CN102476029A - Catalyst-containing purifying apparatus used for processing organic waste gas - Google Patents
Catalyst-containing purifying apparatus used for processing organic waste gas Download PDFInfo
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- CN102476029A CN102476029A CN2010105726100A CN201010572610A CN102476029A CN 102476029 A CN102476029 A CN 102476029A CN 2010105726100 A CN2010105726100 A CN 2010105726100A CN 201010572610 A CN201010572610 A CN 201010572610A CN 102476029 A CN102476029 A CN 102476029A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 135
- 239000007789 gas Substances 0.000 title claims abstract description 114
- 239000010815 organic waste Substances 0.000 title claims abstract description 34
- 238000001179 sorption measurement Methods 0.000 claims abstract description 78
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 65
- 230000003647 oxidation Effects 0.000 claims abstract description 63
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 51
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 13
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000010457 zeolite Substances 0.000 claims abstract description 13
- 229910052751 metal Inorganic materials 0.000 claims abstract description 7
- 239000002184 metal Substances 0.000 claims abstract description 7
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 4
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims description 76
- 230000003197 catalytic effect Effects 0.000 claims description 64
- 238000004140 cleaning Methods 0.000 claims description 26
- 239000011572 manganese Substances 0.000 claims description 21
- 238000003795 desorption Methods 0.000 claims description 18
- 241001672694 Citrus reticulata Species 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 12
- 239000010949 copper Substances 0.000 claims description 12
- 230000000694 effects Effects 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 6
- 229910052802 copper Inorganic materials 0.000 claims description 6
- 229910052709 silver Inorganic materials 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 3
- 229910017052 cobalt Inorganic materials 0.000 claims description 3
- 239000010941 cobalt Substances 0.000 claims description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 239000011133 lead Substances 0.000 claims description 3
- 229910052748 manganese Inorganic materials 0.000 claims description 3
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 3
- 239000011733 molybdenum Substances 0.000 claims description 3
- 239000004332 silver Substances 0.000 claims description 3
- 239000010944 silver (metal) Substances 0.000 claims description 3
- 229910052725 zinc Inorganic materials 0.000 claims description 3
- 239000011701 zinc Substances 0.000 claims description 3
- 238000005187 foaming Methods 0.000 claims description 2
- 238000000746 purification Methods 0.000 abstract description 35
- 239000000126 substance Substances 0.000 description 23
- 239000000463 material Substances 0.000 description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 16
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 16
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 12
- 238000000034 method Methods 0.000 description 12
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 11
- 239000003344 environmental pollutant Substances 0.000 description 11
- 231100000719 pollutant Toxicity 0.000 description 11
- 238000003756 stirring Methods 0.000 description 11
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 10
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 10
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 10
- 238000009835 boiling Methods 0.000 description 9
- 239000000843 powder Substances 0.000 description 8
- 239000000356 contaminant Substances 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 150000001875 compounds Chemical class 0.000 description 6
- 150000002894 organic compounds Chemical class 0.000 description 6
- SQGYOTSLMSWVJD-UHFFFAOYSA-N silver(1+) nitrate Chemical compound [Ag+].[O-]N(=O)=O SQGYOTSLMSWVJD-UHFFFAOYSA-N 0.000 description 6
- 238000005245 sintering Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 4
- 229910004298 SiO 2 Inorganic materials 0.000 description 4
- 239000003463 adsorbent Substances 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 4
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 4
- 230000008025 crystallization Effects 0.000 description 4
- VLXBWPOEOIIREY-UHFFFAOYSA-N dimethyl diselenide Natural products C[Se][Se]C VLXBWPOEOIIREY-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 4
- 230000007246 mechanism Effects 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000007873 sieving Methods 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 238000010792 warming Methods 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 3
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- DNJIEGIFACGWOD-UHFFFAOYSA-N ethanethiol Chemical compound CCS DNJIEGIFACGWOD-UHFFFAOYSA-N 0.000 description 3
- UOGMEBQRZBEZQT-UHFFFAOYSA-L manganese(2+);diacetate Chemical class [Mn+2].CC([O-])=O.CC([O-])=O UOGMEBQRZBEZQT-UHFFFAOYSA-L 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 229910001961 silver nitrate Inorganic materials 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- ARXJGSRGQADJSQ-UHFFFAOYSA-N 1-methoxypropan-2-ol Chemical compound COCC(C)O ARXJGSRGQADJSQ-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- -1 DMS Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 239000011149 active material Substances 0.000 description 2
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 2
- 239000011609 ammonium molybdate Substances 0.000 description 2
- 235000018660 ammonium molybdate Nutrition 0.000 description 2
- 229940010552 ammonium molybdate Drugs 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 229940116318 copper carbonate Drugs 0.000 description 2
- GEZOTWYUIKXWOA-UHFFFAOYSA-L copper;carbonate Chemical compound [Cu+2].[O-]C([O-])=O GEZOTWYUIKXWOA-UHFFFAOYSA-L 0.000 description 2
- SXTLQDJHRPXDSB-UHFFFAOYSA-N copper;dinitrate;trihydrate Chemical compound O.O.O.[Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O SXTLQDJHRPXDSB-UHFFFAOYSA-N 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000005470 impregnation Methods 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 230000007096 poisonous effect Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 description 2
- 229910052723 transition metal Inorganic materials 0.000 description 2
- 150000003624 transition metals Chemical class 0.000 description 2
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 1
- POAOYUHQDCAZBD-UHFFFAOYSA-N 2-butoxyethanol Chemical compound CCCCOCCO POAOYUHQDCAZBD-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- FEWJPZIEWOKRBE-JCYAYHJZSA-N Dextrotartaric acid Chemical compound OC(=O)[C@H](O)[C@@H](O)C(O)=O FEWJPZIEWOKRBE-JCYAYHJZSA-N 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- WAEMQWOKJMHJLA-UHFFFAOYSA-N Manganese(2+) Chemical compound [Mn+2] WAEMQWOKJMHJLA-UHFFFAOYSA-N 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- DQMUQFUTDWISTM-UHFFFAOYSA-N O.[O-2].[Fe+2].[Fe+2].[O-2] Chemical compound O.[O-2].[Fe+2].[Fe+2].[O-2] DQMUQFUTDWISTM-UHFFFAOYSA-N 0.000 description 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- OFOBLEOULBTSOW-UHFFFAOYSA-N Propanedioic acid Natural products OC(=O)CC(O)=O OFOBLEOULBTSOW-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- FEWJPZIEWOKRBE-UHFFFAOYSA-N Tartaric acid Natural products [H+].[H+].[O-]C(=O)C(O)C(O)C([O-])=O FEWJPZIEWOKRBE-UHFFFAOYSA-N 0.000 description 1
- 241000711825 Viral hemorrhagic septicemia virus Species 0.000 description 1
- FMRLDPWIRHBCCC-UHFFFAOYSA-L Zinc carbonate Chemical compound [Zn+2].[O-]C([O-])=O FMRLDPWIRHBCCC-UHFFFAOYSA-L 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- ZOIORXHNWRGPMV-UHFFFAOYSA-N acetic acid;zinc Chemical compound [Zn].CC(O)=O.CC(O)=O ZOIORXHNWRGPMV-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004887 air purification Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 150000001845 chromium compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- AEJIMXVJZFYIHN-UHFFFAOYSA-N copper;dihydrate Chemical compound O.O.[Cu] AEJIMXVJZFYIHN-UHFFFAOYSA-N 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 229960004643 cupric oxide Drugs 0.000 description 1
- QPJDMGCKMHUXFD-UHFFFAOYSA-N cyanogen chloride Chemical compound ClC#N QPJDMGCKMHUXFD-UHFFFAOYSA-N 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 150000004985 diamines Chemical class 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000005203 dry scrubbing Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- PNDPGZBMCMUPRI-UHFFFAOYSA-N iodine Chemical compound II PNDPGZBMCMUPRI-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- VZCYOOQTPOCHFL-UPHRSURJSA-N maleic acid Chemical compound OC(=O)\C=C/C(O)=O VZCYOOQTPOCHFL-UPHRSURJSA-N 0.000 description 1
- 239000011976 maleic acid Substances 0.000 description 1
- 229940071125 manganese acetate Drugs 0.000 description 1
- 229910001437 manganese ion Inorganic materials 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- IHYNKGRWCDKNEG-UHFFFAOYSA-N n-(4-bromophenyl)-2,6-dihydroxybenzamide Chemical compound OC1=CC=CC(O)=C1C(=O)NC1=CC=C(Br)C=C1 IHYNKGRWCDKNEG-UHFFFAOYSA-N 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 150000002898 organic sulfur compounds Chemical class 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000005622 photoelectricity Effects 0.000 description 1
- 229940072033 potash Drugs 0.000 description 1
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- NHDHVHZZCFYRSB-UHFFFAOYSA-N pyriproxyfen Chemical compound C=1C=CC=NC=1OC(C)COC(C=C1)=CC=C1OC1=CC=CC=C1 NHDHVHZZCFYRSB-UHFFFAOYSA-N 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- XMVONEAAOPAGAO-UHFFFAOYSA-N sodium tungstate Chemical compound [Na+].[Na+].[O-][W]([O-])(=O)=O XMVONEAAOPAGAO-UHFFFAOYSA-N 0.000 description 1
- GGCZERPQGJTIQP-UHFFFAOYSA-N sodium;9,10-dioxoanthracene-2-sulfonic acid Chemical compound [Na+].C1=CC=C2C(=O)C3=CC(S(=O)(=O)O)=CC=C3C(=O)C2=C1 GGCZERPQGJTIQP-UHFFFAOYSA-N 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000011975 tartaric acid Substances 0.000 description 1
- 235000002906 tartaric acid Nutrition 0.000 description 1
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 1
- 229910000314 transition metal oxide Inorganic materials 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000004246 zinc acetate Substances 0.000 description 1
- 239000011667 zinc carbonate Substances 0.000 description 1
- 235000004416 zinc carbonate Nutrition 0.000 description 1
- 229910000010 zinc carbonate Inorganic materials 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Catalysts (AREA)
Abstract
The invention relates to a catalyst-containing purifying apparatus used for processing organic waste gas. The apparatus comprises a catalyst-containing adsorption and oxidation unit. An operation temperature is 25-200 DEG C, and a space velocity is 10000-180000h<-1>. The catalyst-containing adsorption and oxidation unit comprises a catalyst which is a metal or a metal oxide, and a porous carrier which is alumina or zeolite, wherein the carrier is used for carrying the catalyst. The catalyst-containing purifying apparatus is used for purifying organic waste gas in a low-concentration occasion with an organic waste gas inflow concentration of 0.001-200ppmv. The purification of the organic waste gas can be further carried out with the cooperation of ozone, such that the organic waste gas purification performance can be improved.
Description
Technical field
The present invention relates to a kind of catalytic conversion unit that is used for cleaning organic waste gas, it removes by catalyst under 25～200 ℃ of normal temperature and contains foul smelling, poisonous and corrosive chemical gas.
Background technology
It is main removing at present stench, poisonous and corrosive gas and mainly be with dry washing absorber (dry scrubbing adsorber), absorption tower and chemisorbed filter material; And major part all has the chemical agent of interpolation to strengthen its removal efficient, to reduce tail gas concentration and to increase treating capacity; And physical absorption, chemisorbed and chemical absorbing are significant feature mechanism in the purifying exhaust air unit, and wherein physical absorption is reversible reaction, mainly carries out pollutant removal with original functional group of dielectric surface or hole character; Chemisorbed and chemisorption then add active material in medium, make the active material in pollutant and the medium carry out adsorption reaction or chemisorption, thus improve pollutant remove the rate and the amount of removing.
Air molecule pollution thing (airborne molecular contamination; AMC) comprise compounds such as hydrogen sulfide, sulfur dioxide, dimethyl disulfide, ammonia, formaldehyde, ethene and isopropyl alcohol; Be present in the context mostly; Mainly due to traffic pollution, building site pollution, agricultural pollution, animals and plants oxidation Decomposition, domestic pollutant such as kitchen, factors such as sanitary equipment, the discharging of inside and outside factory of factory, air gas displacement cause.
And recently; International pay attention to day by day for environmental protection subject under discussion and industry security health and the toilet's molecular contaminants purification of high-tech factory; To such an extent as to consider the harm of industrial waste gas to environment and the general popular health generation of labourer; Strict day by day for the industrial gas emission standard, rules have all been made the relevant concentration and the discharge standard of stink both at home and abroad; On the other hand, the high-order processing procedure of high-tech factory is for unmanageable molecular contaminants (like DMS, DMDS, Acetone, MEK, PGME) such as sulfur-containing compound and low boiling organic compounds recently, and the degree of purification before the toilet of gas introducing outside requires more for harsh.
For example in semiconductor crystal wafer manufactory and TFT-LCD panel photoelectricity manufacturing industry panel technology; Removing photoresistance program (stripping process) employed removing photoresistance stripper (stripper) main component is higher boiling and almost completely water-soluble organic compound, comprises MEA (MEA), dimethyl sulfoxide (DMSO) (DMSO) and ethylene glycol monobutyl ether (BDG) etc.; And in removing photoresistance technology; Though the dimethyl sulfoxide (DMSO) in the removing photoresistance agent is the liquid that a kind of higher boiling is water-soluble and volatility is low; But in processing procedure; The dimethyl disulfide of as easy as rolling off a log formation low boiling and stench (dimethyl sulfide, DMS) and DMDS (dimethyl disulfide, gaseous contaminant DMDS); Yet; Also can't remove the dimethyl disulfide and the DMDS of low boiling and low aqueous solubility fully through traditional absorption method, condensation method and absorption process; And it promptly can produce stench under low concentration; Very easily influence living environment around the factory building and cause common people's protest, also have influence on the product yield of other high-tech factory high-order processing procedure around the factory building simultaneously.
And the character of pollutant DMS is not too identical with general sulfur-bearing gaseous state molecular contaminants, and sulfur-bearing gaseous state molecular contaminants common in the air is hydrogen sulfide and sulfur dioxide, and the mode that removes is main with strong oxidizer such as potassium permanganate etc. then generally, and its reaction mechanism is following:
Sulfur dioxide is removed reaction mechanism
3SO
2+2KMnO
4+4KOH→3K
2SO
4+2MnO
2+2H
2O
MnO
2+SO
2+2KOH→K
2SO
4+MnO+H
2O
2MnO+O
2→2MnO
2
The hydrogen sulfide removal reaction mechanism
3H
2S+2KMnO
4→3S+2MnO
2+2KOH+2H
2O
Yet, not obvious and molecule is less because of its soda acid character though this DMS also belongs to organic sulfur compound with similar performance such as methyl mercaptan, character and hydrogen sulfide near but more difficult oxidized, so quite be difficult for processing.
Wanting under the general situation under 25～200 ℃ of normal temperature, DMS to be decomposed, almost is impossibility, only can the compound that is prone to absorption be removed or changed in its absorption.
Remove sulfide with adsorption method and generally use adsorbent, the activity composition of adsorbent is mainly transition metal, and method has direct use transition metal oxide, or transition metal is dispersed in the porous carrier surface, or both use with each other; The adsorbent patent of relevant removal sulfide can be divided into two types substantially, and one type for being carrier with the activated carbon, metallic salt is contained to be dipped in can remove sulfur dioxide and hydrogen sulfide on the activated carbon, and the normal metallic salt that uses has chromic salts, mantoquita, silver salt etc.; And the activated carbon adsorbent of upgrading has suitable adsorbance for the contaminant gases of high concentration, but its adsorbance can reduce with pollutant levels, and when linear velocity increases, removes efficient and adsorbance all can significantly reduce.
On activated carbon bed, spray directly absorbing sulfur dioxide of solution mode (iodine, KI, vulcanized sodium, sodium bisulfide, water), hydrogen sulfide like United States Patent (USP) 4075282.4196183 of United States Patent (USP)s are at activated carbon surface impregnation cupric oxide or di-iron trioxide, and (20～250ppmv) hydrogen sulfide has 98% the rate that removes for middle concentration.5063196 of United States Patent (USP)s are at activated carbon surface impregnation copper carbonate, Kocide SD, zinc carbonate, silver nitrate, triethyl group diamines (TEDA) and organic acid (maleic and tartaric acid); This chemosorbent can effectively be removed hydrogen cyanide, cyanogen chloride (chlorine, hydrogen chloride, sulfur dioxide), formaldehyde and hydrogen sulfide; And it forms maximum characteristics is not contain chromium compound, and adds alkali compounds to absorb sour gas.United States Patent (USP) 5113856 absorption chlorine, the upgrading activated carbon of sulfur dioxide then contain and soak ammoniacal liquor, copper carbonate and sodium tungstate.And the activated carbon in the United States Patent (USP) 5496785 is to serve as main active the composition with zinc acetate, potash, can effectively remove hydrogen cyanide, carbon tetrachloride, sulfur dioxide, chlorine, hydrogen fluoride and hydrogen sulfide.
In addition, in Japan Patent 1996-323194, disclose a kind of manganese ion is exchanged and on X type zeolite, can be used for removing sulphur compounds such as hydrogen sulfide and methyl mercaptan, at lower space flow speed (hr
-1) descend its initial rate that removes can reach 99.9%.
Space velocity defines according to Smith (1981):
Space velocity (hr
-1Gas flow (the m of)=through catalyst bed
3/ hr)/catalyst bed volume (m
3)
If unit of account then is called gas hourly space velocity (gas hourly space velocity, GHSV again hour to be benchmark; Volume hourly space velocity, VHSV).Space velocity is the inverse of waste gas mean residence time (average residence time) on catalyst bed, is the calculating reference value of catalyst amount.
For general for removal just like unmanageable molecular contaminants such as low threshold value organic molecule, sulfur-containing compound or low boiling organic compound such as DMS; At present still there is not the preferable mode that effectively removes, so the object of the invention promptly provides effective and has higher catalyst filter material and the device thereof that removes rate to this low threshold value organic molecule pollutant.
Summary of the invention
In order to improve the problem that above-mentioned known technology faces; The object of the present invention is to provide a kind of can be under 25～200 ℃ of normal temperature; Effectively remove in the organic exhaust gas catalytic conversion unit of unmanageable organic molecule pollutants such as low threshold value or low boiling organic compound, to lower organic molecule pollutant in factory's discharging organic exhaust gas to influence that environment was caused.
For reaching above-mentioned purpose, the present invention provides a kind of catalytic conversion unit that is used for cleaning organic waste gas, and it comprises catalyst adsorption and oxidation unit, and the operating temperature of this catalyst adsorption and oxidation unit is 25～200 ℃, and space flow speed is 10000～180000h
-1, and this catalyst adsorption and oxidation unit comprises:
Catalyst, it is metal or metal oxide, and this metal is selected from molybdenum, manganese, iron, copper, zinc, lead, cobalt, silver or its combination; And
Porous carrier, it is aluminium oxide or zeolite, is used to carry above-mentioned catalyst;
Wherein, this organic exhaust gas concentration that becomes a mandarin is the low concentration occasion of 0.001～200ppmv.
Aforesaid catalytic conversion unit, wherein this catalyst is selected from CuO, MoO
3, CuO-MoO
3, Ag, Cu, Mn, Ag-Mn or its combination; And this porous carrier is selected from γ-Al
2O
3, ZSM-5 or its combination.
Aforesaid catalytic conversion unit, wherein catalyst in this catalyst adsorption and oxidation unit and porous carrier composition is selected from CuO/ γ-Al
2O
3, CuO-MoO
3/ γ-Al
2O
3, Ag/ZSM-5, Cu/ZSM-5, Mn/ZSM-5, Ag-Mn/ZSM-5 or its combination.
Aforesaid catalytic conversion unit further comprises the ozone supply unit, and it is positioned at before this catalyst adsorption and oxidation unit.
And above-mentioned catalytic conversion unit further comprises concentration runner, and it is positioned at before this catalyst adsorption and oxidation unit, and absorption through this concentration runner and desorption are gone ahead of the rest and concentrated the concentration of organic exhaust gas; Simultaneously, also can further comprise the ozone supply unit, this ozone supply unit is between this concentration runner and this catalyst absorbing unit.
Aforesaid catalytic conversion unit, wherein the pattern of this catalyst absorbing unit can be immobilization bed formula, rotary-type or revolving ring type; And when this catalyst absorbing unit was immobilization bed formula, this immobilization bed can be single tower, double-tower type or multi-tower type; In addition, when this catalyst absorbing unit was rotary-type or revolving ring type, this rotary-type or revolving ring type catalyst bed can comprise adsorption zone and desorption zoneofoxidation; Again, this rotary-type or revolving ring type catalyst bed further comprises the cooling zone, and it is between this desorption zoneofoxidation and this adsorption zone.
Aforesaid catalytic conversion unit, the shape of this catalyst absorbing unit can be graininess, honeycomb, cylindric, foaming shape, Powdered or spherical.
Aforesaid catalytic conversion unit, wherein the operating temperature of this catalyst adsorption and oxidation unit is preferably 100～130 ℃.
Aforesaid catalytic conversion unit, it further comprises incinerator, and this incinerator is positioned at before this catalyst adsorption and oxidation unit, and the high-temperature oxydation effect through this incinerator purifies high-concentration organic waste gas in advance.
Above-mentioned catalytic conversion unit, wherein the exhaust temperature of this incinerator is controlled in 25～200 ℃; And this incinerator is direct-fired incinerator, double tower type or multitower type heat accumulating type incinerator; Simultaneously, the exhaust temperature of this incinerator is controlled at 100～130 ℃.
Aforesaid catalytic conversion unit, wherein this organic exhaust gas concentration that becomes a mandarin is the low concentration occasion of 0.001～20ppmv.
Aforesaid catalytic conversion unit, wherein the operation ozone of this catalyst adsorption and oxidation unit and become a mandarin the organic concentration molar ratio between 0.5～2.0.
The above-mentioned catalytic conversion unit that is used for cleaning organic waste gas; It is through providing catalyst adsorption and oxidation unit; To the concentration that becomes a mandarin is the low concentration organic exhaust gas occasion of organic exhaust gas or the 0.001～20ppmv of 0.001～200ppmv; Between 25～200 ℃ of normal temperature; Can be effectively and the low-concentration organic in the organic exhaust gas such as DMS carry out the adsorption and oxidation effect; Low threshold value such as DMS, acetic acid and DMF or low boiling low concentration organic molecule pollutants such as DMS, Acetone and IPA be can effectively remove,, the manufacturing of high-tech wafer, photoelectric panel manufacturing industry, application press and the relevant chemical industry of high air quantity low concentration discharging are worth being applied to for quite meeting the excellent technique of environmental protection and energy demand; Also can be applicable to simultaneously the effect of the air molecule micropollutants AMC purification of the manufacturing of high-tech wafer, photoelectric panel manufacturing industry toilet pure air purification of sulphur-containing compound and hydrocarbon.
The following example only for explanation, should not limit category of the present invention, reasonably changes, and such as for haveing the knack of this art obviously for reasonable, can carry out in not breaking away under the category of the present invention.
Description of drawings
Fig. 1 is an a kind of sketch map that is used for the catalytic conversion unit of cleaning organic waste gas among the present invention.
Fig. 2 is a sketch map of the catalytic conversion unit of the single tower catalyst-packed column of use immobilization bed formula among the present invention.
Fig. 3 is for using a sketch map of rotary-type catalytic conversion unit among the present invention.
Fig. 4 is an a kind of sketch map that is used for the catalytic conversion unit of cleaning organic waste gas among the present invention.
Fig. 5 is an a kind of sketch map that is used for the catalytic conversion unit of cleaning organic waste gas among the present invention.
Fig. 6 is an a kind of sketch map that is used for the catalytic conversion unit of cleaning organic waste gas among the present invention.
Fig. 7 is an a kind of sketch map that is used for the catalytic conversion unit of cleaning organic waste gas among the present invention.
Fig. 8 is for using a sketch map of rotary-type catalytic conversion unit among the present invention.
Fig. 9 is an a kind of sketch map that is used for the catalytic conversion unit of cleaning organic waste gas among the present invention.
[primary clustering symbol description]
5 blower fans
10 catalyst adsorption and oxidation unit
15 ozone supply unit
20 catalyst-packed columns
21 catalyst filter materials
30 concentration runners
35 heaters
40 incinerators
The A gas access
The B gas vent
The C gas vent
The D gas access
The I adsorption zone
II desorption zoneofoxidation
The III cooling zone
The specific embodiment
For fully understanding the object of the invention, characteristic and effect, existing by following concrete embodiment, and cooperate appended graphicly, the present invention is done a detailed description, explain as after:
Please with reference to Fig. 1; It is an a kind of sketch map that is used for the catalytic conversion unit of cleaning organic waste gas among the present invention; It comprises blower fan 5 and catalyst adsorption and oxidation unit 10; This mode of operation that is used for the catalytic conversion unit of cleaning organic waste gas is: A gets into this catalyst adsorption and oxidation unit 10 via pumping of this blower fan 5 to organic exhaust gas from the gas access, and 25～200 ℃ of normal temperature, and space flow speed is 10000～180000h through the catalyst in this catalyst adsorption and oxidation unit 10
-1Situation
Down and the organic substance effect in the organic exhaust gas, thus discharge from gas vent B after purifying this organic exhaust gas.
This catalyst adsorption and oxidation unit comprises simultaneously: catalyst, and it is metal or metal oxide, and this metal is selected from molybdenum, manganese, iron, copper, zinc, lead, cobalt, silver or its combination; And porous carrier, it is aluminium oxide or zeolite, is used to carry above-mentioned catalyst.
And this catalyst can be selected from CuO, MoO
3, CuO-MoO
3, Ag, Cu, Mn, Ag-Mn or its combination; And this porous carrier can be selected from γ-Al
2O
3, ZSM-5 or its combination.
The catalyst in this catalyst adsorption and oxidation unit and the composition of porous carrier are preferable is selected from CuO/ γ-Al
2O
3, CuO-MoO
3/ γ-Al
2O
3, Ag/ZSM-5, Cu/ZSM-5, Mn/ZSM-5, Ag-Mn/ZSM-5 or its combination.
And the collocation method of above-mentioned catalyst and porous carrier is following:
CuO/r-Al
2O
3
Get commercial r-Al
2O
3Activated alumina 20 gram (diameter 2mm) is got Gerhardite (II) 6.04 grams and is added water 50 grams it is dissolved fully, and copper nitrate (II) solution is slowly added in the activated alumina, stirs and uses the rotation appearance that volatilizees to drain solution after 1 hour; Sintering 8 hours are spent with 500 in the dry back of 110 degree, can get CuO/γ-Al
2O
3Sample.
CuO-MoO
3/γ-Al
2O
3
Get commercial γ-Al
2O
3Activated alumina 20 grams (diameter 2mm); Get that Gerhardite (II)/ammonium molybdate 6.04 grams and 2.46 grams add water 50 respectively and 250 grams (60 ℃) dissolve it fully; After 2 solution are fully mixed copper nitrate (II)/ammonium molybdate solution slowly added and contain in the activated alumina, stirs and use the rotation appearance that volatilizees to drain solution after 1 hour; Sintering 8 hours are spent with 500 in the dry back of 110 degree, can get CuO-MoO
3/ γ-Al
2O
3Sample.
Ag/ZSM-5
Get commercial NH
4-ZSM5 (CBV-5524G, SiO
2/ Al
2O
3=50) zeolite 20 gram adds and fully stirs behind the 120ml water and be warming up to 50 ℃, gets silver nitrate crystallization 1.53 grams and adds water 15 grams it is dissolved fully, liquor argenti nitratis ophthalmicus is slowly splashed in the solution that contains zeolite, stirs and filters after 1 hour and wash.The dry back of 80 degree can get the Ag/ZSM-5 powder with 420 degree sintering 3 hours, again with powder sample economy-combat ingot, pulverize, particle that the program of sieving is got 16～30mesh.
Cu/ZSM-5
Get commercial NH
4-ZSM5 (CBV-5524G, SiO
2/ Al
2O
3=50) zeolite 20 gram adds and fully stirs behind the 120ml water and be warming up to 50 ℃, gets copper nitrate 0.92 gram and adds water 15 grams it is dissolved fully, copper nitrate solution is slowly splashed in the solution that contains zeolite, stirs and filters after 2 hours and wash.80 degree with 530 degree sintering 5 hours, can get the Cu/ZSM-5 powder after dry 3 hours, again with powder sample economy-combat ingot, pulverize, particle that the program of sieving is got 16～30mesh.
Mn/ZSM-5
Get commercial NH
4-ZSM5 (CBV-5524G, SiO
2/ Al
2O
3=50) fully stir and be warming up to 50 ℃ after zeolite 20 grams add 120ml water; Getting 2.3 gram manganese acetates (containing 4 crystallizations water) adds water 20 grams it is dissolved fully; Manganese acetate solution is slowly splashed in the solution that contains zeolite, and solution slowly becomes steel gray, stirs and filters after 1 hour and washing.Sintering 3 hours are spent with 420 in the dry back of 80 degree, can get the Mn/ZSM-5 powder.With powder sample economy-combat ingot, pulverize, particle that the program of sieving is got 16～30mesh.
Ag-Mn/ZSM-5
Get commercial NH
4-ZSM-5 (CBV-5524G, SiO
2/ Al
2O
3=50) zeolite 20 gram adds and fully stirs behind the 120ml water and be warming up to 50 ℃, gets silver nitrate crystallization 1.53 grams and adds water 15 grams it is dissolved fully, liquor argenti nitratis ophthalmicus is slowly splashed in the solution that contains zeolite, stirs and filters after 1 hour and wash.Filter cake is dispersed in the solution 20ml that also will contain 2.3 gram manganese acetates (containing 4 crystallizations water) in the 100ml water splashes into, solution slowly becomes steel gray, stirs filtration and washing after 1 hour, and sintering 3 hours are spent with 420 in 80 degree drying backs, can get the Ag-Mn/ZSM-5 powder.With powder sample economy-combat ingot, pulverize, particle that the program of sieving is got 16～30mesh.
Come again; Please with reference to Fig. 2; It is a sketch map of the catalytic conversion unit of the single tower catalyst-packed column of use immobilization bed formula; It comprises blower fan 5 and reaches-catalyst adsorption and oxidation unit 10; And this catalyst adsorption and oxidation unit 10 is the catalyst-packed column 20 of immobilization bed formula, and this catalyst-packed column 20 contains catalyst filter material 21, and this catalyst filter material 21 is catalyst and porous carrier is formed; The mode of operation of this catalytic conversion unit is: A pumps this catalyst-packed column 20 of entering to organic exhaust gas from the gas access via blower fan 5, is 10000～180000h through the catalyst filter materials 21 in this catalyst-packed column 20 at 25～200 ℃ of normal temperature and space flow speed
-1Under the situation with organic exhaust gas in the organic substance effect, thereby discharge from gas vent B after purifying this organic exhaust gas.
Please with reference to Fig. 3; It is for using the sketch map of rotary-type catalytic conversion unit; It comprises blower fan 5 and catalyst adsorption and oxidation unit 10, and this catalyst adsorption and oxidation unit 10 is concentration runner 30, and this concentration runner 30 contains adsorption zone I and desorption zoneofoxidation II; Also can further comprise cooling zone III; And this dense runner of taking turns promptly is made up of the catalyst filter material, and this catalyst filter material is catalyst and porous carrier is formed, and the mode of operation of this catalytic conversion unit is: A pumps the adsorption zone I that gets into this concentration runner 30 to organic exhaust gas via blower fan 5 from the gas access; Organic substance in the organic exhaust gas of this adsorption zone I is adsorbed by the catalyst filter material among this concentration runner 30 adsorption zone I, and the organic exhaust gas after being cleaned is discharged from gas vent B; And when the catalyst filter material of organic substance in the absorption organic exhaust gas turns to this desorption zoneofoxidation II; Air via 70～200 ℃ of heater 35 heating back normal temperature gets in this desorption zoneofoxidation II, and this moment, the catalyst filter material of adsorb organic compound matter was 10000～180000h in 70～200 ℃ and space flow speed
-1Following and the organic substance on it carries out the desorption oxidation; Making organic substance concentrated the back discharges from another gas vent C; And this concentration runner 30 further can comprise cooling zone III; It to cool off the catalyst filter material on it, makes the catalyst filter material on this concentration runner 30 get into the use of adsorption zone I continued in the cooling back between this desorption zoneofoxidation II and this adsorption zone I.
Moreover; Please with reference to Fig. 4; It is an a kind of sketch map that is used for another specific embodiment of catalytic conversion unit of cleaning organic waste gas of the present invention; It comprises blower fan 5, ozone supply unit 15 and catalyst adsorption and oxidation unit 10, promptly between this blower fan 5 and this catalyst adsorption and oxidation unit 10, this ozone supply unit 15 is provided, and this ozone supply unit 15 provides ozone (ozone of supply and become a mandarin the organic concentration molar ratio between 0.5～2.0); With the catalyst of strengthening this catalyst absorbing unit 10 adsorption and oxidation ability for organic substance in the organic exhaust gas, more effective cleaning organic waste gas; And the purification of this organic gas is as shown in Figure 1, and only before organic exhaust gas got into this catalyst absorbing unit 10, ozone supply no longer was repeated in this description at this with strengthened purification usefulness simultaneously.
Moreover; Please with reference to Fig. 5; It is an a kind of sketch map that is used for another specific embodiment of catalytic conversion unit of cleaning organic waste gas of the present invention; It comprises blower fan 5, ozone supply unit 15 and catalyst adsorption and oxidation unit 10; And this catalyst adsorption and oxidation unit 10 is a catalyst-packed column 20 of immobilization bed formula, and between this blower fan 5 and this catalyst-packed column 20, this ozone supply unit 15 is provided, and this ozone supply unit 15 provides ozone (ozone of supply and become a mandarin the organic concentration molar ratio between 0.5～2.0); To strengthen in this catalyst-packed column 20 catalyst filter material 21 for the adsorption and oxidation ability of organic substance in the organic exhaust gas, more effective cleaning organic waste gas; And the purification of this organic gas only before organic exhaust gas gets into this catalyst absorbing unit 10, utilizes this ozone supply unit 15 while ozone supply with strengthened purification usefulness as shown in Figure 2, no longer is repeated in this description at this.
Moreover; See also Fig. 6, its catalytic conversion unit that is used for cleaning organic waste gas for the present invention is a kind of is the sketch map of a specific embodiment again, and it comprises blower fan 5, concentration runner 30 and catalyst adsorption and oxidation unit 10; And this catalyst adsorption and oxidation unit 10 is the catalyst-packed column 20 of immobilization bed formula; In the present embodiment, organic exhaust gas is advanced into the purification that this concentration runner 30 carries out organic exhaust gas earlier and concentrates, then; Organic exhaust gas after purifying is discharged from gas vent B earlier; D gets into this catalyst-packed column 20 again and carries out follow-up catalyst adsorption and oxidation effect and the organic substance that concentrates back (operation that it is operated with Fig. 3 no longer is repeated in this description) through this concentration runner 30 is through the gas access, so that the more efficiently adsorption and oxidation of the organic substance in the organic exhaust gas.
Please with reference to Fig. 7; It is a kind of sketch map that is used for the another specific embodiment of catalytic conversion unit of cleaning organic waste gas of the present invention, and it comprises blower fan 5, concentration runner 30, ozone supply unit 15 and catalyst adsorption and oxidation unit 10, and this catalyst adsorption and oxidation unit 10 is the catalyst-packed column 20 of immobilization bed formula; In the present embodiment; Organic exhaust gas is advanced into the purification that this concentration runner 30 carries out organic exhaust gas earlier and concentrates, and then, the organic exhaust gas after purifying is first discharges from a gas vent B; And (its operation is with the operation of Fig. 3 after this concentration runner 30 concentrates; No longer be repeated in this description) organic substance get into this catalyst-packed column 20 again and carry out follow-up catalyst adsorption and oxidation effect through a gas access D, only in present embodiment, ozone supply unit (ozone of supply and become a mandarin the organic concentration molar ratio between 0.5～2.0) is provided simultaneously; Provide ozone to get in this catalyst-packed column 20, so that the organic substance in this organic exhaust gas is more effective adsorption and oxidation.
See also Fig. 8; It is for using a sketch map of rotary-type catalytic conversion unit, and it comprises blower fan 5, ozone supply unit 15 and catalyst adsorption and oxidation unit 10, and this catalyst adsorption and oxidation unit 10 is a concentration runner 30; This concentration runner 30 contains adsorption zone I and desorption zoneofoxidation II; Also can further comprise cooling zone III, and this dense runner of taking turns is made up of the catalyst filter material promptly, this catalyst filter material is catalyst and porous carrier is formed; The mode of operation of this catalytic conversion unit is close with the operation of Fig. 3; It is: A pumps the adsorption zone I that gets into this concentration runner 30 via blower fan 5 to organic exhaust gas from the gas access, and the organic substance in this adsorption zone I in the organic exhaust gas is adsorbed by the catalyst filter material among this concentration runner 30 adsorption zone I, and the organic exhaust gas after being cleaned is discharged from gas vent B; And when the catalyst filter material of organic substance in the absorption organic exhaust gas turns to this desorption zoneofoxidation II; Air via 70～200 ℃ of heater 35 heating back normal temperature; In conjunction with the ozone that is provided from this ozone supply unit 15, get in this desorption zoneofoxidation II, the catalyst filter material of adsorb organic compound matter is between 70～200 ℃ at this moment; Combined with ozone and the organic substance on it carry out the desorption oxidation; Make organic substance concentrated the back and discharge from another gas vent C, and this concentration runner 30 further can comprise cooling zone III, it is between this desorption zoneofoxidation II and this adsorption zone I; To cool off the catalyst filter material on it; Make catalyst filter material on this concentration runner 30 after cooling, get into adsorption zone I continued and use, and the ozone that provided of this ozone supply unit can make the desorption oxidation of catalyst filter material and organic substance more complete certainly, can more effective cleaning organic waste gas.
Please with reference to Fig. 9, it is a kind of sketch map that is used for another specific embodiment of catalytic conversion unit of cleaning organic waste gas of the present invention, and it comprises blower fan 5, incinerator 40 and catalyst adsorption and oxidation unit 10; In the present embodiment, organic exhaust gas gets in the incinerator 40, with this organic exhaust gas of high-temp combustion via pumping of this blower fan from gas access A; To reduce the concentration of organic substance in this organic exhaust gas, the organic exhaust gas after these incinerator 40 burnings, organic substance concentration reduction in it; And the exhaust temperature of control incinerator is between 75～200 ℃; Better is to be controlled between 100～130 ℃, sends into this catalyst adsorption and oxidation unit 10 again, more to accomplish the purification of this low-concentration organic exhaust gas; And the organic exhaust gas after purifying is discharged via gas vent B again, to accomplish the purification of organic exhaust gas; And this incinerator can be direct combustion incinerator, double tower type or multitower type heat accumulating type incinerator, and the incinerator in Fig. 9 is the double tower type heat accumulating type incinerator.
The embodiment data:
Table 1, catalyst adsorption and oxidation purification unit are handled purification efficiency (the space flow speed 35000h of DMS
-1)
The data of table 1 are to use the device of Fig. 1 and Fig. 4 operated, and in the data of table 1, the catalyst/porous carrier that uses is Ag/ZSM-5 and Ag-Mn/ZSM-5; Catalyst operating temperature circle is in 100～250 ℃; And when with 200～250 ℃ of operations of higher temperatures, ozone is added purify, and when using 100～150 ℃ of operations; Add ozone and purify, its result shows that purification efficiency can reach more than 75%; But also can find by The above results, can reduce operating temperature behind the adding ozone, and also can promote purification efficiency.
Table 2, catalyst adsorption and oxidation purification unit are handled (the space flow speed 180000h that runs through the time of 20PPM DMS
-1)
The data of table 2 also use the device of Fig. 1 and Fig. 4 operated, and in the data of table 2, the porous carrier that uses is ZSM-5; The catalyst operating temperature is 25 ℃, has ozone free to add the test that purifies reaction, when adding ozone purifies; It is longer that its result shows that this porous carrier is run through the time; Not adding ozone, can to postpone to run through the time over half, and the visible ozone that adds purifies and can effectively promote purification efficiency, and then prolongs the life-span of this porous carrier.
Table 3, catalyst adsorption and oxidation purification unit are handled purification efficiency (the space flow speed 90000h of 20PPM DMS
-1) data of table 3 are to use the device of Fig. 4 operated, in the data of table 3, the catalyst/porous carrier that uses is Ag/ZSM-5, Mn/ZSM-5, Ag-Mn/ZSM-5, CuO/Al
2O
3And CuO-MoO/Al
2O
3, the catalyst operating temperature is 130 ℃, and all adds ozone and purify reaction, its result all is higher than more than 80% for purification efficiency, shows effectively cleaning organic waste gas of catalytic conversion unit of the present invention.
Table 4, catalyst adsorption and oxidation purification unit are handled purification efficiency (the space flow speed 90000h of 20PPM DMS
-1)
The data of table 4 are to use the device of Fig. 4 operated; In the data of table 4, the catalyst/porous carrier that uses is Ag-Mn/ZSM-5, and the catalyst operating temperature is 130 ℃; And adding different mol ratio example ozone concentration; Its result shows that the ozone concentration of higher mole ratio example has higher purification efficiency, no matter only be that molar ratio is that 1/1 or 2/1 purification efficiency all is higher than more than 98%, shows effectively cleaning organic waste gas of catalytic conversion unit of the present invention once more.
Table 5, catalyst adsorption and oxidation purification unit are handled the purification efficiency (ozone concentration (O of 20PPM DMS
3/ VOC molar ratio=2/1))
The data of table 5 are to use the device of Fig. 4 operated, and in the data of table 5, the catalyst/porous carrier that uses is Ag-Mn/ZSM-5; The catalyst operating temperature is 130 ℃; And add the ozone concentration of identical molar ratio 2/1, and only different on space flow speed, be respectively 45000hr
-1, 90000hr
-1And 180000hr
-1, three's purification efficiency is all more than 95%, only changes into SO
2Conversion ratio then improve and weaken with space flow speed, show that lower space flow speed has higher SO
2Conversion ratio.
Table 6, catalyst adsorption and oxidation purification unit are handled the purification efficiency (dense (O of ozone of 20PPM DMS
3/ VOC molar ratio=2/1)
The data of table 6 are to use the device of Fig. 4 operated, and in the data of table 6, the catalyst/porous carrier that uses is Ag/ZSM-5; The catalyst operating temperature is respectively 25 ℃ and 130 ℃; And add the ozone concentration of identical molar ratio 2/1, and space flow speed also is identical, and the different catalyst operating temperature; All can keep and run through the time for a long time more than 300 minutes, only in SO
2Conversion ratio difference to some extent, under 25 ℃, have only 0.2 conversion ratio, at the next conversion ratio that reaches more than 25% of higher temperature.
Table 7, catalyst adsorption and oxidation purification unit are handled purification efficiency (the space flow speed 25000h of Acetone
-1)
The data of table 7 are to use the device of Fig. 4 operated; In the data of table 7, the catalyst/porous carrier that uses is Cu/ZSM-5 and Cu-Ce/ZSM-5, and the catalyst operating temperature is respectively 200～250 ℃ and 100～130 ℃; The ozone concentration that only under 100～130 ℃ condition, adds molar ratio 1/1; And space flow speed is also identical, and the organic substance in the organic exhaust gas is Acetone, and its result is for adding under the ozone condition; Even if catalyst is operated, also can reach higher purification efficiency under the condition of lower temperature.
Show via above-mentioned experimental data; The catalytic conversion unit that is used for cleaning organic waste gas of the present invention; Via catalyst adsorption and oxidation unit is provided; To the concentration that becomes a mandarin is the low concentration organic exhaust gas occasion of organic exhaust gas or the 0.001～20ppmv of 0.001～200ppmv; Between 25～200 ℃ of normal temperature, can be effectively and the low-concentration organic in the organic exhaust gas such as DMS carry out the adsorption and oxidation effect, under the condition that adds ozone, more can improve purification efficiency simultaneously; And under suitable catalyst space flow velocity, effectively remove low threshold value such as DMS, acetic acid and DMF or low boiling low concentration organic molecule pollutants such as DMS, Acetone and IPA, be a kind of excellent technique that quite meets environmental protection and reduce energy demand.
Claims (20)
1. catalytic conversion unit that is used for cleaning organic waste gas, it comprises catalyst adsorption and oxidation unit, and the operating temperature of this catalyst adsorption and oxidation unit is 25～200 ℃, and space flow speed is 10000～180000h
-1, and this catalyst adsorption and oxidation unit, it is characterized in that, comprise:
Catalyst, it is metal or metal oxide, and this metal is selected from molybdenum, manganese, iron, copper, zinc, lead, cobalt, silver or its combination; And
Porous carrier, it is aluminium oxide or zeolite, is used to carry above-mentioned catalyst;
Wherein, to be used for the cleaning organic waste gas concentration that becomes a mandarin be the low concentration occasion of 0.001～200ppmv to this catalytic conversion unit.
2. catalytic conversion unit as claimed in claim 1 is characterized in that this catalyst is selected from CuO, MoO
3, CuO-MoO
3, Ag, Cu, Mn, Ag-Mn or its combination.
3. catalytic conversion unit as claimed in claim 1 is characterized in that this porous carrier is selected from γ-Al
2O
3, ZSM-5 or its combination.
4. catalytic conversion unit as claimed in claim 1 is characterized in that, catalyst in this catalyst adsorption and oxidation unit and porous carrier composition are selected from CuO/ γ-Al
2O
3, CuO-MoO
3/ γ-Al
2O
3, Ag/ZSM-5, Cu/ZSM-5, Mn/ZSM-5, Ag-Mn/ZSM-5 or its combination.
5. catalytic conversion unit as claimed in claim 1 is characterized in that, further comprises the ozone supply unit, and said ozone supply unit is positioned at before this catalyst adsorption and oxidation unit.
6. catalytic conversion unit as claimed in claim 1; It is characterized in that; Further comprise concentration runner, said concentration runner is positioned at before this catalyst adsorption and oxidation unit, and absorption through this concentration runner and desorption are gone ahead of the rest and concentrated the concentration of organic exhaust gas.
7. catalytic conversion unit as claimed in claim 6 is characterized in that, further comprises the ozone supply unit, and this ozone supply unit is between this concentration runner and this catalyst absorbing unit.
8. like each described catalytic conversion unit in the claim 1,5,6,7, it is characterized in that the pattern of this catalyst absorbing unit can be immobilization bed formula, rotary-type or revolving ring type.
9. catalytic conversion unit as claimed in claim 8 is characterized in that, when this catalyst absorbing unit was immobilization bed formula, this immobilization bed was single tower, double-tower type or multi-tower type.
10. catalytic conversion unit as claimed in claim 8 is characterized in that, when this catalyst absorbing unit was rotary-type or revolving ring type, this rotary-type or revolving ring type catalyst bed comprised adsorption zone and desorption zoneofoxidation.
11. catalytic conversion unit as claimed in claim 10 is characterized in that, this rotary-type or revolving ring type catalyst bed further comprises the cooling zone, and it is between this desorption zoneofoxidation and this adsorption zone.
12. like each described catalytic conversion unit in the claim 1,5,6,7, it is characterized in that, this catalyst absorbing unit be shaped as graininess, honeycomb, cylindric, foaming shape, Powdered or spherical.
13., it is characterized in that the operating temperature of this catalyst adsorption and oxidation unit is 100～130 ℃ like each described catalytic conversion unit in the claim 5,7.
14. like each described catalytic conversion unit in the claim 1,5,6,7; It is characterized in that; Further comprise incinerator, this incinerator is positioned at before this catalyst adsorption and oxidation unit, and the high-temperature oxydation effect through this incinerator purifies high-concentration organic waste gas in advance.
15. the catalytic conversion unit described in claim 14 is characterized in that, the exhaust temperature of this incinerator is controlled between 75～200 ℃.
16. the catalytic conversion unit described in claim 15 is characterized in that, this incinerator is direct-fired incinerator, double tower type or multitower type heat accumulating type incinerator.
17. the catalytic conversion unit described in claim 16 is characterized in that, the exhaust temperature of this incinerator is controlled between 100～130 ℃.
18., it is characterized in that it is the low concentration occasion of 0.001～20ppmv that this catalytic conversion unit is used for the cleaning organic waste gas concentration that becomes a mandarin like each described catalytic conversion unit in the claim 1,5,6,7.
19. the catalytic conversion unit described in claim 14 is characterized in that, it is the low concentration occasion of 0.001～20ppmv that this catalytic conversion unit is used for the cleaning organic waste gas concentration that becomes a mandarin.
20., it is characterized in that the operation ozone of this catalyst adsorption and oxidation unit and become a mandarin the organic concentration molar ratio between 0.5～2.0 like each described catalytic conversion unit in the claim 5,6,7,17.
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