CN203577632U - Electrochemical reaction device - Google Patents
Electrochemical reaction device Download PDFInfo
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- CN203577632U CN203577632U CN201320678152.8U CN201320678152U CN203577632U CN 203577632 U CN203577632 U CN 203577632U CN 201320678152 U CN201320678152 U CN 201320678152U CN 203577632 U CN203577632 U CN 203577632U
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- 238000003487 electrochemical reaction Methods 0.000 title claims abstract description 23
- 239000006185 dispersion Substances 0.000 claims abstract description 28
- 239000007789 gas Substances 0.000 abstract description 136
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 abstract description 30
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 29
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 26
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 25
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 25
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 abstract description 22
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 17
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 17
- 239000011574 phosphorus Substances 0.000 abstract description 17
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 15
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 13
- 239000001569 carbon dioxide Substances 0.000 abstract description 13
- 238000012545 processing Methods 0.000 abstract description 13
- 229910000147 aluminium phosphate Inorganic materials 0.000 abstract description 11
- 239000012528 membrane Substances 0.000 abstract 2
- 229910052717 sulfur Inorganic materials 0.000 abstract 2
- 239000011593 sulfur Substances 0.000 abstract 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 abstract 1
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 47
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 39
- 239000003054 catalyst Substances 0.000 description 32
- 238000007254 oxidation reaction Methods 0.000 description 28
- 230000003647 oxidation Effects 0.000 description 27
- 230000003197 catalytic effect Effects 0.000 description 26
- 239000000243 solution Substances 0.000 description 21
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 17
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 17
- 239000005997 Calcium carbide Substances 0.000 description 15
- 239000005864 Sulphur Substances 0.000 description 15
- 238000000034 method Methods 0.000 description 15
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 15
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 14
- 239000008246 gaseous mixture Substances 0.000 description 14
- 229910021529 ammonia Inorganic materials 0.000 description 12
- 239000007791 liquid phase Substances 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 12
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 10
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 10
- 238000002360 preparation method Methods 0.000 description 10
- 238000000746 purification Methods 0.000 description 10
- 238000006056 electrooxidation reaction Methods 0.000 description 8
- 238000000909 electrodialysis Methods 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- 239000002253 acid Substances 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 238000005868 electrolysis reaction Methods 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052763 palladium Inorganic materials 0.000 description 5
- KWSLGOVYXMQPPX-UHFFFAOYSA-N 5-[3-(trifluoromethyl)phenyl]-2h-tetrazole Chemical compound FC(F)(F)C1=CC=CC(C2=NNN=N2)=C1 KWSLGOVYXMQPPX-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- 229910001379 sodium hypophosphite Inorganic materials 0.000 description 4
- OBSZRRSYVTXPNB-UHFFFAOYSA-N tetraphosphorus Chemical compound P12P3P1P32 OBSZRRSYVTXPNB-UHFFFAOYSA-N 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 238000000855 fermentation Methods 0.000 description 3
- 230000004151 fermentation Effects 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 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 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 239000004065 semiconductor Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000001360 synchronised effect Effects 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 229910052725 zinc Inorganic materials 0.000 description 3
- 239000011701 zinc Substances 0.000 description 3
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 2
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Chemical compound [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- 229910021380 Manganese Chloride Inorganic materials 0.000 description 1
- GLFNIEUTAYBVOC-UHFFFAOYSA-L Manganese chloride Chemical compound Cl[Mn]Cl GLFNIEUTAYBVOC-UHFFFAOYSA-L 0.000 description 1
- ROJYSBSWRTYOFQ-UHFFFAOYSA-N N#CC#N.[S].[P] Chemical compound N#CC#N.[S].[P] ROJYSBSWRTYOFQ-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 1
- 238000007084 catalytic combustion reaction Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 1
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 1
- 229910000428 cobalt oxide Inorganic materials 0.000 description 1
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 description 1
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000005518 electrochemistry Effects 0.000 description 1
- 238000010894 electron beam technology Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000011565 manganese chloride Substances 0.000 description 1
- 235000002867 manganese chloride Nutrition 0.000 description 1
- 229940099607 manganese chloride Drugs 0.000 description 1
- 229940099596 manganese sulfate Drugs 0.000 description 1
- 239000011702 manganese sulphate Substances 0.000 description 1
- 235000007079 manganese sulphate Nutrition 0.000 description 1
- SQQMAOCOWKFBNP-UHFFFAOYSA-L manganese(II) sulfate Chemical compound [Mn+2].[O-]S([O-])(=O)=O SQQMAOCOWKFBNP-UHFFFAOYSA-L 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000006385 ozonation reaction Methods 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 150000005838 radical anions Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 229910001428 transition metal ion Inorganic materials 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000011592 zinc chloride Substances 0.000 description 1
- 235000005074 zinc chloride Nutrition 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
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Abstract
The utility model discloses an electrochemical reaction device. The electrochemical reaction device comprises a positive electrode, a negative electrode, a gas dispersion device and an electrolytic bath, wherein a baffle plate is arranged inside the electrolytic bath, is close to the positive electrode and is connected with a cover plate, a negative membrane is arranged in the electrolytic bath and is close to the negative electrode, the negative membrane is connected with the bottom of the electrolytic bath, and the gas dispersion device is arranged in a gas inlet on the bottom of the electrolytic bath. The electrochemical reaction device can be used for processing one or more of mixed gases containing phosphorus, sulfur and cyanogen at low temperature and normal pressure, and the phosphorus, the sulfur and the cyanogen are respectively oxidized to obtain phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia gas after the processing.
Description
Technical field
The utility model relates to a kind of electrochemical reaction appts, belongs to isolation of purified and the environmental engineering technical field of poisonous dusty gas.
Background technology
Not only environmental pollution is controlled for phosphorus, sulphur, cyanogen deep purifying, reduction of greenhouse gas discharge is significant, can also promote cleaning process technology level, promote the industry restructuring of western low developed area, promote resource and the comprehensive utilization of gaseous mixture, produce significant economic benefit, phosphorus (PH
3), sulphur (H
2s), cyanogen (HCN) is as hypertoxic odorant pollutant, can be present in the tail gas of many industrial production discharges, a large amount of containing H such as all producing in the processes such as biomass cracking, coal tar, coal liquefaction, coal gasification, blast furnace ironmaking
2the tail gas of S, HCN, can produce in the processes such as phosphorus production, calcium carbide production simultaneously containing PH
3, H
2the tail gas of S, HCN; Yellow phosphoric tail gas, calcium carbide stove exhaust, blast furnace gas, tail gas of converter etc. are again often the tail gas that is rich in valuable source value CO on the other hand, if phosphorus sulphur cyanogen wherein is effectively purified and will make these tail gas become valuable resource, particularly for being mainly distributed in the yellow phosphorus in west area and the tail gas in closed calcium carbide furnace production process, the selective deep removal technology of phosphorus, sulphur, cyanogen realizes especially exhaust-gas resource high value added utilization, promotes the key technology of industrial structure upgrading transition, not only environmental pollution can be reduced, significant economic benefit can also be produced; In phosphorus production process, the discharge of every production 1t yellow phosphorus is containing tail gas 2500～3000Nm of 85%～95% CO in theory
3, by this, calculate, only Yunnan Province's yellow phosphorus electric furnace at least produces CO 1,200,000,000 Nm for 2011
3, amount to CO
2discharge capacity 2,360,000 t/a, if the impurity such as these yellow phosphoric tail gas that are rich in CO institute after purifying is phosphorous, sulphur, cyanogen are lower than 1mg/m
3, can be used as most valuable material gas and produce C1 chemical products, can create the output value of 13,800,000,000 yuans every year, both can avoid environmental pollution, can turn waste into wealth again, reduce the production cost of yellow phosphorus.But due to the PH in yellow phosphoric tail gas
3, H
2s, HCN impurity are difficult to effective purification, current most of yellow phosphoric tail gas can only be used as the dry inferior fuel of the distillation of phosphorus mud, phosphorus ore and coke, after unnecessary gas ignition, discharge, the phosphide that burning produces, sulfide, fluoride etc. are with greenhouse gases CO
2enter in the lump atmosphere, ecological environment is caused to great pollution, be also the waste of CO resource simultaneously; Calcium carbide have the good reputation of " mother of organic synthesis industry ", is important foundation industrial chemicals, China calcium carbide output 1,737 ten thousand t in 2011, and in the closed calcium carbide furnace calcium carbide production process of conduct calcium carbide production from now on main flow, every production 1t calcium carbide produces approximately 400 Nm
3containing the tail gas of CO 80%～85%, as using after these tail gas clean-ups as C1 material gas, CO
2reduction of discharging will be over 1,000 ten thousand t/a, and the economic benefit of creation surpasses 60,000,000,000 yuan/a.Compare with yellow phosphoric tail gas, closed calcium carbide furnace tail gas is high containing Dust Capacity, but exist equally existing phosphorus, sulphur, cyanogen remove technology be difficult to meet its purify after as the problem of C1 material gas requirement, most with the direct burning and exhausting of the form of igniting the torch in closed calcium carbide furnace tail gas at present, also caused the waste of serious secondary pollution, a large amount of greenhouse gas emission and CO resource.
Existing in a large number to PH both at home and abroad
3, H
2the Study on purification report of S and HCN, but most research is only confined to the purification of pure gas component, the research purifying about their synchronous depth-selectiveness also lacks very much, and purification techniques far can not meet actual industrial gas low-cost high-efficiency and purify requirement.At present for PH
3purification have the methods such as burning, oxidant oxidation absorption, physical absorption, solid catalysis oxidation, thermal decomposition, liquid phase catalytic oxidation.For H
2the purification of S has the methods such as bioanalysis, physical absorption, Ozonation, electrochemical oxidation, electron beam irradiation microwave decomposition method, Immesion active carbon catalytic oxidation, liquid phase catalytic oxidation, and has the methods such as chemisorbed purification, Low Temperature Solid-Phase catalytic oxidation, CaO high-temperature oxydation, catalytic combustion, catalyzing hydrolysis for the purification of HCN.In addition, also report has for producing H in living beings or coal thermal cracking processes
2the technology such as the KXIT purification that the selective bi-component of S and HCN purifies, liquid phase catalytic oxidation technology.
Yet there are no the research report about phosphorus, sulphur, the synchronous device for deep cleaning of cyanogen, if realizing phosphorus, sulphur, the synchronous degree of depth of cyanogen deviates from, not only can shortened process, effectively reduce and purify cost, and can promote the large-scale application of tail gas recycling engineering.
Summary of the invention
The purpose of this utility model is a kind of electrochemical reaction appts, this device comprises: anode 1, negative electrode 2, gas dispersion apparatus 8, electrolytic cell 11, electrolytic cell 11 is interior has baffle plate 5 near anode 1 place, baffle plate 5 is connected with cover plate 10, with electrolytic cell 11 bottoms from, on the cover plate 10 between baffle plate 5 and anode 1, be provided with anodic gas outlet 3, at the interior close negative electrode of electrolytic cell 11, there is cavity block 6 at 2 places, cavity block 6 is connected with electrolytic cell 11 bottoms, with cover plate 10 from, on the cover plate 10 between cavity block 6 and negative electrode 2, be provided with cathode gas outlet 4, there is gas dispersion apparatus 8 at 7 places, electrolytic cell 11 gas access, bottom, gas access 7 is connected with gas dispersion apparatus 8.
Electrochemical reaction appts described in the utility model is used for to catalyzing, oxidizing and purifying phosphorus, sulphur, cyanogen, comprise the steps: under normal pressure, pass through electrochemical oxidation, the acting in conjunction of liquid-phase catalyst catalytic oxidation is by phosphine containing, hydrogen sulfide, the gaseous mixture of one or more in hydrogen cyanide is processed, by hydrogen phosphide, hydrogen sulfide, hydrogen cyanide is oxidized to respectively phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia, in conjunction with electrodialysis, realize the purification of mist, Sync enrichment concentrating and separating catalytic oxidation product, reaction temperature is 4 ~ 100 ℃, the power supply mode of electrochemical reaction comprises direct current or pulse, voltage is 0.1-40V, current density is 30-900A/m
2.
Catalyst described in the utility model is one or both the aqueous solution or the acid solution of soluble transition metal ion containing in palladium, manganese, copper, zinc, cobalt, nickel, iron, process for preparation is: get the material that one or both contain palladium, manganese, copper, zinc, cobalt, nickel, iron, stirring and dissolving is in mass percent is less than or equal to 30% acid solution or distilled water respectively, mix, filter to obtain mixed catalytic agent solution, in mixed catalytic agent solution, precious metal palladium mass percent concentration is 0.05
~50g/L, the mass percent concentration of iron, manganese, copper, zinc, nickel, cobalt is 0.1
~150g/L, acid solution described in the utility model is a kind of in hydrochloric acid, nitric acid, sulfuric acid.
Electrochemical reaction appts described in the utility model is for catalyzing, oxidizing and purifying phosphorus, sulphur, cyanogen, and detailed process is as follows: one or more the tail gas in phosphorous, sulphur, cyanogen be take to gas flow rate as 1-15m
3the flow velocity of/h enters in reactor through gas dispersion apparatus 8 from the gas access 7 of device bottom, under the effect of catalyst in reactor, there is catalytic oxidation in gas component, wherein hydrogen phosphide is oxidized to phosphoric acid, hydrogen sulfide is oxidized to elemental sulfur, hydrogen cyanide is absorbed at absorption chamber more greatly because of solubility, and catalyzed carbon dioxide and nitrogen or the ammonia of being oxidized to of part, part is passed through baffle plate 5 bottom mass transfers near anode 1, near anode 1, by electrochemistry oxygen, turned to carbon dioxide and nitrogen or ammonia, gas is discharged from the gas vent 3 of anode chamber, through purified gas, from cathode chamber gas vent 4, discharge, the cation of catalyst is isolated by cavity block 6, can not migrate to negative electrode 2 is reduced
,anode 1 electrolysis produces oxygen, can be oxidized the catalytic component being reduced on the one hand, catalyst is regenerated, keep its activity, and then the stability of the interior catalyst system and catalyzing of maintenance reactor, the oxygen that electrolysis produces on the other hand, can alleviate because of oxygen content deficiency and oxygen in mixed tail gas to mass transfer in liquid phase phosphorus, sulphur, the restrictive function of cyanogen catalytic oxidation, baffle plate 5 can prevent that the gas that anode 1 generates from entering in purified gas, the hydrogen that negative electrode 2 electrolysis produce can be incorporated in purified gas, after liquid phase acid solution reaches certain concentration, the electrode direction of transposing anode 1 and negative electrode 2, by electrodialytic method, make the acid radical anion generating see through cavity block 6, reach the acid generating and the object of catalyst separation, elemental sulfur air supporting under the effect that enters groove air-flow that reaction generates rises to liquid level, sulphur cream 9 can regularly strike off.
Cleaning principle of the present utility model:
PH
3+2O
2=H
3PO
4
2H
2S+O
2=2S↓+2H
2O
4HCN+5O
2=2N
2+4CO
2+2H
2O
The beneficial effects of the utility model:
(1) can synchronously evolve phosphorus, sulphur, cyanogen of device described in the utility model, technological process is simple, under low temperature, normal pressure, carries out, and operating condition is gentle;
(2) device described in the utility model can be oxidized to phosphorus, sulphur, cyanogen respectively phosphoric acid, elemental sulfur, carbon dioxide and the nitrogen (or ammonia) of low toxicity, and oxidation product is easy to separation, and phosphoric acid and elemental sulfur etc. can further utilize;
(3) device described in the utility model carries out purified treatment to being rich in yellow phosphoric tail gas and the closed calcium carbide furnace tail gas of carbon monoxide, at cathode chamber, can electrolysis produce hydrogen, it is synthetic that this part gas and purified gas (principal component is carbon monoxide) are mixed for carbonyl, reduce the required device of conversion and expense, be conducive to the resource recycling of refuse;
(4) in the electrolytic cell of device described in the utility model, contained soluble catalyst solution can be recycled, little on catalytic oxidation performance impact.
Accompanying drawing explanation
Fig. 1 is the structural representation of catalytic oxidizing equipment in the utility model;
In figure: 1-anode, 2-negative electrode, the outlet of 3-anodic gas, the outlet of 4-cathode gas, 5-baffle plate, 6-cavity block, 7-gas access, 8-gas dispersion apparatus, the sulphur simple substance that 9-reaction produces, 10-cover plate, electrolytic cell 11.
The specific embodiment
Below in conjunction with embodiment and accompanying drawing, the utility model is described in further detail, but the utility model protection domain is not limited to described content.
Embodiment 1:
Electrochemical reaction appts described in the present embodiment, comprise anode 1, negative electrode 2, gas dispersion apparatus 8, electrolytic cell 11, electrolytic cell 11 is interior has baffle plate 5 near anode 1 place, baffle plate 5 is connected with cover plate 10, with electrolytic cell 11 bottoms from, on the cover plate 10 between baffle plate 5 and anode 1, be provided with anodic gas outlet 3, at the interior close negative electrode of electrolytic cell 11, there is cavity block 6 at 2 places, cavity block 6 is connected with electrolytic cell 11 bottoms, with cover plate 10 from, on the cover plate 10 between cavity block 6 and negative electrode 2, be provided with cathode gas outlet 4, there is gas dispersion apparatus 8 at 7 places, electrolytic cell 11 gas access, bottom, as shown in Figure 1.
With yellow phosphoric tail gas, (main component percent by volume consists of CO 85%-90%, CO to the present embodiment
21%-4%, H
21%-8%, N
22%-5%, H
2o 2%-5%, PH
3400-1400mg/m
3, H
2s 800-3000mg/Nm
3, HCN 100-300mg/Nm
3) for processing object, under normal pressure, one or more the gaseous mixture in phosphine containing, hydrogen sulfide, hydrogen cyanide is processed in acting in conjunction by electrochemical oxidation, liquid-phase catalyst catalytic oxidation, hydrogen phosphide, hydrogen sulfide, hydrogen cyanide are oxidized to respectively to phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia, in conjunction with electrodialysis, realize the Sync enrichment concentrating and separating catalytic oxidation product that purifies gaseous mixture, reaction temperature is 4 ℃, the power supply mode of electrochemical reaction is pulse, current density 30A/m
2.
The preparation of catalyst described in the present embodiment: get 1500g copper chloride and be dissolved in 5L water, 0.5g palladium bichloride is dissolved in the hydrochloric acid of 5L 10%, then both are mixed, filters, and discards filter residue, obtains catalyst solution;
Will through washing and alkali cleaning after yellow phosphoric tail gas with 1m
3/ h flow velocity passes into electrolytic cell from reactor lower part gas access 7 through gas dispersion apparatus 8, when being 4 ℃, temperature reacts with the catalyst solution preparing, the solubility of hydrogen cyanide is larger, by baffle plate 5, can make its part that there is no complete oxidation enter anode chamber by baffle plate 5 bottoms, in anode chamber, be further oxidized to carbon dioxide and nitrogen or ammonia, gas is discharged from the gas vent 3 of anode chamber, hydrogen through purified gas and cathode chamber electrolysis generation is discharged from cathode chamber gas vent 4, after measured, in the yellow phosphoric tail gas of processing in electrolytic cell, Phosphine content is 0, hydrogen sulfide content is 0, hydrogen cyanide content is 0.
Embodiment 2:
Electrochemical reaction appts described in the present embodiment, comprise anode 1, negative electrode 2, gas dispersion apparatus 8, electrolytic cell 11, electrolytic cell 11 is interior has baffle plate 5 near anode 1 place, baffle plate 5 is connected with cover plate 10, with electrolytic cell 11 bottoms from, on the cover plate 10 between baffle plate 5 and anode 1, be provided with anodic gas outlet 3, at the interior close negative electrode of electrolytic cell 11, there is cavity block 6 at 2 places, cavity block 6 is connected with electrolytic cell 11 bottoms, with cover plate 10 from, on the cover plate 10 between cavity block 6 and negative electrode 2, be provided with cathode gas outlet 4, there is gas dispersion apparatus 8 at 7 places, electrolytic cell 11 gas access, bottom.
With closed calcium carbide furnace tail gas, (main component percent by volume consists of CO 80%-85%, H to the present embodiment
26%-8%, CO
21%-3%, O
21.5%-3.5%, N
26%-8%, PH
3200-950mg/m
3, H
2s 300-900mg/Nm
3, HCN 1500-3000mg/Nm
3) for processing object, under normal pressure, one or more the gaseous mixture in phosphine containing, hydrogen sulfide, hydrogen cyanide is processed in acting in conjunction by electrochemical oxidation, liquid-phase catalyst catalytic oxidation, hydrogen phosphide, hydrogen sulfide, hydrogen cyanide are oxidized to respectively to phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia, in conjunction with electrodialysis, realize the Sync enrichment concentrating and separating catalytic oxidation product that purifies gaseous mixture, reaction temperature is 40 ℃, the power supply mode of electrochemical reaction is pulse, and current density is 100A/m
2.
The preparation of catalyst described in the present embodiment: get 1200g zinc nitrate and be dissolved in 5L water, 60g cobalt nitrate is dissolved in 5L 30% nitric acid, then both are mixed, filters, and discards filter residue, obtains mixed catalyst solution for standby.
To after dust removal process, take closed calcium carbide furnace tail gas that carbon monoxide is main component with 15m
3/ h flow velocity passes into electrolytic cell from reactor lower part gas access 7 through gas dispersion apparatus 8, when temperature is 40 ℃ with the mixed catalyst solution reaction for preparing, the solubility of hydrogen cyanide is larger, by baffle plate 5, can make its part that there is no complete oxidation enter anode chamber by baffle plate 5 bottoms, in anode chamber, be further oxidized to carbon dioxide and nitrogen or ammonia, gas is discharged from the gas vent 3 of anode chamber, hydrogen through purified gas and cathode chamber electrolysis generation is discharged from cathode chamber gas vent 4, after measured, in the closed calcium carbide furnace tail gas of processing in electrolytic cell, Phosphine content is 0, hydrogen sulfide content is 0, hydrogen cyanide content is 0.
Embodiment 3:
Electrochemical reaction appts described in the present embodiment, comprise anode 1, negative electrode 2, gas dispersion apparatus 8, electrolytic cell 11, electrolytic cell 11 is interior has baffle plate 5 near anode 1 place, baffle plate 5 is connected with cover plate 10, with electrolytic cell 11 bottoms from, on the cover plate 10 between baffle plate 5 and anode 1, be provided with anodic gas outlet 3, at the interior close negative electrode of electrolytic cell 11, there is cavity block 6 at 2 places, cavity block 6 is connected with electrolytic cell 11 bottoms, with cover plate 10 from, on the cover plate 10 between cavity block 6 and negative electrode 2, be provided with cathode gas outlet 4, there is gas dispersion apparatus 8 at 7 places, electrolytic cell 11 gas access, bottom.
The present embodiment be take semi-conductor industry production tail gas as processing object, under normal pressure, one or more the gaseous mixture in phosphine containing, hydrogen sulfide, hydrogen cyanide is processed in acting in conjunction by electrochemical oxidation, liquid-phase catalyst catalytic oxidation, hydrogen phosphide, hydrogen sulfide, hydrogen cyanide are oxidized to respectively to phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia, in conjunction with electrodialysis, realize the Sync enrichment concentrating and separating catalytic oxidation product that purifies gaseous mixture, reaction temperature is 60 ℃, the power supply mode of electrochemical reaction is direct current, and current density is 400A/m
2.
The preparation of catalyst described in the present embodiment: get 500g simple substance palladium and be dissolved in 5L 5% hydrochloric acid, 1g manganese chloride is dissolved in 5L water, then both are mixed, filters, and discards filter residue, obtains mixed catalyst solution for standby.
By Phosphine content, be 400mg/m
3, O
2the semi-conductor industry of percent by volume 20% left and right is produced tail gas with 10m
3/ h flow velocity passes into electrolytic cell from reactor lower part gas access 7 through gas dispersion apparatus 8, when temperature is 60 ℃ with the mixed catalyst solution reaction for preparing, through purified gas, from cathode chamber gas vent 4, discharge, after measured, it is 0 that the semi-conductor industry of processing in electrolytic cell is produced Phosphine content in tail gas.
Embodiment 4:
Electrochemical reaction appts described in the present embodiment, comprise anode 1, negative electrode 2, gas dispersion apparatus 8, electrolytic cell 11, electrolytic cell 11 is interior has baffle plate 5 near anode 1 place, baffle plate 5 is connected with cover plate 10, with electrolytic cell 11 bottoms from, on the cover plate 10 between baffle plate 5 and anode 1, be provided with anodic gas outlet 3, at the interior close negative electrode of electrolytic cell 11, there is cavity block 6 at 2 places, cavity block 6 is connected with electrolytic cell 11 bottoms, with cover plate 10 from, on the cover plate 10 between cavity block 6 and negative electrode 2, be provided with cathode gas outlet 4, there is gas dispersion apparatus 8 at 7 places, electrolytic cell 11 gas access, bottom.
It is processing object that the present embodiment Using Sodium Hypophosphite is produced the tail gas producing, under normal pressure, one or more the gaseous mixture in phosphine containing, hydrogen sulfide, hydrogen cyanide is processed in acting in conjunction by electrochemical oxidation, liquid-phase catalyst catalytic oxidation, hydrogen phosphide, hydrogen sulfide, hydrogen cyanide are oxidized to respectively to phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia, in conjunction with electrodialysis, realize the Sync enrichment concentrating and separating catalytic oxidation product that purifies gaseous mixture, reaction temperature is 55 ℃, the power supply mode of electrochemical reaction is direct current, and current density is 600A/m
2.
It is processing object that the present embodiment Using Sodium Hypophosphite is produced the tail gas producing, and concrete steps are as follows:
The preparation of catalyst described in the present embodiment: get 100g zinc oxide and be dissolved in 5L water, 150g manganese sulfate is dissolved in the hydrochloric acid of 5L 25%, mixes both, filters, and discards filter residue, obtains catalyst solution standby.
To take Sodium hypophosphite production tail gas that hydrogen phosphide is main component with 2m
3/ h flow velocity passes into electrolytic cell from reactor lower part gas access 7 through gas dispersion apparatus 8, at 55 ℃, react with the catalyst solution preparing, through purified gas, from cathode chamber gas vent 4, discharge, in the tail gas that treated Sodium hypophosphite production produces, Phosphine content is 0.
Embodiment 5:
Electrochemical reaction appts described in the present embodiment, comprise anode 1, negative electrode 2, gas dispersion apparatus 8, electrolytic cell 11, electrolytic cell 11 is interior has baffle plate 5 near anode 1 place, baffle plate 5 is connected with cover plate 10, with electrolytic cell 11 bottoms from, on the cover plate 10 between baffle plate 5 and anode 1, be provided with anodic gas outlet 3, at the interior close negative electrode of electrolytic cell 11, there is cavity block 6 at 2 places, cavity block 6 is connected with electrolytic cell 11 bottoms, with cover plate 10 from, on the cover plate 10 between cavity block 6 and negative electrode 2, be provided with cathode gas outlet 4, there is gas dispersion apparatus 8 at 7 places, electrolytic cell 11 gas access, bottom.
Tail gas (the PH that the present embodiment produces with feed fermentation
3content is less than 50mg/Nm
3) for processing object, under normal pressure, one or more the gaseous mixture in phosphine containing, hydrogen sulfide, hydrogen cyanide is processed in acting in conjunction by electrochemical oxidation, liquid-phase catalyst catalytic oxidation, hydrogen phosphide, hydrogen sulfide, hydrogen cyanide are oxidized to respectively to phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia, in conjunction with electrodialysis, realize the Sync enrichment concentrating and separating catalytic oxidation product that purifies gaseous mixture, reaction temperature is 80 ℃, the power supply mode of electrochemical reaction is direct current, and current density is 750A/m
2.
The preparation of catalyst described in the present embodiment: get cobalt oxide 300g and be dissolved in 5L water, 800g zinc chloride is dissolved in the hydrochloric acid of 5L 20%, then both are mixed, and is mixed with 10L solution, filters, and discards filter residue, obtains mixed catalyst solution for standby.
The tail gas that feed fermentation is produced is with 14m
3the flow velocity of/h passes into electrolytic cell from reactor lower part gas access 7 through gas dispersion apparatus 8, when temperature is 80 ℃ with the mixed catalyst solution reaction for preparing, through purified gas, from cathode chamber gas vent 4, discharge, after measured, in the tail gas that the feed fermentation of processing in electrolytic cell produces, Phosphine content is 0.
Embodiment 6:
Electrochemical reaction appts described in the present embodiment, comprise anode 1, negative electrode 2, gas dispersion apparatus 8, electrolytic cell 11, electrolytic cell 11 is interior has baffle plate 5 near anode 1 place, baffle plate 5 is connected with cover plate 10, with electrolytic cell 11 bottoms from, on the cover plate 10 between baffle plate 5 and anode 1, be provided with anodic gas outlet 3, at the interior close negative electrode of electrolytic cell 11, there is cavity block 6 at 2 places, cavity block 6 is connected with electrolytic cell 11 bottoms, with cover plate 10 from, on the cover plate 10 between cavity block 6 and negative electrode 2, be provided with cathode gas outlet 4, there is gas dispersion apparatus 8 at 7 places, electrolytic cell 11 gas access, bottom.
It is to process object that the present embodiment be take the tail gas that magnesium powder preparation produces, under normal pressure, one or more the gaseous mixture in phosphine containing, hydrogen sulfide, hydrogen cyanide is processed in acting in conjunction by electrochemical oxidation, liquid-phase catalyst catalytic oxidation, hydrogen phosphide, hydrogen sulfide, hydrogen cyanide are oxidized to respectively to phosphoric acid, elemental sulfur, carbon dioxide and nitrogen or ammonia, in conjunction with electrodialysis, realize the Sync enrichment concentrating and separating catalytic oxidation product that purifies gaseous mixture, reaction temperature is 100 ℃, the power supply mode of electrochemical reaction is direct current, and current density is 900A/m
2.
The preparation of catalyst described in the present embodiment: get copper sulphate 1000g and be dissolved in 10L water, be mixed with 10L solution, filter, discard filter residue, obtain mixed catalyst solution for standby.
By the phosphine containing producing in magnesium powder preparation process (content < 50mg/m
3) tail gas is with 15m
3/ h flow velocity passes into electrolytic cell from reactor lower part gas access 7 through gas dispersion apparatus 8, when temperature is 100 ℃ with the mixed catalyst solution reaction preparing, through purified gas, from cathode chamber gas vent 4, discharge, after measured, in the tail gas that the magnesium powder preparation of processing in electrolytic cell produces, Phosphine content is 0.
Claims (1)
1. an electrochemical reaction appts, it is characterized in that: comprise anode (1), negative electrode (2), gas dispersion apparatus (8), electrolytic cell (11), in electrolytic cell (11), near anode (1), located baffle plate (5), baffle plate (5) is connected with cover plate (10), with electrolytic cell (11) bottom from, on the cover plate (10) between baffle plate (5) and anode (1), be provided with anodic gas outlet (3), in electrolytic cell (11), near negative electrode (2), located cavity block (6), cavity block (6) is connected with electrolytic cell (11) bottom, with cover plate (10) from, on the cover plate (10) between cavity block (6) and negative electrode (2), be provided with cathode gas outlet (4), gas dispersion apparatus (8) has been located in electrolytic cell (11) gas access, bottom (7), gas access (7) is connected with gas dispersion apparatus (8).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103551031A (en) * | 2013-10-31 | 2014-02-05 | 昆明理工大学 | Method and device for purifying phosphorus, sulfur and cyanogen under synergetic action of electrochemical oxidation and liquid phase catalytic oxidation |
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2013
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103551031A (en) * | 2013-10-31 | 2014-02-05 | 昆明理工大学 | Method and device for purifying phosphorus, sulfur and cyanogen under synergetic action of electrochemical oxidation and liquid phase catalytic oxidation |
| CN103551031B (en) * | 2013-10-31 | 2015-05-20 | 昆明理工大学 | Method and device for purifying phosphorus, sulfur and cyanogen under synergetic action of electrochemical oxidation and liquid phase catalytic oxidation |
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