the slag of salt containing charcoal includes dissolved salt tank, level-one ultrafiltration apparatus, breeze collector, two
Grade ultrafiltration apparatus and trace solid residue collector, the output end of the rotary pyrolysis oven are connected with the input terminal of dissolved salt tank
Setting, the output end of the dissolved salt tank are connected setting with the input terminal of level-one ultrafiltration apparatus, between dissolved salt tank, level-one ultrafiltration apparatus
Pipeline on be connected precipitating reagent input terminal be set, by the precipitating reagent input terminal can to dissolved salt tank, level-one ultrafiltration apparatus it
Between pipeline in input precipitating reagent, the output end of the level-one ultrafiltration apparatus includes breeze output end and strong brine output end, institute
It states the breeze output end of level-one ultrafiltration apparatus and the input terminal of breeze collector is connected setting, the output end of the breeze collector
Be connected setting with dual firing chamber；The strong brine output end of the level-one ultrafiltration apparatus is connected with the input terminal of two-stage ultrafiltering device
It is arranged, is connected on the pipeline between level-one ultrafiltration apparatus, two-stage ultrafiltering device and precipitating reagent input terminal is set, pass through the precipitating reagent
Input terminal can input precipitating reagent into the pipeline between level-one ultrafiltration apparatus, two-stage ultrafiltering device；
The output end of the two-stage ultrafiltering device includes residue output end and strong brine output end, the two-stage ultrafiltering device
Residue output end is connected setting with trace solid residue collector, the trace solid residue in the trace solid residue collector
It can be transported to cement kiln comprehensive utilization outside or transfer to the processed in units with related qualification.
Moreover, the evaporation point salt system includes carbonating column, magma thickener and evaporation and crystallization system, the carbonating
The input terminal of tower includes strong brine input terminal and CO2Input terminal, the strong brine input terminal and two-stage ultrafiltering device of the carbonating column
Strong brine output end be connected setting, the CO of the carbonating column2Input terminal and CO2Be connected setting, passes through the CO2Input
End can input CO into carbonating column2, the output end of the carbonating column is connected setting with the input terminal of magma thickener, should
The output end of magma thickener includes NaHCO3Output end and magma output end, the NaHCO3Output end can export NaHCO3
Crude product, the NaHCO3Crude product can obtain NaHCO after centrifugation, drying, packaging operation3Product；The magma output end and evaporation
The input terminal of crystal system is connected setting, and the output end of the evaporation and crystallization system includes condensed water output end and salt output end,
The condensed water output end can export condensed water after processing, which is respectively connected with dissolved salt tank, water storage tank
Setting, the salt output end can export finished product salt；
The strong brine output end of the two-stage ultrafiltering device is also directly connected with the input terminal of evaporation and crystallization system setting,
Sour input terminal is set on the pipeline between two-stage ultrafiltering device, evaporation and crystallization system, it can be super to second level by the acid input terminal
Filter input acid in the pipeline between device, evaporation and crystallization system.
Moreover, the disposal system further includes abraum salt II disposal system, the abraum salt II disposal system includes the molten system of acid
And exclusion device, the input terminal of the molten system of acid can input abraum salt II, the input terminal of the exclusion device includes the molten place of acid
Liquid input terminal and reducing agent/precipitating reagent input terminal are managed, the molten treatment fluid of acid of the output end and exclusion device of the molten system of acid is defeated
Enter end to be connected setting, reducing agent/precipitating reagent input terminal of the exclusion device is connected setting with reducing agent/precipitating reagent, passes through
The reducing agent/precipitating reagent input terminal can input reducing agent/precipitating reagent into exclusion device, and the output end of the exclusion device includes
Impurity filter residue output end and filtrate output end, the impurity filter residue output end can export impurity filter residue, the exclusion device
Filtrate output end is connected setting with the input terminal of evaporation and crystallization system.
Abraum salt recycling treatment disposal system as described above in terms of the abraum salt recycling treatment in application.
The advantages of present invention obtains and good effect are:
1, this system includes the charing pyrolysis system for being sequentially connected the abraum salt for connecing setting, the dissolution filter system of the slag of salt containing charcoal
Divide salt system with evaporation, which can carry out refinement treatment to industrial waste salt, carry out removing organic pollutant, mixing to abraum salt
Inorganic salinity salt treatment, final output industry second level product salt, such as anhydrous sodium sulfate, sodium chloride, sodium bicarbonate finished product salt, it is real
The recycling of existing abraum salt has preferable economic benefit and good social benefit, and can be realized and generate in production process
Flue gas qualified discharge, the system can be applied in terms of the abraum salt recycling treatment；
In addition, this system need not occupy a large amount of soil, secondary pollution will not be caused, processing cost is low, no secondary useless
Water and sludge generate, and for the highly concentrated salt containing organic matter, the effect that physical chemistry is disposed after dissolution can be ensured, using steady
It is fixed, it can be applied to industrialize, the higher inorganic salt product of purity can be made.
2, the waste salt dregs recycling treatment that this system is generated suitable for industrial processes, abraum salt is through medium temperature pyrolytic carbon
Change, dissolution filter, evaporation divide salt process, finally obtain the higher product salt of purity, and mixed salt production quantity is few.This system technology is first
Into easily operated, product quality is controllable, it can be ensured that the overall process recycling of abraum salt.
3, the rotary pyrolysis oven of this system is to carry out medium temperature pyrolysis to organic matter under anaerobic or anoxia condition, due to this
Process is to carry out in reducing atmosphere, can avoid generating dioxin, and with being pyrolyzed, high-efficient, equipment is simple, breeze low output
The characteristics of；In addition, the rotary pyrolysis oven can adjust the residence time of material pyrolysis according to the physicochemical property of material, design is used
Optimum speed operation, fully ensures that pyrolysis efficiency, can match frequency control motor, using frequency control, use is more flexible.
4, the level-one ultrafiltration apparatus, two-stage ultrafiltering device of this system are immersion ultrafiltration apparatus, immersion ultrafiltration technology
It is most economical, technique that energy consumption is minimum in current isolation of purified technique, is widely used, technology maturation.Immersion ultrafiltration has such as
Lower advantage:
A) effluent quality of submerged ultrafiltration is good, and water stabilization, delivery turbidity is usually less than 1NTU.
B) use scope is wide, easy cleaning.Membrane material is PVDF (Kynoar) material, and chemical resistance is very strong, is applicable in model
It encloses very extensive.Online or offline cleaning is carried out when component can be filtered in time.
C) low energy consumption, high-efficient.In about 0.02m3It include 10m in space2Hollow-fibre membrane.Membrane module immerses in water, can
Keep high-throughput under the low pressure of 0.05MPa, therefore energy consumption is very low.
D) filtering accuracy height, not fracture of wire.The doughnut used has the uniformly aperture less than 0.05 μm, can remove
Microorganism, colloid, algae and other cause muddy substance.And due to TiO2The reason of hydridization, the tensile resistance of film wire
Much it is better than common pvdf membrane.
E) occupied area is small.The solid-liquid separating equipments such as precipitating, filtering need not be set up, keeps whole system process simple, is easy to
Integrated, system footprint greatly reduces.
F) it is low that simple and convenient, high degree of automation, operating cost are managed.It is not required to set sterilizing equipment decontaminating apparatus, is not required to dosing.Complete machine energy
Enough realize automatic intermittent operation.
5, the evaporation and crystallization system of this system includes MVR (Mechanical Vapor Recompression) evaporator,
The evaporation and crystallization system can use MVR evaporation technology technology, while by the steam condensate generated in MVR vapo(u)rization system return to
Dissolved salt tank dissolves the inorganic salts after pyrolysis, so that steam condensate has carried out cycling and reutilization, reduces in dissolution system
The dosage of industry water reduces public work consumption.
6, the waste heat boiler with flue gas of this system white device that disappears are connected setting, and the flue gas white device that disappears can utilize waste heat
Boiler generate low-pressure steam to flue gas carry out backheat disappear it is white processing then discharge again, both taken full advantage of the steam of waste heat boiler
Resource, reduces energy consumption, and it is white also to have achieved the effect that flue gas disappears, while also reducing flue gas and disappearing white equipment investment.
Detailed description of the invention
Fig. 1 is the structure connection diagram of present system.
Specific embodiment
Below with reference to the invention will be further described by specific embodiment, following embodiment be it is descriptive, no
It is restrictive, this does not limit the scope of protection of the present invention.
The structure that the present invention is not described in detail specifically can be understood as the conventional structure of this field.
A kind of abraum salt recycling treatment disposal system, as shown in Figure 1, the system comprises be sequentially connected the abraum salt for connecing setting
Charing pyrolysis system, the slag of salt containing charcoal dissolution filter system and evaporation divide salt system, the charing pyrolysis system energy of the abraum salt
It is enough that charing pyrolysis processing is carried out to the abraum salt I being made of sodium chloride, sodium sulphate monomer salt or mixed abraum salt, and can be to tail gas
Handle simultaneously qualified discharge；The dissolution filter system of the slag of salt containing charcoal can charing pyrolysis system to abraum salt treated
The slag of salt containing charcoal dissolved, filter operation；After the evaporation divides salt system can be to the processing of the dissolution filter system of the slag of salt containing charcoal
Strong brine be evaporated concentration, fractional crystallization and drying process, obtain product salt.
In the present embodiment, the charing pyrolysis system of the abraum salt includes conveying system, rotary pyrolysis oven, combustion system
And exhaust treatment system, the input terminal of the conveying system can input abraum salt I to be processed, the output end of the conveying system with
The input terminal of rotary pyrolysis oven is connected setting, and the output end of the rotary pyrolysis oven includes the slag output end of salt containing charcoal and pyrolysis
Gas output end, the slag output end of salt containing charcoal are connected setting with the dissolution filter system of the slag of salt containing charcoal, the pyrolysis gas output
Hold the setting that is connected with exhaust treatment system；The input terminal of the combustion system is connected setting with natural gas, the combustion system
Output end be also connected with the input terminal of rotary pyrolysis oven setting；
The exhaust treatment system includes dual firing chamber, waste heat boiler, chilling tower, bag filter, forecooler, two-stage washing
Tower, flue gas disappear white device, chimney and circulating water chennel, and the dual firing chamber includes input terminal and flue gas output end, the dual firing chamber it is defeated
Entering end includes natural gas input, pyrolysis gas input terminal and ammonium hydroxide input terminal, and the natural gas input is connected with natural gas
Setting can input natural gas by the natural gas input into dual firing chamber, the pyrolysis gas input terminal of the dual firing chamber with return
The pyrolysis gas output end of rotatable pyrolysis oven is connected setting, and the ammonium hydroxide input terminal is connected setting with ammonium hydroxide, passes through the ammonium hydroxide
Input terminal can input ammonium hydroxide into dual firing chamber；
The input terminal of the waste heat boiler includes soft water input terminal and flue gas input terminal, and the output end of the waste heat boiler includes
Steam output end and flue gas output end, the flue gas input terminal of the waste heat boiler is connected with the flue gas output end of dual firing chamber to be set
Set, the soft water input terminal of the waste heat boiler is connected setting with soft water, by the soft water input terminal can into waste heat boiler it is defeated
Enter soft water, the steam output end of the waste heat boiler and evaporation point salt system, the flue gas white device that disappears are connected setting；
The input terminal of the chilling tower includes flue gas input terminal and quencher input terminal, the flue gas input terminal of chilling tower with it is remaining
The flue gas output end of heat boiler is connected setting, and the quencher input terminal is connected setting with quencher, passes through the quencher
Input terminal can input quencher into chilling tower, and the output end of the chilling tower is connected with the input terminal of bag filter to be set
It sets, is provided with active carbon input terminal on the pipeline between the output end of chilling tower, bag filter, passes through the active carbon input terminal
Active carbon, the output end of the bag filter can be inputted into the pipeline between the output end, bag filter of chilling tower
Be connected setting with the input terminal of forecooler, and the output end of the forecooler is connected setting with the input terminal of two-stage scrubbing tower；
The output end of the two-stage scrubbing tower includes waste water output end and flue gas output end, the waste water of the two-stage scrubbing tower
Output end and the input terminal of evaporation point salt system, circulating water chennel are respectively connected with setting, the flue gas output end of the two-stage scrubbing tower
It is connected setting with the disappear input terminal of white device of flue gas, the flue gas output end of white device that disappears is connected with the input terminal of chimney and sets
It sets, the output end of the chimney can export the flue gas of qualified discharge；
The output end of the circulating water chennel is connected setting with the input terminal of two-stage scrubbing tower, which can be to two
Lye is inputted in grade scrubbing tower, which can reach discharge standard for the contaminant removal in flue gas.
In the present embodiment, the conveying system uses screw feeding structure, matching setting frequency control motor, discharging system
System equally uses screw feeding structure；More preferably, the screw feeding structure and material contact portion use Stainless steel 316 L material
Matter；
Alternatively, the combustion system is combustor, for providing heat for pyrolysis oven, fuel is using natural gas, more preferably,
It is assembled inside the combustion chamber of the combustor using refractory material, frame is made using fashioned iron in centre, and has insulating layer, and outside is adopted
It is closed with color steel plate；
Alternatively, the scrubbing tower is wet scrubber tower, which can remove sour gas.
In the present embodiment, the pyrolytic process of abraum salt is in 550 DEG C~600 DEG C, anoxic item in the rotary pyrolysis oven
Under part, so that the organic matter in abraum salt is generated incomplete oxidation, be decomposed into CH4/CO/H2And coke.Since reaction temperature is low, it is not easy
Generate dioxin-like chemical.More preferably, the rotary pyrolysis oven is pyrolyzed using two sections formula pyrolysis oven, upper section pyrolysis
Furnace pyrolysis temperature is 400-500 DEG C, is low temperature drying process, and lower section is 550 DEG C~600 DEG C high temperature pyrolysis processes of pyrolysis temperature.
In the present embodiment, the pyrolysis gas generated in the abraum salt pyrolytic process in the rotary pyrolysis oven can contain part
Toxic gas, it is necessary to burn, the pyrolysis smoke that pyrolysis oven generates is passed through dual firing chamber and is heated up to 1100 DEG C or more, and two
It fires indoor stop 2 seconds or more, makes exhaust gas full combustion, complete oxidation CO2With H2O；For dual firing chamber generate high-temperature flue gas into
The high-temperature flue gas that dual firing chamber is discharged is passed through waste heat boiler and carries out heat recovery, recycles heat through waste heat boiler by row heat recovery
Afterwards, flue-gas temperature is down to 550 DEG C or so by original 1100 DEG C and is wanted into chilling tower for the chance of reduction " dioxin " synthesis
Flue gas is reduced in 200~500 DEG C of residence time, the measure taken is " chilling ".Chilling tower has both the effect of cooling and depickling,
Cooled down using atomizing chilling tower to tail gas, quencher uses limewash, can react, can effectively go with the sour gas in tail gas
Except HCl, SOx, NOx etc. in tail gas.Residence time of the flue gas in chilling tower is less than 1s, the flue-gas temperature come out from chilling tower
220 DEG C are down to by original 550 DEG C or so.Through cool down and depickling after flue gas enter bag filter, the flue gas after dedusting into
Enter wet process deacidification system, the SO in flue gas2, HCl and NaOH solution further neutralize, the pollutant in flue gas is fully achieved at this time
Discharge standard, but temperature is relatively low, also needs the white device heating that disappears by flue gas, avoids dew point corrosion and white cigarette from generating, by heating
Flue gas chimney standard discharge is sent to by air-introduced machine.
In the present embodiment, the bag filter selects high temperature resistant material, and the exhaust temperature into cloth bag is controlled 220
± 5 DEG C, filter bag is caused to block to avoid acid mist condensation or condensation vapor；
Alternatively, the chilling tower is half dry type chilling tower (half dry type gas washing)；Alternatively, the cleaning solution of the two-stage scrubbing tower
Interior mixing is provided with catalyst (CuCl2) and chelating agent, promote more water-soluble HgCl2It generates, then has been inhaled with chelating agent fixation
Receive the circulation fluid of mercury.
A kind of feasibility analysis up to standard of flue gas emission is as follows:
Sour gas control technology
For the sour gas in tail gas, depickling cooling is carried out to the tail gas that combustion system generates using semidry method, specifically
Method is to spray into limewash using atomizing chilling tower to react deacidification with sour gas, and the limewash of penetrating has cooling down simultaneously
Effect.
In order to ensure flue gas can reach emission request, the further desulfurization of two-stage scrubbing tower is used after bag-type dust.From
In forecooler come out flue gas enter wet scrubber tower A, flue gas is passed through from wash tower bottoms, in flue gas uphill process with sprinkling
Alkaline solution meet, neutralization reaction occurs for the sour gas in flue gas and alkaline solution:
2NaOH+SO2→Na2SO3+H2O
It is actually to utilize Na that wet type sodium alkali, which absorbs,XH2-XSO3Process that (X=1~2) constantly recycle absorbs in flue gas
SO2, acid salt NaHSO generated in absorption process3To SO2Without absorbability, with the progress of absorption process,
NaHSO in absorbing liquid3Quantity increases, the absorbability decline of absorbing liquid, therefore lye need to be supplemented into absorbing liquid, makes part
NaHSO3It is converted into Na2SO3, keep Na in absorbing liquid2SO3The relatively stable absorbability to keep absorbing liquid of concentration ratio.
The SO contained in flue gas simultaneously3, the sour gas such as HCl can also be absorbed agent absorption simultaneously, following reaction occurs:
Therefore, in sodium alkali sulfur removal technology the absorber portion on absorption tower by the SO in flue gas2Absorb, obtain sodium sulfite or
Product and a small amount of sodium sulphate and sodium chloride among sodium hydrogensulfite.Flue gas is reached the contaminant removal in flue gas by two-stage scrubbing tower
To discharge standard.
The sour gas of this system by the half dry type depickling of chilling tower to the removal efficiency of sour gas about 90% with
On, along with the secondary response that pharmacy response carries out on bag filter surface, whole system can be improved, sour gas is gone
Except rate (HCl98%, SOx90% or more), in addition, subsequent two-stage wet scrubber tower by lye spray in a manner of in scrubbing tower into
Row acid-base neutralization reaction removes the hydrogen chloride in flue gas from flue gas, the removal efficiency of wet scrubber tower up to 95% or more,
It can remove a variety of sour gas such as hydrogen sulfide, sulfur dioxide simultaneously.The pickling waste waters of formation (can contain sodium hydrogensulfite, sulfurous acid
The mixed liquor of the acid salinity of sodium) pH adjusted heel row to evaporation and crystallization system front end, mixes with condensed water as salinated water, warp
After precipitating filtering, into evaporation element.Realize production wastewater zero discharge.
·NOXPollution control technology
Generated nitrogen oxides is largely divided into 3 kinds in combustion process, and fuel nitrogen oxides (Fuel NOx), source is
Nitrogen component combustion in fuel generates, wink formula nitrogen oxides (PromptNOx), be CO in flame and nitrogenous organic gas from
Son effect generates and hot type nitrogen oxides (Thermal NOx), is under the hot environment more than 1500 DEG C in air
Nitrogen and oxygen self-acting generate, in the present system since what is taken is the rotary pyrolysis oven drying of first segment, second segment time
The cleaning pyrolysis way of rotatable pyrolysis oven pyrolysis, therefore the generation of nitrogen oxides is seldom, furthermore only 1100 DEG C of the temperature of dual firing chamber,
Far away from 1500 DEG C, therefore there is no hot type formation of nitrogen oxides substantially.
In the present system, SNCR method can be used, by spraying ammonium hydroxide in dual firing chamber, in 850~1050 DEG C of region,
NOXIt is reacted with ammonia and is reduced to N2.There is no the NH3 of fully reacting to react with the HCl in flue gas and generates NH4Cl, it is remaining in flue gas
NH3Generally less than 10 × 10-6.Currently, SNCR is most widely used in flue gas purification system, U.S.EPA, European Union be equal
Recommend using SNCR as solid waste incineration fume denitrating technique.
The control technology of flue dust (Dust)
The flue dust prevention and treatment of this system is to select suitable cloth bag using bag-type dust and the dual dust removal design of wet scrubber tower
99.9% dust pollution object can be substantially effectively removed, bag-type dust is also uniquely to be proved that PM2.5 can be effectively removed at present
Equipment, small particles can also be gathered into big grain using sorptive force of the water to flue dust by flue dust by the wet scrubber tower after bag-type dust
Son is washed in recirculated water and is discharged.
Bag filter selects high temperature resistant material, and the exhaust temperature into cloth bag is controlled at 220 DEG C or so, to avoid acid mist
Condensation or condensation vapor cause filter bag to block.
Volatile organic matter (VOCs)
Organic matter of the link that VOCs may occur in this system in the stage of abraum salt drying, abraum salt may evaporate
As thermal current enters in dual firing chamber together.In the dual firing chamber that flue gas enters high temperature, under sufficient air effect, wave
Volatile material and pyrolysis gas, which are fully burned to be converted into, to be stablized harmless carbon dioxide and water and discharges its thermal energy.
Heavy metal control technology
Bag filter and chilling tower (half dry type gas washing) and used time, except mercury, to the removal effect ten of heavy metal
Divide excellent.Mercury metal is not easy to condense since its saturated vapor pressure is higher, for the concentration of emission for reducing mercury, sprays before bag filter
Enter active carbon to reinforce the suction-operated to mercury metal, and in wet processing operation, can add in the cleaning solution of scrubbing tower
Enter catalyst (CuCl2), promote more water-soluble HgCl2It generates, then with the fixed circulation fluid for having absorbed mercury of chelating agent.
Dioxin (Dioxin) control technology
This system designs dual firing chamber in pyrolysis oven rear end, enters dual firing chamber after flue gas self-pyrolysis fire grate goes out after pyrolysis immediately,
Enough air and auxiliary fuel are passed through in dual firing chamber to be mixed and burned flue gas wherein to 1100 DEG C flue gas and enables it
Stop 2 seconds or more, so that organic matter is fully converted to harmless CO2And H2O, and be sufficiently destroyed issuable dioxin and two and dislike
English predecessor.Because the calorific value of the volatile materials and pyrolysis gas that come out from pyrolysis oven is lower, it is not enough to that secondary furnace temperature is maintained to exist
On 1100 DEG C, it is therefore desirable to which dual firing chamber provides additional auxiliary fuel and combustion air to provide enough thermal energy.Dual firing chamber goes out
The high-temperature flue gas of mouth enters waste heat boiler recycling heat immediately.Flue gas through waste heat boiler recycle heat after, into chilling tower cooler,
Depickling subsequently enters bag filter, adds active carbon powder injection device in the flue before entering bag-type dust collector,
Powdered Activated Carbon is periodically sprayed into flue gas makes active carbon form carbon dust layer in cloth bag surface, can effectively be adsorbed using this carbon dust layer
Dioxin, theoretically in dual firing chamber the residence time 2 seconds or more under 1100 DEG C of conditions of high temperature, dioxin is broken flue gas
Bad, active powdered carbon cooperation bag-type dust will ensure that no dioxin.Active carbon is according to 200mg/Nm3Flue gas dosage is added.
In the present embodiment, the dissolution filter system of the slag of salt containing charcoal includes dissolved salt tank, level-one ultrafiltration apparatus, breeze receipts
Storage, two-stage ultrafiltering device and trace solid residue collector, the input of the output end and dissolved salt tank of the rotary pyrolysis oven
End is connected setting, and the output end of the dissolved salt tank is connected setting with the input terminal of level-one ultrafiltration apparatus, dissolved salt tank, level-one ultrafiltration
It is connected on pipeline between device and precipitating reagent input terminal is set, it can be super to dissolved salt tank, level-one by the precipitating reagent input terminal
It filters and inputs precipitating reagent in the pipeline between device, the output end of the level-one ultrafiltration apparatus includes that breeze output end and strong brine are defeated
Outlet, the breeze output end of the level-one ultrafiltration apparatus are connected setting with the input terminal of breeze collector, the breeze collector
Output end be connected with dual firing chamber setting, the breeze filtered out, which is delivered to dual firing chamber, further to burn；The level-one ultrafiltration
The strong brine output end of device is connected setting with the input terminal of two-stage ultrafiltering device, level-one ultrafiltration apparatus, two-stage ultrafiltering device
Between pipeline on be connected precipitating reagent input terminal be set, can be to level-one ultrafiltration apparatus, second level by the precipitating reagent input terminal
Precipitating reagent is inputted in pipeline between ultrafiltration apparatus；
The output end of the two-stage ultrafiltering device includes residue output end and strong brine output end, the two-stage ultrafiltering device
Residue output end is connected setting with trace solid residue collector, the trace solid residue in the trace solid residue collector
It can be transported to cement kiln comprehensive utilization outside or transfer to the processed in units with related qualification.
In the present embodiment, the dissolution filter system of the slag of salt containing charcoal further includes that chemical medicine system (is not shown in figure
Out), the chemistry medicine system and the mating setting of dissolved salt tank, with remove in abraum salt heavy metal ion that may be present or other it is miscellaneous from
Sub (such as calcium, magnesium)；
Alternatively, the level-one ultrafiltration apparatus, two-stage ultrafiltering device are immersion ultrafiltration apparatus.
In the present embodiment, the evaporation point salt system includes carbonating column, magma thickener and evaporation and crystallization system, institute
The input terminal for stating carbonating column includes strong brine input terminal and CO2Input terminal, the strong brine input terminal and second level of the carbonating column
The strong brine output end of ultrafiltration apparatus is connected setting, the CO of the carbonating column2Input terminal and CO2Be connected setting, by this
CO2Input terminal can input CO into carbonating column2, the output end of the carbonating column is connected with the input terminal of magma thickener
Setting, the output end of the magma thickener includes NaHCO3Output end and magma output end, the NaHCO3Output end can export
NaHCO3Crude product, the NaHCO3Crude product can obtain NaHCO after centrifugation, drying, packaging operation3Product；The magma output end
Be connected setting with the input terminal of evaporation and crystallization system, and the output end of the evaporation and crystallization system includes that condensed water output end and salt are defeated
Outlet, the condensed water output end can export condensed water after processing, which distinguishes phase with dissolved salt tank, water storage tank
Connection setting, the salt output end can export finished product salt, for example, NaCl, anhydrous sodium sulphate, KCl, Ca (NO3)2Deng；
The strong brine output end of the two-stage ultrafiltering device is also directly connected with the input terminal of evaporation and crystallization system setting,
Sour input terminal is set on the pipeline between two-stage ultrafiltering device, evaporation and crystallization system, it can be super to second level by the acid input terminal
Filter input acid in the pipeline between device, evaporation and crystallization system.
In the present embodiment, the evaporation and crystallization system includes MVR (Mechanical Vapor Recompression)
Evaporator, alternatively, the evaporation and crystallization system includes MVR (the Mechanical Vapor of setting of being connected
Recompression) evaporator and single effect evaporator.
The evaporation and crystallization system of this system includes MVR (Mechanical Vapor Recompression) evaporator, will
The steam condensate generated in MVR vapo(u)rization system is returned to dissolved salt tank, is dissolved to the inorganic salts after pyrolysis, so that steam is solidifying
Liquid has carried out cycling and reutilization, while decreasing the dosage of industry water in dissolution system, reduces public work consumption；Separately
Outside, the technique that can be combined using MVR evaporation technique+single effect evaporation to the separation of mixed inorganic carries out fractional crystallization.First
In MVR evaporation system, Na2SO4 is first subjected to Crystallization Separation under worst hot case, post mother liquor by decompression cooling, in list
NaCl is subjected to Crystallization Separation again under effect vapo(u)rization system worst cold case, to reach solventing-out.
In the present embodiment, the disposal system further includes abraum salt II disposal system (according to the reality for the abraum salt that the later period collects
Border situation is configured), described its main component of abraum salt II is saltcake and a small amount of chromic salts, is free of organic pollutant, therefore, abraum salt
II is without carrying out pyrolysis processing.The abraum salt II disposal system includes the molten system of acid and exclusion device, the molten system of acid it is defeated
Abraum salt II can be inputted by entering end, and the input terminal of the exclusion device includes that the molten treatment fluid input terminal of acid and reducing agent/precipitating reagent are defeated
Enter end, the output end of the molten system of acid is connected setting with the sour molten treatment fluid input terminal of exclusion device, the exclusion device
Reducing agent/precipitating reagent input terminal is connected setting with reducing agent/precipitating reagent, can be to by the reducing agent/precipitating reagent input terminal
Inputting reducing agent/precipitating reagent in exclusion device, the output end of the exclusion device includes impurity filter residue output end and filtrate output end,
The impurity filter residue output end can export impurity filter residue, the filtrate output end of the exclusion device and evaporation and crystallization system it is defeated
Enter end to be connected setting.
A kind of working principle and process of abraum salt recycling treatment disposal system of the present invention are as follows:
Sodium chloride, sodium sulphate monomer abraum salt and its mixing abraum salt that this system is generated suitable for industrial processes
Recycling treatment.In process of production, according to the difference of abraum salt type, abraum salt I and two class of abraum salt II are roughly divided into.Abraum salt I: main
If being made of sodium chloride, sodium sulphate monomer salt or mixed abraum salt.The part abraum salt is according to the difference of ingredient type, through medium temperature
Pyrolysis charring, dissolution filter respectively enter different evaporations and divide salt process, finally obtain the higher product salt of purity.Abraum salt II
Its main component is saltcake and a small amount of chromic salts, is free of organic pollutant, and therefore, abraum salt II is without carrying out pyrolysis processing.This system
Technologically advanced, easily operated, product quality is controllable, it can be ensured that the overall process recycling of abraum salt.
1, in factory abraum salt conveying
The abraum salt for being temporarily stored into warehouse is transported to pyrolysis workshop by fork truck, then is promoted to feed inlet, abraum salt by lifting device
Mixed salt pond is fallen into feed inlet, after compatibility, by helical feed to pyrolysis oven feed well, feed well lower end connects helical feed
Machine, the charging rate that abraum salt is set are sent to pyrolysis oven.The present invention more preferably uses screw feeding structure, distribution transforming frequency modulation
Speed motor, discharge system equally use screw feeding structure.Screw conveyor and material contact portion use Stainless steel 316 L material
Matter.
2, the charing pyrolysis of abraum salt
The pyrolytic process of abraum salt is a complicated chemical reaction process, fracture, isomerization of the key comprising macromolecular etc.
Chemical reaction.In pyrolytic process, for in-between product there are two kinds of variation tendencies, on the one hand they become small molecule from macromolecular
The even cracking process of gas, the polymerization process on the one hand thering is small molecule to aggregate into bigger molecule again.Pyrolytic process includes cracking
Reaction, dehydrogenation reaction, hydrogenation reaction, condensation reaction, bridged bond decomposition reaction etc..
The charing pyrolysis system of abraum salt includes conveying system, pyrolysis oven, combustion system, exhaust treatment system.What is generated is useless
Salt by dedicated dangerous waste haulage vehicle collect to warehouse it is temporary after, abraum salt is sent to pyrolysis oven and is carbonized by screw feeding structure
Pyrolysis, pyrolysis oven match frequency control motor.The pyrolytic process of abraum salt is made in abraum salt under 550 DEG C~600 DEG C, anoxia condition
Organic matter generate incomplete oxidation, be decomposed into CH4/CO/H2 and coke.Since reaction temperature is low, it is not likely to produce dioxin
Substance.This system can design 2 sets of parallel pyrolysis systems, and the pyrolytic process of every set pyrolysis system carries out in two stages.
The generation of abraum salt pyrolytic process is flammable large-minded, especially in the higher situation of temperature, the 50% of organic principle in abraum salt
It is all converted to gaseous products above.These products are with H2、CO、CH4Based on, calorific value is up to 6.37 × 103~1.021 ×
104kJ/kg.In addition to needed for small part supply pyrolytic process from the mount of using heat, most of gas becomes combustible gas product.Due to useless
Salt belongs to dangerous waste, therefore pyrolysis gas can not be utilized directly, it is necessary to carry out burning processing, make toxic gas full combustion therein
Carbon dioxide and water.
3, the dissolution filter of the slag of salt containing charcoal
After rotary pyrolysis oven pyrolysis charring, the organic matter in abraum salt is removed abraum salt, is obtained containing a small amount of coke (charcoal
Slag) inorganic salts.The inorganic salts containing charcoal that pyrolysis system is obtained are dissolved in the distilled water of heat, and are filtered by immersion ultrafiltration technology
After breeze, strong brine is obtained.Dual stage filter apparatus is arranged in dissolution filter unit, by adding precipitating reagent (such as lye), removes
Heteroion.After double-filtration purifies, according to the ingredient of inorganic salts contained in strong brine, selection enters corresponding vapo(u)rization system.
The breeze filtered out, which is sent to dual firing chamber, further to burn.To avoid incombustible from accumulating in system, periodically dissolution filter unit is arranged
Solid slag (predominantly inorganic salts precipitating) centralized collection out transfers to the processed in units with related qualification.
In addition, its main component of such abraum salt is saltcake and a small amount of chromic salts, without organic for being difficult to water-soluble abraum salt II
Pollutant, such abraum salt is acidified, reduction and precipitation process, isolate heteroion, after exclusion device, obtained sulphur
Acid sodium-salt solution is mixed into vapo(u)rization system with the salting liquid handled by pyrolysis charring and dissolution filter, crystallizes out salt.Dissolved salt
Tank can the chemical medicine system of mating setting, with remove in abraum salt heavy metal ion that may be present or other heteroions (such as calcium,
Magnesium etc.).
4, evaporation divides salt process
Abraum salt handles removal organic matter through pyrolysis charring, then after dissolution filter removes breeze, and the strong brine of formation enters
Vapo(u)rization system forms product salt by evaporation and concentration, fractional crystallization and drying.According to expected abraum salt type, using different several
Item divides salt route.
It (1) is the abraum salt of single inorganic salts ingredients: the dense salt after pyrolysis charring, dissolution filter for raw material, using MVR
Evaporating and concentrating process is evaporated (sodium chloride crystallization temperature is 90-95 degree, sulfate crystal temperature 85-90 degree), crystallizes out list
Component inorganic salts
(2) for the abraum salt of sodium chloride-containing, sodium sulphate bi-component inorganic salt: gained is dense after pyrolysis charring, dissolution filter
Saline solution enters solventing-out system, by fractional crystallization technique, crystallizes out NaCl, Na2SO410H2O respectively at different processes,
NaCl obtains product NaCl salt through fluidized bed drying after packing.Na2SO410H2O is then sent to one pack system vapo(u)rization system, removal knot
Brilliant water, to prepare anhydrous sodium sulfate.
(3) for the abraum salt of tri- kinds of component of inorganic salts containing NaCl-Na2SO4-Na2CO3: (being lower than Na2CO3 content is lower
0.5%) in the case where, by adding sulfuric acid to dissolution filter unit, Na2CO3 is made to be converted into Na2SO4, and then pass through sal prunella point
Sodium chloride product salt, anhydrous sodium sulphate are obtained respectively from purification route.For tri- kinds of component of inorganic salts containing NaCl-Na2SO4-Na2CO3
Abraum salt, in the higher situation of Na2CO3 content, evaporation element setting carbonating column divide salt system, to isolate NaHCO3。
The main function of carbonating column is to convert Na2CO3 contained in waste water to NaHCO3, and then realize carbonate and sulphur
The separation of hydrochlorate/sodium chloride salt.By blasting CO2 into waste water, so that Na2CO3 in system is fully converted to NaHCO3, make
NaHCO3 is precipitated from system first, to realize the separation of carbonate, the salting liquid after reaction with NaHCO3 crystal is (brilliant
Slurry) it is discharged from carbonization tower bottom, into magma thickener, crystal and salting liquid is made to carry out initial gross separation.Magma thickener top
Clear liquid (filtrate), which overflows in filtrate storage tank, to be collected, and sodium carbonate, carbonization separation stepmother are generated after sodium bicarbonate heat drying
Liquid returns to evaporation leading portion；Subsequently into corresponding NaCl-Na2SO4 evaporation and crystallization system, further desalting processing is carried out.Through thickening
Magma from flow into whizzer be further dehydrated.Dewatered crystal is transported to gas flow dryer and is dried, and does
Product after dry can enter product packaging line and carry out last packaging, obtain the pure salt of product sodium carbonate, the pure salt of product sodium chloride and
Anhydrous sodium sulphate.
5, vent gas treatment
Pyrolysis system generates vent gas treatment mode and removes for dual firing chamber's burning, the cooling of waste heat boiler heat recovery, chilling, cloth bag
Dirt, two-stage spray washing, flue gas heat exchange take off white.
The pyrolysis smoke that abraum salt pyrolysis generates in production process is passed through dual firing chamber and is heated up to 1100 DEG C or more, keeps exhaust gas abundant
Burning, complete oxidation are CO2 and H2O；Enough air and auxiliary fuel are passed through in dual firing chamber makes flue gas to 1100 DEG C
Pyrolysis gas is mixed and burned wherein and enables its stop 2 seconds or more, so that pernicious gas thoroughly decomposed, burnt, is fully converted to harmless
CO2And H2O, and it is sufficiently destroyed issuable dioxin and dioxin predecessor.Theoretically it is in flue gas dual firing chamber
1100 DEG C -1200 DEG C the condition of high temperature lower residence time 2 seconds or more, dioxin has been destroyed.Dual firing chamber is (for example, dual firing chamber is main
Component may include: that cylinder is rolled with steel plate, and liner is corrosion-resistant, and refractory brick resistant to high temperature sets temperature point, pressure-measuring-point, contains
Oxygen amount measuring point, burner opening, observation panel, sets explosion proof door and dump chimney at the top of dual firing chamber at overfiren air port) high temperature of outlet
Flue gas is worth with recuperation of heat, process steam needed for generalling use waste heat boiler Mist heat recovering and producing regenerative process.
For the high-temperature flue gas of dual firing chamber's discharge after waste heat boiler carries out heat exchange, temperature is down to 550 by original 1100 DEG C
DEG C or so enter chilling tower, for reduction " dioxin " synthesis chance, to reduce flue gas in 200~500 DEG C of residence time, adopt
The measure taken is " chilling ".Chilling tower has both the effect of cooling and depickling, is cooled down using atomizing chilling tower to tail gas, quencher is adopted
It with limewash, can be reacted with the sour gas in tail gas, HCl, SOx, NOx etc. in tail gas can be effectively removed.Flue gas is in urgency
Residence time in cold tower is less than 1s, and the flue-gas temperature come out from chilling tower is down to 220 DEG C by original 550 DEG C or so.Through dropping
Flue gas after mild depickling enters bag filter, thus the flue-gas temperature due to entering bag filter may be used at 200 DEG C or more
Bag filter dew condensation phenomenon is avoided, the pre-cooled device of the flue gas after dedusting enters wet process deacidification system, the SO in flue gas2, HCl with
NaOH solution is further neutralized and is removed.
The dual dust removal design of bag-type dust and wet scrubber tower, and select suitable cloth bag that can substantially effectively remove
99.9% dust pollution object, bag-type dust is also the equipment for being uniquely proved that PM2.5 can be effectively removed at present, after bag-type dust
Wet scrubber tower small particles can also be gathered into big particle to the sorptive force of flue dust using water by flue dust and wash in recirculated water and arrange
Out.Sour gas in flue gas is anti-carrying out acid-base neutralization in scrubbing tower in the way of lye spray by wet scrubber tower
The hydrogen chloride in flue gas should be made to remove from flue gas, the removal efficiency of wet scrubber tower can remove chlorine up to 95% or more
Change a variety of sour gas such as hydrogen, sulfur dioxide.
After the processing of above-mentioned chilling, dedusting and washing, purifying, discharge standard, but temperature is fully achieved in the pollutant in flue gas
It spends relatively low, also needs the white device that disappears by flue gas, avoid dew point corrosion and white cigarette from generating, sent by the flue gas of heating by air-introduced machine
Toward chimney standard discharge.
Although disclosing the embodiment of the present invention for the purpose of illustration, it will be appreciated by those skilled in the art that: not
Be detached from the present invention and spirit and scope of the appended claims in, various substitutions, changes and modifications be all it is possible, therefore, this
The range of invention is not limited to the embodiment disclosure of that.
Claims (10)
1. a kind of abraum salt recycling treatment disposal system, it is characterised in that: the system comprises be sequentially connected the abraum salt for connecing setting
Charing pyrolysis system, the slag of salt containing charcoal dissolution filter system and evaporation divide salt system, the charing pyrolysis system energy of the abraum salt
It is enough that charing pyrolysis processing is carried out to the abraum salt I being made of sodium chloride, sodium sulphate monomer salt or mixed abraum salt, and can be to tail gas
Handle simultaneously qualified discharge；The dissolution filter system of the slag of salt containing charcoal can charing pyrolysis system to abraum salt treated
The slag of salt containing charcoal dissolved, filter operation；After the evaporation divides salt system can be to the processing of the dissolution filter system of the slag of salt containing charcoal
Strong brine be evaporated concentration, fractional crystallization and drying process, obtain product salt.
2. abraum salt recycling treatment disposal system according to claim 1, it is characterised in that: the charing of the abraum salt is pyrolyzed
System includes conveying system, rotary pyrolysis oven, combustion system and exhaust treatment system, and the input terminal of the conveying system can
Input abraum salt I to be processed, the output end of the conveying system is connected setting with the input terminal of rotary pyrolysis oven, this is rotary
The output end of pyrolysis oven includes the slag output end of salt containing charcoal and pyrolysis gas output end, the slag output end of salt containing charcoal and the slag of salt containing charcoal
Dissolution filter system is connected setting, and the pyrolysis gas output end is connected setting with exhaust treatment system；The combustion system
Input terminal be connected with natural gas setting, the output end of the combustion system, which is also connected with the input terminal of rotary pyrolysis oven, to be set
It sets；
The exhaust treatment system include dual firing chamber, waste heat boiler, chilling tower, bag filter, forecooler, two-stage scrubbing tower,
Flue gas disappears white device, chimney and circulating water chennel, and the dual firing chamber includes input terminal and flue gas output end, the input terminal of the dual firing chamber
Including natural gas input, pyrolysis gas input terminal and ammonium hydroxide input terminal, the natural gas input is connected setting with natural gas,
Natural gas, the pyrolysis gas input terminal of the dual firing chamber and rotary heat can be inputted into dual firing chamber by the natural gas input
The pyrolysis gas output end of solution furnace is connected setting, and the ammonium hydroxide input terminal is connected setting with ammonium hydroxide, passes through the ammonium hydroxide input terminal
Ammonium hydroxide can be inputted into dual firing chamber；
The input terminal of the waste heat boiler includes soft water input terminal and flue gas input terminal, and the output end of the waste heat boiler includes steam
Output end and flue gas output end, the flue gas input terminal of the waste heat boiler are connected setting with the flue gas output end of dual firing chamber, should
The soft water input terminal of waste heat boiler is connected setting with soft water, can be inputted into waste heat boiler by the soft water input terminal soft
Water, the steam output end of the waste heat boiler and evaporation point salt system, the flue gas white device that disappears are connected setting；
The input terminal of the chilling tower includes flue gas input terminal and quencher input terminal, the flue gas input terminal and waste heat pot of chilling tower
The flue gas output end of furnace is connected setting, and the quencher input terminal is connected setting with quencher, is inputted by the quencher
End can input quencher into chilling tower, and the output end of the chilling tower is connected setting with the input terminal of bag filter,
It is provided with active carbon input terminal on pipeline between the output end of chilling tower, bag filter, passes through the active carbon input terminal energy
It is enough to input active carbon into the pipeline between the output end, bag filter of chilling tower, the output end of the bag filter with
The input terminal of forecooler is connected setting, and the output end of the forecooler is connected setting with the input terminal of two-stage scrubbing tower；
The output end of the two-stage scrubbing tower includes waste water output end and flue gas output end, the waste water output of the two-stage scrubbing tower
End and the input terminal of evaporation point salt system, circulating water chennel are respectively connected with setting, the flue gas output end and cigarette of the two-stage scrubbing tower
The disappear input terminal of white device of gas is connected setting, and the flue gas output end of white device that disappears is connected setting with the input terminal of chimney,
The output end of the chimney can export the flue gas of qualified discharge；
The output end of the circulating water chennel is connected setting with the input terminal of two-stage scrubbing tower, which can wash to two-stage
It washs and inputs lye in tower, which can reach discharge standard for the contaminant removal in flue gas.
3. abraum salt recycling treatment disposal system according to claim 2, it is characterised in that: the conveying system uses spiral shell
Feeding structure, matching setting frequency control motor are revolved, discharge system equally uses screw feeding structure；
Alternatively, the combustion system is combustor, fuel uses natural gas；
Alternatively, the scrubbing tower is wet scrubber tower, which can remove sour gas.
4. abraum salt recycling treatment disposal system according to claim 2, it is characterised in that: in the rotary pyrolysis oven
The pyrolytic process of abraum salt is so that the organic matter in abraum salt is generated incomplete oxidation under 550 DEG C~600 DEG C, anoxia condition, decompose
For CH4/CO/H2And coke.
5. abraum salt recycling treatment disposal system according to claim 2, it is characterised in that: in the rotary pyrolysis oven
After the pyrolysis smoke of generation is passed through dual firing chamber, dual firing chamber is heated up to 1100 DEG C or more, and stops 2 seconds or more in dual firing chamber；Or
Person, the chilling tower are atomizing chilling tower, and quencher uses limewash, and residence time of the flue gas in chilling tower is less than 1s.
6. abraum salt recycling treatment disposal system according to claim 2, it is characterised in that: the bag filter selection
High temperature resistant material, the exhaust temperature into cloth bag are controlled at 220 ± 5 DEG C；
Alternatively, the chilling tower is half dry type chilling tower；Alternatively, mixing is provided with catalysis in the cleaning solution of the two-stage scrubbing tower
Agent and chelating agent.
7. abraum salt recycling treatment disposal system according to any one of claims 1 to 6, it is characterised in that: described to contain charcoal
The dissolution filter system of salt slag includes that dissolved salt tank, level-one ultrafiltration apparatus, breeze collector, two-stage ultrafiltering device and trace solid are residual
Slag collector, the output end of the rotary pyrolysis oven are connected setting with the input terminal of dissolved salt tank, the output end of the dissolved salt tank
Be connected setting with the input terminal of level-one ultrafiltration apparatus, and being connected on the pipeline between dissolved salt tank, level-one ultrafiltration apparatus, it is heavy to be arranged
Agent input terminal in shallow lake can input precipitating reagent into the pipeline between dissolved salt tank, level-one ultrafiltration apparatus by the precipitating reagent input terminal,
The output end of the level-one ultrafiltration apparatus includes breeze output end and strong brine output end, and the breeze of the level-one ultrafiltration apparatus is defeated
Outlet is connected setting with the input terminal of breeze collector, and the output end of the breeze collector is connected setting with dual firing chamber；Institute
It states the strong brine output end of level-one ultrafiltration apparatus and the input terminal of two-stage ultrafiltering device is connected setting, level-one ultrafiltration apparatus, two
It is connected on pipeline between grade ultrafiltration apparatus and precipitating reagent input terminal is set, it can be to level-one ultrafiltration by the precipitating reagent input terminal
Precipitating reagent is inputted in pipeline between device, two-stage ultrafiltering device；
The output end of the two-stage ultrafiltering device includes residue output end and strong brine output end, the residue of the two-stage ultrafiltering device
Output end is connected setting with trace solid residue collector, and the trace solid residue in the trace solid residue collector can
It is transported to cement kiln comprehensive utilization outside or transfers to the processed in units with related qualification.
8. abraum salt recycling treatment disposal system according to any one of claims 1 to 6, it is characterised in that: the evaporation
Point salt system includes carbonating column, magma thickener and evaporation and crystallization system, and the input terminal of the carbonating column includes strong brine
Input terminal and CO2Input terminal, the strong brine input terminal of the carbonating column are connected with the strong brine output end of two-stage ultrafiltering device
Setting, the CO of the carbonating column2Input terminal and CO2Be connected setting, passes through the CO2Input terminal can be defeated into carbonating column
Enter CO2, the output end of the carbonating column is connected setting with the input terminal of magma thickener, the output end packet of the magma thickener
Include NaHCO3Output end and magma output end, the NaHCO3Output end can export NaHCO3Crude product, the NaHCO3Crude product pass through from
NaHCO can be obtained after the heart, drying, packaging operation3Product；The magma output end is connected with the input terminal of evaporation and crystallization system
Setting is connect, the output end of the evaporation and crystallization system includes condensed water output end and salt output end, and the condensed water output end can
Condensed water after output processing, the condensed water output end and dissolved salt tank, water storage tank are respectively connected with setting, and the salt output end can
Export finished product salt；
The strong brine output end of the two-stage ultrafiltering device is also directly connected with the input terminal of evaporation and crystallization system setting, second level
Sour input terminal is set on the pipeline between ultrafiltration apparatus, evaporation and crystallization system, can be filled to two-stage ultrafiltering by the acid input terminal
It sets, input acid in the pipeline between evaporation and crystallization system.
9. abraum salt recycling treatment disposal system according to claim 8, it is characterised in that: the disposal system further includes
Abraum salt II disposal system, the abraum salt II disposal system include the molten system of acid and exclusion device, the input terminal of the molten system of acid
Abraum salt II can be inputted, the input terminal of the exclusion device includes the molten treatment fluid input terminal of acid and reducing agent/precipitating reagent input terminal,
The molten treatment fluid input terminal of acid of the output end of the molten system of acid and exclusion device is connected setting, the reduction of the exclusion device
Agent/precipitating reagent input terminal is connected setting with reducing agent/precipitating reagent, can be to removal of impurities by the reducing agent/precipitating reagent input terminal
Input reducing agent/precipitating reagent in device, the output end of the exclusion device includes impurity filter residue output end and filtrate output end, described
Impurity filter residue output end can export impurity filter residue, the filtrate output end of the exclusion device and the input terminal of evaporation and crystallization system
Be connected setting.
10. abraum salt recycling treatment disposal system as described in any one of claim 1 to 9 in terms of the abraum salt recycling treatment in
Application.
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| CN110790440A (en) * | 2019-12-09 | 2020-02-14 | 郭玉伟 | High COD high salt effluent disposal system |
| CN110805907A (en) * | 2019-10-16 | 2020-02-18 | 北京航化节能环保技术有限公司 | Process and device for treating solid waste salt cracking furnace containing water, organic matters and other soluble gases |
| CN110935718A (en) * | 2019-12-18 | 2020-03-31 | 汪瑜 | Industrial salt slag pretreatment system and pretreatment method thereof |
| CN110938838A (en) * | 2019-11-06 | 2020-03-31 | 东北大学 | Method for treating anode carbon slag of aluminum electrolysis cell by using NaCl molten salt extraction method |
| CN111112296A (en) * | 2019-12-27 | 2020-05-08 | 洛南环亚源铜业有限公司 | Resource utilization treatment method for industrial waste salt |
| CN111380060A (en) * | 2020-03-21 | 2020-07-07 | 深圳市海文环保技术有限公司 | Chemical waste salt harmless treatment system and method |
| CN111484365A (en) * | 2020-03-12 | 2020-08-04 | 山东清博生态材料综合利用有限公司 | Organic potash fertilizer prepared from waste potassium salt and preparation method thereof |
| CN111498871A (en) * | 2020-05-31 | 2020-08-07 | 湖南申联环保科技有限公司 | System and method for treating waste salt residues mixed by sodium sulfate and sodium chloride |
| CN111689634A (en) * | 2020-06-10 | 2020-09-22 | 南京工业大学 | Method for treating trichloropyridine sodium alcoholate wastewater |
| CN111790731A (en) * | 2020-07-20 | 2020-10-20 | 杭州碳氢科技研究有限公司 | Industrial waste salt conversion device and method |
| CN112320822A (en) * | 2020-10-20 | 2021-02-05 | 绍兴凤登环保有限公司 | Waste salt recycling treatment method |
| CN112390235A (en) * | 2020-11-26 | 2021-02-23 | 安道麦股份有限公司 | Treatment method of acephate rectification residual liquid |
| CN112984515A (en) * | 2021-03-29 | 2021-06-18 | 航天神禾(北京)环保有限公司 | Multistage atomizing spray gun, quench tower and waste salt recycling system |
| CN113510140A (en) * | 2021-08-17 | 2021-10-19 | 陕西省石油化工研究设计院 | Waste salt recycling treatment system and method |
| CN113562745A (en) * | 2021-07-07 | 2021-10-29 | 天津天一爱拓科技有限公司 | System and method for treating waste salt by using two-stage pyrolysis technology |
| CN113623661A (en) * | 2021-07-07 | 2021-11-09 | 天津天一爱拓科技有限公司 | Catalytic pyrolysis system and method for treating waste salt |
| CN114289478A (en) * | 2021-12-30 | 2022-04-08 | 连云港职业技术学院 | Resource treatment method for waste salt containing organic matters |
| CN114349026A (en) * | 2021-04-08 | 2022-04-15 | 李广柱 | Treatment process of high-risk waste salt |
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| CN110805907A (en) * | 2019-10-16 | 2020-02-18 | 北京航化节能环保技术有限公司 | Process and device for treating solid waste salt cracking furnace containing water, organic matters and other soluble gases |
| CN110805907B (en) * | 2019-10-16 | 2022-04-22 | 北京航化节能环保技术有限公司 | Process and device for treating solid waste salt cracking furnace containing water, organic matters and other soluble gases |
| CN110938838A (en) * | 2019-11-06 | 2020-03-31 | 东北大学 | Method for treating anode carbon slag of aluminum electrolysis cell by using NaCl molten salt extraction method |
| CN110938838B (en) * | 2019-11-06 | 2021-12-31 | 东北大学 | Method for treating anode carbon slag of aluminum electrolysis cell by using NaCl molten salt extraction method |
| CN110790440A (en) * | 2019-12-09 | 2020-02-14 | 郭玉伟 | High COD high salt effluent disposal system |
| CN110790440B (en) * | 2019-12-09 | 2024-03-26 | 郭玉伟 | High COD high salt wastewater treatment system |
| CN110935718B (en) * | 2019-12-18 | 2021-03-26 | 汪瑜 | Industrial salt slag pretreatment system and pretreatment method thereof |
| CN110935718A (en) * | 2019-12-18 | 2020-03-31 | 汪瑜 | Industrial salt slag pretreatment system and pretreatment method thereof |
| CN111112296A (en) * | 2019-12-27 | 2020-05-08 | 洛南环亚源铜业有限公司 | Resource utilization treatment method for industrial waste salt |
| CN111484365A (en) * | 2020-03-12 | 2020-08-04 | 山东清博生态材料综合利用有限公司 | Organic potash fertilizer prepared from waste potassium salt and preparation method thereof |
| CN111484365B (en) * | 2020-03-12 | 2022-05-27 | 山东清博生态材料综合利用有限公司 | Organic potash fertilizer prepared from waste potassium salt and preparation method thereof |
| CN111380060A (en) * | 2020-03-21 | 2020-07-07 | 深圳市海文环保技术有限公司 | Chemical waste salt harmless treatment system and method |
| CN111498871A (en) * | 2020-05-31 | 2020-08-07 | 湖南申联环保科技有限公司 | System and method for treating waste salt residues mixed by sodium sulfate and sodium chloride |
| CN111689634A (en) * | 2020-06-10 | 2020-09-22 | 南京工业大学 | Method for treating trichloropyridine sodium alcoholate wastewater |
| CN111790731A (en) * | 2020-07-20 | 2020-10-20 | 杭州碳氢科技研究有限公司 | Industrial waste salt conversion device and method |
| CN112320822A (en) * | 2020-10-20 | 2021-02-05 | 绍兴凤登环保有限公司 | Waste salt recycling treatment method |
| CN112390235A (en) * | 2020-11-26 | 2021-02-23 | 安道麦股份有限公司 | Treatment method of acephate rectification residual liquid |
| CN112984515B (en) * | 2021-03-29 | 2021-10-19 | 航天神禾(北京)环保有限公司 | Multistage atomizing spray gun, quench tower and waste salt recycling system |
| CN112984515A (en) * | 2021-03-29 | 2021-06-18 | 航天神禾(北京)环保有限公司 | Multistage atomizing spray gun, quench tower and waste salt recycling system |
| CN114349026A (en) * | 2021-04-08 | 2022-04-15 | 李广柱 | Treatment process of high-risk waste salt |
| CN113623661A (en) * | 2021-07-07 | 2021-11-09 | 天津天一爱拓科技有限公司 | Catalytic pyrolysis system and method for treating waste salt |
| CN113562745A (en) * | 2021-07-07 | 2021-10-29 | 天津天一爱拓科技有限公司 | System and method for treating waste salt by using two-stage pyrolysis technology |
| CN113510140A (en) * | 2021-08-17 | 2021-10-19 | 陕西省石油化工研究设计院 | Waste salt recycling treatment system and method |
| CN114289478A (en) * | 2021-12-30 | 2022-04-08 | 连云港职业技术学院 | Resource treatment method for waste salt containing organic matters |
| CN114289478B (en) * | 2021-12-30 | 2023-05-16 | 连云港职业技术学院 | Method for recycling waste salt containing organic matters |
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Application publication date: 20190906 |