CN103920365B - Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide - Google Patents
Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide Download PDFInfo
- Publication number
- CN103920365B CN103920365B CN201410160445.6A CN201410160445A CN103920365B CN 103920365 B CN103920365 B CN 103920365B CN 201410160445 A CN201410160445 A CN 201410160445A CN 103920365 B CN103920365 B CN 103920365B
- Authority
- CN
- China
- Prior art keywords
- sulfur dioxide
- furnace gas
- nitrogen
- gas
- variable
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 174
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 239000007789 gas Substances 0.000 title claims abstract description 71
- 238000000034 method Methods 0.000 title claims abstract description 60
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 44
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 229910052683 pyrite Inorganic materials 0.000 title claims abstract description 30
- 239000011028 pyrite Substances 0.000 title claims abstract description 30
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 28
- 238000011084 recovery Methods 0.000 title claims description 16
- 239000007788 liquid Substances 0.000 claims abstract description 48
- 230000008569 process Effects 0.000 claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 14
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000001035 drying Methods 0.000 claims abstract description 10
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims abstract description 10
- 239000004810 polytetrafluoroethylene Substances 0.000 claims abstract description 10
- -1 polytetrafluoroethylene Polymers 0.000 claims abstract description 9
- 230000018044 dehydration Effects 0.000 claims abstract description 7
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 7
- 229910052742 iron Inorganic materials 0.000 claims abstract description 6
- 230000006835 compression Effects 0.000 claims abstract description 5
- 238000007906 compression Methods 0.000 claims abstract description 5
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims abstract description 5
- 238000012545 processing Methods 0.000 claims abstract description 3
- 239000003463 adsorbent Substances 0.000 claims description 48
- 229910052799 carbon Inorganic materials 0.000 claims description 23
- 238000001179 sorption measurement Methods 0.000 claims description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 18
- 239000002893 slag Substances 0.000 claims description 17
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 claims description 14
- 239000002808 molecular sieve Substances 0.000 claims description 13
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 13
- 238000001556 precipitation Methods 0.000 claims description 9
- 238000000855 fermentation Methods 0.000 claims description 8
- 230000004151 fermentation Effects 0.000 claims description 8
- 239000008367 deionised water Substances 0.000 claims description 7
- 229910021641 deionized water Inorganic materials 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 239000010802 sludge Substances 0.000 claims description 7
- 208000005156 Dehydration Diseases 0.000 claims description 6
- 238000006253 efflorescence Methods 0.000 claims description 6
- 238000011068 loading method Methods 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- 206010037844 rash Diseases 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- 229910000831 Steel Inorganic materials 0.000 claims description 5
- 238000003795 desorption Methods 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 238000001125 extrusion Methods 0.000 claims description 5
- 238000007710 freezing Methods 0.000 claims description 5
- 230000008014 freezing Effects 0.000 claims description 5
- 239000010959 steel Substances 0.000 claims description 5
- 230000000274 adsorptive effect Effects 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- 239000005539 carbonized material Substances 0.000 claims description 4
- ONCZQWJXONKSMM-UHFFFAOYSA-N dialuminum;disodium;oxygen(2-);silicon(4+);hydrate Chemical compound O.[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[Na+].[Na+].[Al+3].[Al+3].[Si+4].[Si+4].[Si+4].[Si+4] ONCZQWJXONKSMM-UHFFFAOYSA-N 0.000 claims description 4
- 229910052573 porcelain Inorganic materials 0.000 claims description 4
- 239000000843 powder Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 4
- 229940080314 sodium bentonite Drugs 0.000 claims description 4
- 229910000280 sodium bentonite Inorganic materials 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 238000012216 screening Methods 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims description 2
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 2
- 238000010926 purge Methods 0.000 claims description 2
- 239000013589 supplement Substances 0.000 claims description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 6
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 abstract description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 3
- 125000004122 cyclic group Chemical group 0.000 abstract description 3
- 239000001569 carbon dioxide Substances 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 235000010269 sulphur dioxide Nutrition 0.000 description 63
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 16
- 239000001301 oxygen Substances 0.000 description 16
- 229910052760 oxygen Inorganic materials 0.000 description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003575 carbonaceous material Substances 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 230000009965 odorless effect Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- JVBXVOWTABLYPX-UHFFFAOYSA-L sodium dithionite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])=O JVBXVOWTABLYPX-UHFFFAOYSA-L 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- ZKQDCIXGCQPQNV-UHFFFAOYSA-N Calcium hypochlorite Chemical compound [Ca+2].Cl[O-].Cl[O-] ZKQDCIXGCQPQNV-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-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
- 239000004952 Polyamide Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 239000007844 bleaching agent Substances 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000000645 desinfectant Substances 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- CEYULKASIQJZGP-UHFFFAOYSA-L disodium;2-(carboxymethyl)-2-hydroxybutanedioate Chemical compound [Na+].[Na+].[O-]C(=O)CC(O)(C(=O)O)CC([O-])=O CEYULKASIQJZGP-UHFFFAOYSA-L 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000002085 irritant Substances 0.000 description 1
- 231100000021 irritant Toxicity 0.000 description 1
- 229940057995 liquid paraffin Drugs 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000001509 sodium citrate Substances 0.000 description 1
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 description 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000004291 sulphur dioxide Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Landscapes
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses the method that nitrogen in roasting pyrite furnace gas and sulfur dioxide are reclaimed in the absorption of a kind of variable-frequency variable-voltage, processing step is: after the furnace gas udst separation of roasting pyrite drying and cooling, and the filter for refined sulfuric acid furnace gas through 200 order polytetrafluoroethylene (PTFE) materials removes grit and iron rust; Again by after the dehydration of essence de-tank degree of depth essence, deoxidation and carbon dioxide removal, the way of recycling variable-frequency variable-voltage absorption realizes N
2with SO
2separation, and then by compress or cool, gas-liquid separation obtains liquid SO
2, by the nitrogen separated and liquid SO
2bottling is for industrial; Be not liquefied be separated SO2 enter again compression or cooling, gas-liquid separation cyclic process, SO wherein
2constantly separate; The present invention realizes to roasting pyrite containing the comprehensive utilization of the mixing furnace gas of a large amount of nitrogen and sulfur dioxide and zero-emission, and the liquid sulfur dioxide purity of acquisition is high, and its process is green, safety, and energy-conservation, zero-emission, cost are low.
Description
Technical field
The present invention relates to the method that nitrogen in roasting pyrite furnace gas and sulfur dioxide are reclaimed in variable-frequency variable-voltage absorption.
Background technology
Liquid sulfur dioxide is the liquid of water white transparency, irritant stink.Its gasification property is strong, and when in air, sulfur dioxide concentration reaches 0.04% ~ 0.05%, sucking human body will be poisoning, has spread effect to breathing and eyes.Liquid sulfur dioxide is of many uses, it is a kind of important industrial chemicals, both can be used for producing synthetic fibers (mainly polyamide fibre), washing agent, rubber chemicals, sodium hydrosulfite (sodium dithionite), plastics, dyestuff, medicine, lubricating oil and asccharin etc., can be used as again cold-producing medium, bleaching powder, extinguishing chemical and disinfectant etc.In recent years, along with the development of China's modern industry, the demand of liquid towards sulfur dioxide is growing, and the output of sulfur dioxide liquid increases year by year, and the market demand is increasingly vigorous.
Furnace gas or the sulfur dioxide in tail gas of roasting pyrite account for about 7% ~ 12%, and sulfur trioxide accounts for 0.05% ~ 0.4%, and the sublimed sulfur of trace, oxygen and acid mist etc., and all the other are nitrogen.Be colourless gas under sulfur dioxide normal temperature and pressure, there is intense stimulus smell.Be discharged in air and can be oxidized to sulfur trioxide, sulfur trioxide is combined with steam and generates acid mist, thus corrosion relevant ferrous metal equipment, pipeline and instrument, shorten its service life.Therefore, remove or reclaim the sulfur dioxide in the furnace gas of roasting pyrite or tail gas, and being used, changing harmful to treasure, seem particularly urgent!
At present, the industrial sulphur dioxide production liquid sulfur dioxide that reclaims from roasting pyrite furnace gas or tail gas mainly contains ammonia-acid system, sodium citrate absorption method, water absorption method, partial condensation method and Wei Sangman---Luo Defa etc. both at home and abroad, all first these methods absorb the sulfur dioxide of flue gas or furnace gas with absorbents such as the organic amine of easy sulfur dioxide absorption, water or ammonia, desorb again, obtains high-concentration sulfur dioxide; Then high-concentration sulfur dioxide pressurization or freezing are obtained liquid sulfur dioxide.The restrictions such as these technology are more or less subject to that engineering reliability, economic rationality, reagent source are regional, the requirement of industry production feature and environmental protection.Ammonia-acid system as current domestic extensive utilization adopts liquefied ammonia or ammoniacal liquor as absorbent, and absorption efficiency is high, desulfurization is thorough, but technological process is complicated, equipment investment is large, operating cost is high, and the source of ammonia is subject to the restriction of region.Calcium method adopts limewash or milk of lime washing containing the flue gas of sulfur dioxide, forms calcium sulfite precipitation, generate calcium sulfate.This law technology is ripe, and production cost is low, but absorption rate is slow, absorbability is little, the actual application value of byproduct calcium sulfate little, the output quantity of slag is many, causes equipment Pipe-Line fouling serious.Sodium method uses the alkaline matters such as natrium citricum, sodium carbonate or NaOH to absorb the flue gas containing sulfur dioxide, generate sodium sulfite or solution of sodium bisulfite, advantage is that absorbability is large, absorption rate is fast, desulfuration efficiency is high, equipment is simple, easy to operate and less scaling, weak point is that raw material soda is more expensive, and production cost is high.The common issue of said method is: 1. desulphurization plant engineering investment cost is large.The subsequent treatment of the accessory substance 2. after desulfurization is difficult.Requirement or the environmental protection operating cost that 3. cannot meet environmental protection are high.
Nitrogen is a kind of gas of colorless and odorless odorless; nontoxic; there is good stability and very low boiling point; be widely used in oil exploitation, chemical industry security protection, protection weld metal, filling bulb, breeding, fruit grain accumulating, fresh-keeping, fire extinguishing, medical science, pharmacy etc.; it accounts for the 78.12%(volume fraction of air total amount), be the Main Ingredients and Appearance of air.
At present, the main method of industrial separation and recovery nitrogen from air has both at home and abroad: cryogenic rectification method, pressure swing adsorption method, membrane separation process and chemiadsorption etc., respectively have its pluses and minuses.
Wherein, the mechanism of cryogenic rectification method is liquefied by air compressing, according to the difference of each component boiling point, is separated, obtains required product through rectifying column rectifying.Large-scale industrial production oxygen, nitrogen, be most economical with cryogenic rectification method, occupy firmly dominant position in air separating method; Refrigerating loss simultaneously can low, institute's calorific requirement be tried one's best few as far as possible.Low temperature process is separated mainly containing the double-column process of separated oxygen, nitrogen simultaneously and producing the three-column process flow two kinds of oxygen, nitrogen and argon simultaneously of air.The development trend of low temperature process is: (1) maximizes, and maximumly reaches 220000m
3/ h nitrogen; (2) adopt structured packing, advantage is that flow is large, resistance is little, operating flexibility is large, efficiency is high; (3) combine with other process, reduce energy consumption, improve overall gross efficiency.The equipment operating of cryogenic rectification method is complicated, and investment is large, and energy consumption is large.
Pressure swing adsorption method oxygen utilizes zeolite molecular sieve to the absorption affinity of nitrogen higher than the characteristic oxygen separation of the absorption affinity to oxygen and nitrogen, or utilize the diffusion velocity of oxygen in carbon molecule microcellular system narrow gap be greater than nitrogen diffusion velocity, under far from equilibrium condition separated oxygen, nitrogen.Pressure swing adsorption method oxygen, nitrogen carry out at normal temperatures, and technical process has pressurized adsorbent, normal pressure desorb; Normal pressure adsorbs, vacuum desorption.The adsorbance of adsorbent to gas increases along with the rising of pressure, reduces along with the reduction of pressure, in the process reducing pressure, releases by the gas adsorbed, makes adsorbent reactivation.Pressure-variable adsorption is subject to the restriction of two key technologies: one is the exploitation of high-efficiency adsorbent; Two is the valve reliability of frequent switch and the raising of flexibility.At present, large-scale PSA device majority is steel and iron industry hydrogen manufacturing and being separated of syngas for synthetic ammonia CO2, and in sky divides, at present, separating power majority is 6000m
3device under/h.
Membrane separation process has strong adaptability, efficiency is high, flow process is short, equipment is simple, without running gear, easy to operate, floor space is little, small investment, energy-conservation, advanced technology, low power consumption and other advantages, development prospect and application wide.But the cost of film is very high, and reliability is low!
Chemical absorption method refers to that high-temperature alkaline fused salt mixt can absorb the oxygen in air under catalyst action, then releases oxygen through step-down or intensification desorb.The oxygen deviate from from fused salt, purity is 98% ~ 99.5%.This method is used for Large Air Separation Devices oxygen very large future, and oxygen output is at more than 500t/d, and compare with traditional low temperature process oxygen, efficiency can improve about 50%, also can produce a large amount of high-temperature water vapors simultaneously.
In sum, utilize both at home and abroad at present pressure swing adsorption improve from the mixing furnace gas of roasting pyrite the sulfur dioxide of furnace gas and nitrogen concentration, obtain liquid sulfur dioxide and nitrogen-rich gas rarely has report simultaneously.Therefore, be necessary to propose a kind of method utilizing transformation absorption technology to reclaim nitrogen in roasting pyrite furnace gas and sulfur dioxide, overcome the problem that tradition recovery valuable gases exists large, the follow-up accessory substance process difficulty of equipment investment and cannot meet environmental requirement, realize the comprehensive utilization to roasting pyrite flue gas and zero-emission.
Summary of the invention
The technical problem to be solved in the present invention is to provide the method that nitrogen in roasting pyrite furnace gas and sulfur dioxide are reclaimed in the absorption of a kind of variable-frequency variable-voltage, obtain liquid sulfur dioxide and nitrogen-rich gas by the method simultaneously, realize the comprehensive utilization of roasting pyrite flue gas, product diversification, its process is green, safety, zero-emission, and without the need to separately purchasing raw material, cost is low.
The present invention solves the problems of the technologies described above with following technical scheme:
Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide, processing step is as follows:
(1) by temperature purification and low temperature purification during the fluidized bed furnace furnace gas containing sulfur dioxide out of roasting pyrite is after the waste heat recovery cooling of high-temperature residual heat boiler, cyclone dust removal and electric precipitation, dedusting, except sulfur trioxide, drying and cooling, now, furnace gas temperature is 35 DEG C ~ 40 DEG C, be 7% ~ 12%, CO containing sulfur dioxide
2and O
2content lower than 1%, N
2be 87% ~ 92%;
(2) furnace gas after step (1) purge drying removes the grit and iron rust carried secretly in furnace gas again through the filter for refined sulfuric acid furnace gas of polytetrafluoroethylene (PTFE) material;
(3) step (2) gained furnace gas takes off water, the O of the trace in the adsorbent removing furnace gas of tank by the essence of loading combination carbon molecular sieve
2and CO
2, now, the water content in furnace gas is reduced to 2.1mg/kg ~ 3.2mg/kg, and the content of sulfur dioxide is 7.5% ~ 12.5%, N
2content be 87.5% ~ 92.5%;
(4) step (3) gained furnace gas enters surge tank, through the compression of band frequency converter compressor, at the bottom of adsorption tower, enters adsorption tower, and the sulfur dioxide in furnace gas, by the adsorbent on adsorbent bed, realizes nitrogen and is separated with sulfur dioxide; By the sulfur dioxide that adsorbs after depressurization desorption, by the vavuum pump suction surge tank of frequency converter, obtain liquid sulfur dioxide with pressurization or freezing; Gas-liquid mixture containing liquid sulfur dioxide and gaseous sulfur dioxide enters gas-liquid separator and carries out gas-liquid separation, and gained liquid sulfur dioxide is drained in steel cylinder to be collected stand-by, and its purity is 98.6% ~ 99.5%; Adsorbent obtains holomorphosis simultaneously; Adsorbent bed be evacuated after, be 0.10MPa ~ 0.50MPa with ejecting purity is 98.5% ~ 99.8%, pressure is 0.11MPa ~ 0.53MPa nitrogen from adsorption tower to the adsorbent bed reverse adsorptive pressure that boosts to again, adsorbent bed just beginning enters next sorption cycle process;
(5) be not liquefied a small amount of SO be separated
2circulation carry out step (4) compressed or cool, gas-liquid separation, sulfur dioxide wherein is constantly separated;
(6) be 98.5% ~ 99.8% by adsorption tower tower top nitrogen gas purity out, enter surge tank, then it be stand-by to bottle.
In described step (2), filter for refined sulfuric acid furnace gas is 200 orders.
The composition that the middle essence of loading combination carbon molecular sieve of described step (3) takes off the adsorbent of tank is: from the bottom up, the silochrom of the bottom to be quality be adsorbent mass 30% ~ 40%, the Kiselgel A of the second layer to be quality be adsorbent mass 20% ~ 30%, the sodium bentonite of third layer to be quality be adsorbent mass 10% ~ 20%, 4th layer is quality is adsorbent mass 5% ~ 10%13X molecular sieve, the carbon molecular sieve of the superiors' to be quality be adsorbent mass 15% ~ 20%, the mass percent summation of above-mentioned each component is 100%.
In described step (4), the pressure at expulsion of band frequency converter compressor is 0.13MPa ~ 0.55MPa, and delivery temperature is 35 DEG C ~ 41 DEG C.
Adsorbent described in described step (4), based on the active carbon made by natural pond slag, adds multiple Compound Supplement, its each component and mass percent as follows:
The mass percent summation of each component is 100% above.
Described natural pond slag active carbon is with natural pond slag for raw material, and its preparation method is: carry out extrusion dehydration with the natural pond slag after methane-generating pit fermentation through cleaning, filtration, removal of impurities and screw extruder or three roller extruders, make its moisture content be 8% ~ 10%; Again through mass ratio be 10%-20%, temperature be 30 DEG C ~ 40 DEG C liquor zinci chloridi soak 35 ~ 40 hours; Through screw extruder or three roller extruder extrusion dehydrations, dry or dry, making its moisture content be 5% ~ 10%; Gained natural pond slag is placed on the microwave irradiation being 2000W ~ 3000W through irradiation power in the crucible of porcelain or carborundum and carbonizes, exposure time is 20 minutes ~ 30 minutes, naturally after cooling, dry 25 hours with after 30 DEG C ~ 40 DEG C rinsed with deionized water again, efflorescence is 200 ~ 400 order attritive powders again, obtains described natural pond slag active carbon.
Described methane tank sludge carbonized material with marsh gas fermentation pool mud for raw material, its preparation method is: marsh gas fermentation pool mud is after screening precipitation drains, add the liquor zinci chloridi that mass concentration is 10%-20%, temperature is 30 DEG C ~ 40 DEG C and soak 20 hours, drain rear baking 24h, be placed on the microwave irradiation being 2000W ~ 3000W through irradiation power in the crucible of porcelain or carborundum to carbonize, exposure time is 10 minutes ~ 20 minutes, dry 25 hours with after 30 DEG C ~ 40 DEG C rinsed with deionized water again, efflorescence becomes 200 ~ 400 order attritive powders, obtains described methane tank sludge carbonized material.
Method of the present invention has the following advantages:
1, nitrogen and liquid sulfur dioxide can be obtained from roasting pyrite furnace gas simultaneously, achieve the comprehensive utilization of roasting pyrite furnace gas, and cost be low, process green, safety, zero-emission.
2, avoid the huge construction investment of enterprise's desulphurization plant and the environmental protection operating cost of great number, it also avoid the difficult disposal of sweetening process accessory substance simultaneously.
Accompanying drawing explanation
Fig. 1 is the process chart that the method for nitrogen in roasting pyrite furnace gas and sulfur dioxide is reclaimed in variable-frequency variable-voltage of the present invention absorption.
Detailed description of the invention
Embodiments of the present invention are described in detail below in conjunction with Fig. 1.
As shown in Figure 1, present invention process flow process is: what realize nitrogen and sulfur dioxide by the dehydration of the fluidized bed furnace furnace gas → cyclone dust removal → electric precipitation → drying → cooling → essence out of roasting pyrite de-tank degree of depth essence, deoxidation and carbon dioxide removal → transformation absorption is separated → compresses → condensation → gas-liquid separation → cooling → acquisition liquid SO2.
Embodiment 1:
By gentle low temperature cooling, purifying during the furnace gas out of the fluidized bed furnace by roasting pyrite is after high-temperature residual heat boiler recovery waste heat, cyclone dust removal and electric precipitation, dedusting and sulfur trioxide, drying and cooling, now, furnace gas temperature is 35 DEG C, be 12%, CO containing sulfur dioxide mass ratio
2and O
2content be 87% lower than 1%, N2; Filter for refined sulfuric acid furnace gas again through 200 order polytetrafluoroethylene (PTFE) materials removes the grit and iron rust carried secretly in gaseous mixture, and the essence then through loading combination carbon molecular sieve takes off minor amount of water, O in tank absorption removing mixing furnace gas
2and CO
2, now, the water content in mixing furnace gas is reduced to 2.1mg/kg, and the content of sulfur dioxide is about 12.5%, N
2content be about 87.5%; Then the compression of band frequency converter compressor, the exhaust pressure of band frequency converter compressor is 0.13MPa, and delivery temperature is normal temperature 35 DEG C; Furnace gas enters in adsorption tower bottom adsorption tower afterwards, the adsorbent sulfur dioxide on adsorbent bed, realizes being separated of nitrogen and sulfur dioxide; By adsorbent sulfur dioxide depressurization desorption, extracted by vavuum pump and send into surge tank, again high-concentration sulfur dioxide pressurization or freezing are obtained liquid sulfur dioxide, enter gas-liquid separator containing gas-liquid mixture that is liquid and gaseous sulfur dioxide and carry out gas-liquid separation, liquid sulfur dioxide after separation is drained in steel cylinder to be collected, and the purity of liquid sulfur dioxide is 98.6%; Adsorbent obtains holomorphosis simultaneously; Adsorbent bed vacuumize after, then be 0.10MPa with ejecting purity is 98.5%, pressure is 0.11MPa nitrogen from adsorption tower to the adsorbent bed reverse adsorptive pressure that boosts to, adsorbent bed just beginning enters next sorption cycle process.Be not liquefied a small amount of SO be separated
2again enter band frequency converter compressor, carry out compressing, cool and the cyclic process of gas-liquid separation, liquid sulfur dioxide wherein is constantly separated, and bottling confession is industrial.Be the N of 98.5% by tower top purity out
2bottle after entering surge tank stand-by.
The composition that described essence of loading combination carbon molecular sieve takes off the adsorbent of tank is: from the bottom up, the bottom is silochrom, and the second layer is Kiselgel A, and third layer is sodium bentonite, and the 4th layer is 13X molecular sieve, and the superiors are carbon molecular sieves.
Described adsorbent bed on adsorbent be based on the active carbon made by natural pond slag, add sludge carbon material, liquid paraffin and bicarbonate mixture, sodium bentonite that Ludox, mass ratio are 1 ﹕ 5, mediation forms.
The preparation method of described natural pond slag active carbon is: the natural pond slag after methane-generating pit fermentation, through cleaning, filtration, removal of impurities, soaks through liquor zinci chloridi, then embathes by deionized water, equal extrusion dehydration after above-mentioned every step; Then dry or dry, microwave irradiation carbonizes, and naturally after cooling, dries efflorescence, obtain described natural pond slag active carbon after rinsed with deionized water.
The preparation method of described sludge carbon material is: marsh gas fermentation pool mud drains through screening precipitation, and liquor zinci chloridi soaks, and drains post-drying, and microwave irradiation carbonizes, and the post-drying of rinsed with deionized water, efflorescence, obtains described sludge carbon material.
Embodiment 2:
By the fluidized bed furnace by roasting pyrite out containing the furnace gas of sulfur dioxide through high-temperature residual heat boiler recovery waste heat, middle temperature cooling, purifying after cyclone dust removal and electric precipitation and low temperature cooling, purifying, dedusting and except sulfur trioxide, drying with lower the temperature, now, furnace gas temperature is 40 DEG C, be 7%, CO containing sulfur dioxide
2and O
2content lower than 1%, N
2be 92%; Filter for refined sulfuric acid furnace gas again through 200 order polytetrafluoroethylene (PTFE) materials removes the grit and iron rust, smart minor amount of water, the O taken off in tank absorption removing mixing furnace gas carried secretly in gaseous mixture
2and CO
2, now, the water content in mixing furnace gas is reduced to 3.2mg/kg, and the content that the content of sulfur dioxide is about 7.5%, N2 is about 92.5%; Then the compression of band frequency converter compressor, exhaust pressure with frequency converter compressor is 0.55MPa, and delivery temperature is normal temperature about 41 DEG C, enters the adsorbent bed of adsorption tower at the bottom of adsorption tower, adsorbent sulfur dioxide, realizes being separated of nitrogen and sulfur dioxide.By the sulfur dioxide depressurization desorption adsorbed in adsorbent, extracted by the vavuum pump of frequency converter, enter surge tank, again high-concentration sulfur dioxide pressurization or freezing are obtained liquid sulfur dioxide, gas-liquid mixed gas containing liquid sulfur dioxide and gaseous sulfur dioxide enters gas-liquid separator and carries out gas-liquid separation, sulfur dioxide after separation is drained in steel cylinder to be collected, and the purity of liquid sulfur dioxide is 99.5%.Adsorbent obtains holomorphosis simultaneously.After vacuumizing, then be 0.50MPa with ejecting purity is 99.8%, pressure is 0.53MPa nitrogen from adsorption tower to the adsorbent bed reverse adsorptive pressure that boosts to, adsorbent bed just beginning enters next sorption cycle process.Be not liquefied a small amount of SO be separated
2circulation enters band frequency converter compressor again, and carry out compressing, cool and the cyclic process of gas-liquid separation, liquid sulfur dioxide wherein is constantly separated, and bottling confession is industrial.Be 99.8% enter surge tank by tower top N2 purity out, bottling, for industrial.
All the other are with embodiment 1.
Claims (7)
1. the nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide, is characterized in that processing step is as follows:
(1) by temperature purification and low temperature purification during the fluidized bed furnace furnace gas containing sulfur dioxide out of roasting pyrite is after the waste heat recovery cooling of high-temperature residual heat boiler, cyclone dust removal and electric precipitation, dedusting, except sulfur trioxide, drying and cooling, now, furnace gas temperature is 35 DEG C ~ 40 DEG C, be 7% ~ 12%, CO containing sulfur dioxide
2and O
2content lower than 1%, N
2be 87% ~ 92%;
(2) furnace gas after step (1) purge drying removes the grit and iron rust carried secretly in furnace gas again through the filter for refined sulfuric acid furnace gas of polytetrafluoroethylene (PTFE) material;
(3) step (2) gained furnace gas takes off water, the O of the trace in the adsorbent removing furnace gas of tank by the essence of loading combination carbon molecular sieve
2and CO
2, now, the water content in furnace gas is reduced to 2.1mg/kg ~ 3.2mg/kg, and the content of sulfur dioxide is 7.5% ~ 12.5%, N
2content be 87.5% ~ 92.5%;
(4) step (3) gained furnace gas enters surge tank, through the compression of band frequency converter compressor, at the bottom of adsorption tower, enters adsorption tower, and the sulfur dioxide in furnace gas, by the adsorbent on adsorbent bed, realizes nitrogen and is separated with sulfur dioxide; By the sulfur dioxide that adsorbs after depressurization desorption, extracted by vavuum pump and send into surge tank, obtain liquid sulfur dioxide with pressurization or freezing; Gas-liquid mixture containing liquid sulfur dioxide and gaseous sulfur dioxide enters gas-liquid separator and carries out gas-liquid separation, and gained liquid sulfur dioxide is drained in steel cylinder to be collected stand-by, and its purity is 98.6% ~ 99.5%; Adsorbent obtains holomorphosis simultaneously; Adsorbent bed be evacuated after, be 0.10MPa ~ 0.50MPa with ejecting purity is 98.5% ~ 99.8%, pressure is 0.11MPa ~ 0.53MPa nitrogen from adsorption tower to the adsorbent bed reverse adsorptive pressure that boosts to again, adsorbent bed just beginning enters next sorption cycle process;
(5) be not liquefied a small amount of SO be separated
2circulation carry out step (4) compressed or cool, gas-liquid separation, sulfur dioxide wherein is constantly separated;
(6) be 98.5% ~ 99.8% by adsorption tower tower top nitrogen gas purity out, enter surge tank, then it be stand-by to bottle.
2. the nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas as claimed in claim 1 and the method for sulfur dioxide, it is characterized in that, in described step (2), filter for refined sulfuric acid furnace gas is 200 orders.
3. the nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas as claimed in claim 1 and the method for sulfur dioxide, it is characterized in that the composition that the middle essence of loading combination carbon molecular sieve of described step (3) takes off the adsorbent of tank is: from the bottom up, the silochrom of the bottom to be quality be adsorbent mass 30% ~ 40%, the Kiselgel A of the second layer to be quality be adsorbent mass 20% ~ 30%, the sodium bentonite of third layer to be quality be adsorbent mass 10% ~ 20%, 4th layer is quality is adsorbent mass 5% ~ 10%13X molecular sieve, the carbon molecular sieve of the superiors' to be quality be adsorbent mass 15% ~ 20%, the mass percent summation of above-mentioned each component is 100%.
4. the nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas as claimed in claim 1 and the method for sulfur dioxide, it is characterized in that the pressure at expulsion being with frequency converter compressor in described step (4) is 0.13MPa ~ 0.55MPa, delivery temperature is 35 DEG C ~ 41 DEG C.
5. the nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas as claimed in claim 1 and the method for sulfur dioxide, it is characterized in that adsorbent described in described step (4) is based on the active carbon made by natural pond slag, add multiple Compound Supplement, its each component and mass percent as follows:
The mass percent summation of each component is 100% above.
6. the nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas as claimed in claim 5 and the method for sulfur dioxide, it is characterized in that described natural pond slag active carbon with natural pond slag for raw material, its preparation method is: carry out extrusion dehydration with the natural pond slag after methane-generating pit fermentation through cleaning, filtration, removal of impurities and screw extruder or three roller extruders, make its moisture content be 8% ~ 10%; Again through mass ratio be 10%-20%, temperature be 30 DEG C ~ 40 DEG C liquor zinci chloridi soak 35 ~ 40 hours; Through screw extruder or three roller extruder extrusion dehydrations, dry or dry, making its moisture content be 5% ~ 10%; Gained natural pond slag is placed on the microwave irradiation being 2000W ~ 3000W through irradiation power in the crucible of porcelain or carborundum and carbonizes, exposure time is 20 minutes ~ 30 minutes, naturally after cooling, dry 25 hours with after 30 DEG C ~ 40 DEG C rinsed with deionized water again, efflorescence is 200 ~ 400 order attritive powders again, obtains described natural pond slag active carbon.
7. the nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas as claimed in claim 5 and the method for sulfur dioxide, it is characterized in that, described methane tank sludge carbonized material with marsh gas fermentation pool mud for raw material, its preparation method is: marsh gas fermentation pool mud is after screening precipitation drains, adding mass concentration is 10%-20%, temperature is that the liquor zinci chloridi of 30 DEG C ~ 40 DEG C soaks 20 hours, drain rear baking 24h, be placed on the microwave irradiation being 2000W ~ 3000W through irradiation power in the crucible of porcelain or carborundum to carbonize, exposure time is 10 minutes ~ 20 minutes, dry 25 hours with after 30 DEG C ~ 40 DEG C rinsed with deionized water again, efflorescence becomes 200 ~ 400 order attritive powders, obtain described methane tank sludge carbonized material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410160445.6A CN103920365B (en) | 2014-04-21 | 2014-04-21 | Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410160445.6A CN103920365B (en) | 2014-04-21 | 2014-04-21 | Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103920365A CN103920365A (en) | 2014-07-16 |
| CN103920365B true CN103920365B (en) | 2016-01-27 |
Family
ID=51138899
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410160445.6A Expired - Fee Related CN103920365B (en) | 2014-04-21 | 2014-04-21 | Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103920365B (en) |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106139814A (en) * | 2015-03-26 | 2016-11-23 | 四川瑞城实业有限公司 | A kind of method removing sulfur dioxide in tail gas |
| CN105251313A (en) * | 2015-11-20 | 2016-01-20 | 苏州韵蓝环保科技有限公司 | Adsorption device for sulfur dioxide |
| CN105597488B (en) * | 2015-12-25 | 2019-01-15 | 杨皓 | A method of nitrogen and rich sour gas are produced from flue gas using pressure swing adsorption technique |
| CN105413394B (en) * | 2015-12-25 | 2019-01-15 | 杨皓 | A method of combined using pressure swing adsorption technique from flue gas and produces sour gas and purity nitrogen |
| CN107191357A (en) * | 2016-03-15 | 2017-09-22 | 哈尔滨宏万智科技开发有限公司 | A kind of air compressor machine cooling and dedusting system |
| CN105752943B (en) * | 2016-04-07 | 2019-05-07 | 北京清新环境技术股份有限公司 | A kind of richness SO2Condensation cleaning prepares liquid sulfur dioxide device to vapor step by step |
| CN108380001B (en) * | 2018-05-09 | 2023-11-21 | 安徽实华工程技术股份有限公司 | Storage tank area protection nitrogen recycling system and method |
| CN111375270B (en) * | 2018-12-31 | 2022-03-08 | 中国石油化工股份有限公司 | Containing SO2Flue gas treatment method and device |
| CN111375273B (en) * | 2018-12-31 | 2022-05-03 | 中国石油化工股份有限公司 | Treatment method and device for sulfur dioxide-containing waste gas |
| CN109813055B (en) * | 2019-01-15 | 2020-04-10 | 北京科技大学 | Method and device for rectifying and recovering NO2 and SO2 in flue gas |
| CN110342476B (en) * | 2019-05-28 | 2021-08-06 | 苏州海宇分离技术有限公司 | Pressure swing adsorption nitrogen making device |
| CN112742160A (en) * | 2019-10-31 | 2021-05-04 | 中国石油化工股份有限公司 | Containing SO2Method and apparatus for treating exhaust gas |
| CN111085082B (en) * | 2019-12-31 | 2021-10-15 | 江苏大东新材料科技有限公司 | Waste gas treatment device |
| CN113562702B (en) * | 2021-08-25 | 2022-11-01 | 福建福豆新材料有限公司 | Method for purifying high-purity electronic-grade sulfur dioxide |
| CN115340072B (en) * | 2022-09-14 | 2024-01-26 | 江西洪安化工有限公司 | Sulfur dioxide gas preparation system and method |
| CN115970441B (en) * | 2022-11-02 | 2023-06-13 | 原初科技（北京）有限公司 | Carbon dioxide absorbing furnace and using method thereof |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6402813B2 (en) * | 2000-01-25 | 2002-06-11 | L'AIR LIQUIDE, SOCIETE ANONYME A DIRECTOIRE éT CONSEIL DE SURVEILLANCE POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE | Process for purifying a gas by adsorption of the impurities on several active carbons |
| WO2006112977A2 (en) * | 2005-04-19 | 2006-10-26 | Knaebel Kent S | Temperature swing adsorption system |
| CN101417200A (en) * | 2007-10-22 | 2009-04-29 | 辽河石油勘探局 | Carbon dioxide, nitrogen gas recovering method in boiler flue gas |
| CN101837231A (en) * | 2010-04-23 | 2010-09-22 | 北京工业大学 | Sludge-based desulfurizer and preparation method thereof |
| CN102351156A (en) * | 2011-07-28 | 2012-02-15 | 湖南科技大学 | Sulfuric acid plant production device without discharge of tail gas and process method therefor |
| CN202343084U (en) * | 2011-11-15 | 2012-07-25 | 荆门市熊兴化工有限公司 | Sulfurous iron ore acid making production line with tail gas recycling device |
| CN102872677A (en) * | 2012-09-24 | 2013-01-16 | 广西大学 | Method for frequency-variable pressure-variable adsorption purification enrichment of carbon dioxide in sugar refinery flue gas |
-
2014
- 2014-04-21 CN CN201410160445.6A patent/CN103920365B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6402813B2 (en) * | 2000-01-25 | 2002-06-11 | L'AIR LIQUIDE, SOCIETE ANONYME A DIRECTOIRE éT CONSEIL DE SURVEILLANCE POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE | Process for purifying a gas by adsorption of the impurities on several active carbons |
| WO2006112977A2 (en) * | 2005-04-19 | 2006-10-26 | Knaebel Kent S | Temperature swing adsorption system |
| CN101417200A (en) * | 2007-10-22 | 2009-04-29 | 辽河石油勘探局 | Carbon dioxide, nitrogen gas recovering method in boiler flue gas |
| CN101837231A (en) * | 2010-04-23 | 2010-09-22 | 北京工业大学 | Sludge-based desulfurizer and preparation method thereof |
| CN102351156A (en) * | 2011-07-28 | 2012-02-15 | 湖南科技大学 | Sulfuric acid plant production device without discharge of tail gas and process method therefor |
| CN202343084U (en) * | 2011-11-15 | 2012-07-25 | 荆门市熊兴化工有限公司 | Sulfurous iron ore acid making production line with tail gas recycling device |
| CN102872677A (en) * | 2012-09-24 | 2013-01-16 | 广西大学 | Method for frequency-variable pressure-variable adsorption purification enrichment of carbon dioxide in sugar refinery flue gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103920365A (en) | 2014-07-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103920365B (en) | Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide | |
| CN101596391B (en) | Method for pressure swing adsorption and staged concentration of low concentration gas | |
| CN104087354B (en) | A kind of technique utilizing yellow phosphoric tail gas synthetic natural gas | |
| CN101643209A (en) | Method for purifying and reclaiming carbon dioxide from landfill gas and device thereof | |
| SE2350521A1 (en) | System and method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and psa method | |
| AU2009254260A1 (en) | Method and system for purifying biogas for extracting methane | |
| CN107285279B (en) | A method of purified synthesis gas using Quan Wencheng pressure-variable adsorption with separate | |
| CN110683544A (en) | Method for improving concentration of carbon dioxide in tail gas of lime rotary kiln | |
| CN102190541A (en) | Method for recovering methane for industrial production of clean fuel through deep purification of landfill gas | |
| CN201168557Y (en) | Flue gas processing system | |
| CN111375271B (en) | Method and device for treating flue gas containing sulfur dioxide | |
| CN105413429A (en) | Method for separating and purifying lime kiln tail gas | |
| CN111375273B (en) | Treatment method and device for sulfur dioxide-containing waste gas | |
| KR20160013686A (en) | Biogas pretreatment apparatus | |
| CN104556035A (en) | Preparation method and preparation device of food-grade high-purity liquid carbon dioxide | |
| CN111375270B (en) | Containing SO2Flue gas treatment method and device | |
| CN210332252U (en) | To CO in cement kiln tail flue gas2Trapping, concentrating and utilizing system | |
| CN102441309A (en) | Method for recovering oil gas and device | |
| CN111375274B (en) | Containing SO 2 Gas treatment method and apparatus | |
| CN103949213B (en) | A kind of absorbent charcoal based adsorbent composition for reclaiming sulfur dioxide and nitrogen in roasting pyrite furnace gas | |
| CN101015761A (en) | Pressure-swing-adsorption purging regeneration method without using vacuum pump | |
| CN105779047A (en) | Technology and system for making flue gas into liquified natural gas | |
| CN101948707A (en) | Purification device for oxygen-containing coal bed methane | |
| CN106811251A (en) | The small-sized methane purification technique that a kind of pressure and temperature varying absorption is combined | |
| CN102516028B (en) | Method for preparing methanol and dimethyl ether by taking calcium carbide furnace tail gas and sodium chlorate tail gas as well as other hydrogen-containing gas sources as raw materials |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160127 |