CN106669360A - Method and apparatus for flue gas desulfurization and sulfuric acid production - Google Patents
Method and apparatus for flue gas desulfurization and sulfuric acid production Download PDFInfo
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- CN106669360A CN106669360A CN201510740288.0A CN201510740288A CN106669360A CN 106669360 A CN106669360 A CN 106669360A CN 201510740288 A CN201510740288 A CN 201510740288A CN 106669360 A CN106669360 A CN 106669360A
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- liquid
- flue gas
- sulfuric acid
- desulfurization
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 152
- 239000003546 flue gas Substances 0.000 title claims abstract description 79
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 74
- 230000023556 desulfurization Effects 0.000 title claims abstract description 72
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 238000000034 method Methods 0.000 title claims abstract description 48
- 238000004519 manufacturing process Methods 0.000 title abstract description 6
- 239000007788 liquid Substances 0.000 claims abstract description 109
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 46
- 239000007791 liquid phase Substances 0.000 claims abstract description 44
- 230000003647 oxidation Effects 0.000 claims abstract description 43
- 239000000428 dust Substances 0.000 claims abstract description 37
- 239000007789 gas Substances 0.000 claims abstract description 31
- 238000003860 storage Methods 0.000 claims abstract description 25
- 238000005406 washing Methods 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000013505 freshwater Substances 0.000 claims abstract description 13
- 238000010521 absorption reaction Methods 0.000 claims abstract description 12
- 239000012071 phase Substances 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 239000002910 solid waste Substances 0.000 claims abstract description 6
- 238000011084 recovery Methods 0.000 claims abstract description 4
- 238000011069 regeneration method Methods 0.000 claims abstract description 4
- 101100341609 Drosophila melanogaster jing gene Proteins 0.000 claims description 50
- 230000003009 desulfurizing effect Effects 0.000 claims description 30
- 239000007921 spray Substances 0.000 claims description 17
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 16
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 239000003729 cation exchange resin Substances 0.000 claims description 8
- 230000002378 acidificating effect Effects 0.000 claims description 7
- 239000000945 filler Substances 0.000 claims description 7
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 239000002250 absorbent Substances 0.000 claims description 5
- 230000002745 absorbent Effects 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 239000003517 fume Substances 0.000 claims description 5
- 239000007800 oxidant agent Substances 0.000 claims description 5
- 239000003463 adsorbent Substances 0.000 claims description 4
- 238000004523 catalytic cracking Methods 0.000 claims description 4
- 239000003245 coal Substances 0.000 claims description 4
- 239000003456 ion exchange resin Substances 0.000 claims description 4
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 4
- 230000007420 reactivation Effects 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 238000010410 dusting Methods 0.000 claims description 2
- 239000007792 gaseous phase Substances 0.000 claims description 2
- 206010022000 influenza Diseases 0.000 claims description 2
- 238000005342 ion exchange Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 24
- 229910052815 sulfur oxide Inorganic materials 0.000 abstract description 9
- 238000001816 cooling Methods 0.000 abstract description 2
- 238000010791 quenching Methods 0.000 abstract 2
- 230000000171 quenching effect Effects 0.000 abstract 2
- 230000008929 regeneration Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 7
- 235000010269 sulphur dioxide Nutrition 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 239000005864 Sulphur Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000013589 supplement Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000005273 aeration Methods 0.000 description 4
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 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 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000001413 cellular effect Effects 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000012286 potassium permanganate Substances 0.000 description 2
- 238000004080 punching Methods 0.000 description 2
- 235000010265 sodium sulphite Nutrition 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229940023913 cation exchange resins Drugs 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000005056 compaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 229940079827 sodium hydrogen sulfite Drugs 0.000 description 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/14—Packed scrubbers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
- C01B17/76—Preparation by contact processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
- C01B17/76—Preparation by contact processes
- C01B17/80—Apparatus
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
- B01D2247/10—Means for removing the washing fluid dispersed in the gas or vapours
- B01D2247/107—Means for removing the washing fluid dispersed in the gas or vapours using an unstructured demister, e.g. a wire mesh demister
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
Abstract
The present invention discloses a method and an apparatus for flue gas desulfurization and sulfuric acid production. The method comprises that (1) flue gas is subjected to heat exchange through a sulfuric acid storage tank, and then the obtained flue gas enters a dust removing quenching tower and is subjected to primary dust removing cooling; (2) the cooled flue gas enters a desulfurization tower and sequentially passes through a deep dust removing unit, a desulfurization unit and a water washing unit from bottom to top; (3) in the water washing unit, the SOx in the flue gas is absorbed with fresh water, the liquid phase overflows and sequentially passes through the desulfurization unit and the deep dust removing unit, the obtained liquid phase enters the dust removing quenching tower to obtain a rich absorption liquid, solid-liquid separation is performed, and the gas phase is discharged in atmosphere after defogging; and (4) the rich absorption liquid being subjected to solid waste separation is discharged into an oxidation tank, the liquid phase enters a regeneration tower, the Fe<3+>/Fe<2+> in the liquid phase is removed, and the obtained liquid phase enters the sulfuric acid storage tank in the form of dilute sulfuric acid. With the method and the apparatus of the present invention, the SO2 in the flue gas can be absorbed and concentrated, and can be oxidized into the sulfuric acid so as to produce the high concentration sulfuric acid, the purified flue gas can meet the national or local relevant standard requirements, and the method and the apparatus are suitable for the recovery treatment of flue gas containing various concentrations of sulfur dioxide.
Description
Technical field
The invention belongs to environmental technology field, more particularly to a kind of flue gas desulfurization and the method and apparatus of sulfuric acid is produced.
Background technology
Since two thousand three, China SO2Total emission volumn remains high always, China SO in 201421974.4 ten thousand tons of total emission volumn, is less than first since two thousand three 20000000 tons.Although the target that China the Eleventh Five-Year Plan period cuts down sulfur dioxide 10% has been carried out, the current Acid Rain Pollution area of China（Account for the 30% of area）Still constantly expanding, and just from " sulfuric acid type " to " sulfonitric is compound " conversion.Every year because of acid rain and SO2Pollution causes the economic loss of the aspects such as crops, forest and health more than 100,000,000,000 yuan, and sulfur dioxide (SO2) emissions control still can not be ignored.Fume desulphurization method can be divided into two kinds of dry and wet, and compared with dry desulfurization, wet desulphurization equipment is little, simple to operate, and desulfuration efficiency is high, and at present, the Wet Flue Gas Desulfurization Technique of application includes sodium method, magnesium processes, ammonia process and calcium method etc., wherein most with sodium method and calcium method.Whether wet desulphurization can also useful according to product, is divided into the method for abandoning and absorption method, and absorption method enjoys the concern of people because of its economic factor.Now widely used absorption method is limestone-gypsum method, but the added value of accessory substance-gypsum is relatively low, and drug on the market, while limestone-gypsum method easily causes equipment or pipeline scale and blocking, desulfurizer operation is cumbersome, and on-site sanitation situation is also poor.To abandon method, the sulphite in desulfurization wastewater shows as COD to the desulfurization of sodium method（COD）, typically>8000mg/L, therefore, be ensure desulfurization wastewater can qualified discharge, build flue gas desulfurization device when, it is necessary to while build desulfurization wastewater oxidation treatment device.Due to sodium sulfite oxidation rate it is slower, it usually needs 5～8h, investment, take up an area and operating cost is higher, such as patent US4627965A and US5928615A.In addition, abandon method a large amount of Sulphur ressources are wasted.Though the Sulphur ressource in ammonia process of desulfurization energy recovered flue gas, product ammonium sulfate can make soil compaction, be rarely employed, and the heavy metal ion in flue gas is also fully entered in ammonium sulfate product, and secondary pollution, and and then harm human body health are caused to soil.
CN1265934A is with intermetallic composite coating discarded object iron filings or aluminium skimmings as desulfurizing agent, acid and reactive desulfurizing agent generation ferrous sulfate or aluminum sulfate that the sulfur dioxide in flue gas is produced are absorbed using water, afterwards Jing air oxidations are obtained poly-ferric chloride or polyaluminium sulfate in oxidizing tower.Sulphur ressource of the technology in recovered flue gas in the form of flocculant, but the dust in flue gas is equally brought into flocculant, affects the using effect of flocculant.
CN1391975A absorbs the sulfur dioxide in flue gas using the NaOH that electrolytic saltwater is produced, hydrochloric acid is generated using the chlorine and hydrogen reaction produced in electrolytic process, the sulfur dioxide for producing high concentration is reacted with the sodium sulfite in desulfurization wastewater/sodium hydrogensulfite, it is achieved thereby that the concentration and recycling of sulfur dioxide.The technology chlorine is toxic gas, and hydrogen reacts and produces the process of hydrochloric acid and needs to take effectively anti-corrosion and containment measures, and to operation and equipment/pipe material higher technical requirements are proposed.
CN200810012741.6 is with the SO in ozone oxidation flue gas2And NOx, mix acid liquor is collected into Jing after charged coalescence, most after Jing fractionation concentrate sulfuric acid and nitric acid.The technology ozone consumption and electrisity consumption are big, and operating cost is higher, and sulfuric acid belongs to strong acid with nitric acid, it is more difficult to separate.
The content of the invention
For the deficiencies in the prior art, the present invention proposes a kind of flue gas desulfurization and produces the method and apparatus of sulfuric acid, and the inventive method and device can be by the SO in flue gas2Absorb concentration, and it is oxidized be converted into sulfuric acid, so as to produce the sulfuric acid solution of higher concentration, purifying smoke can meet country or local correlation standard is required, it is adaptable to which the off-gas recovery containing various concentration sulfur dioxides is processed.
The flue gas desulfurization of the present invention and the method for producing sulfuric acid, including following content：
（1）Flue gas is contacted into dedusting chilling tower Jing after sulfuric acid storage tank heat exchange with absorbing liquid, carries out rough dusting temperature-fall period, removes most of dust and part SO in flue gas2；
（2）Step（1）The flue gas Jing for obtaining connects flue and sequentially passes through depth dust removing units, desulfurization unit, washing unit from the bottom to top into desulfurizing tower；Wherein the remaining fine dust in flue gas is trapped to desulfurization tower bottom and held in the absorbing liquid of liquid bath by depth dust removing units；Desulfurization unit passes through the gas-liquid mass transfer desulfidation of absorbing liquid and flue gas, further by the SO in flue gas2Absorb and be transferred to liquid phase；
（3）In washing unit, the SO in flue gas is absorbed by fresh waterxLiquid phase overflow passes sequentially through desulfurization unit, depth dust removing units, then rich absorbing liquid is obtained into dedusting chilling tower by overflow Jing flues, rich absorbing liquid carries out separation of solid and liquid by dedusting chilling tower into solid-liquid separator, and gas phase enters air Jing after demister unit removes droplet；
（4）The rich absorbing liquid for isolating solid waste enters oxidation tank, while adding ferrum sulfuricum oxydatum solutum, and air is passed through as oxidant, by the H in rich absorbing liquid2SO3Oxidation is converted into H2SO4, the liquid phase after oxidation enters regenerator；
（5）Regenerator, by ion exchange, removes the Fe in liquid phase built with hydro-strong acidic cation exchange resin3+/Fe2+, sulfuric acid storage tank is entered in the form of dilute sulfuric acid.
In the inventive method, described flue gas is fire coal boiler fume, catalytic cracking catalyst regenerated flue gas, Furnace flue gas, S-zorb adsorbent reactivation flue gases etc., wherein SO2100 ~ 150000mg/Nm of concentration3。
In the inventive method, described absorbing liquid is water, and fresh water is supplemented by desulfurization tower top washing unit；The concentration of described ferrum sulfuricum oxydatum solutum is 0.1wt%～20wt%.
Step（1）The tube bank of DN25～DN500 flue gas heat exchanges is provided with described sulfuric acid storage tank, flue gas can partly or entirely flow through heat-exchanging tube bundle, water vapour is incorporated to flue, it is concentrated after obtain sulfuric acid as product, 30～80 DEG C of temperature.
Step（1）Described dedusting chilling tower can be from one or more in venturi scrubber, Tuan Chong, packed tower or spray column, absorbing liquid from the liquid bath of holding of dedusting chilling tower bottom, by desulfurization tower bottom hold liquid bath overflow and supplemented by the absorbing liquid held in liquid bath of dedusting chilling tower bottom.The ratio of absorbing liquid and flue gas is 1：1～30：1, L：m3。
Step（2）Described depth dust removing units are filled with filler, theoretical cam curve is 2～15 pieces, the remaining fine dust in flue gas is all trapped to desulfurization tower bottom by the effect of impact and filling batch of filler to the filtration crown_interception of dust using dust in flue gas is held in the absorbing liquid of liquid bath.Depth dust removing units liquid-gas ratio 3：1～300：1, L：m3, preferably 5：1～10：1, L：m3。
Step（2）Desulfurization unit is followed successively by from the bottom to top firsts and seconds circulation desulfurization in described desulfurizing tower, may also set up three-level or multiple stage circulation desulfurization, it is provided with per one-level circulation desulfurization and independent holds liquid bath, as shown in Figure 2, absorbing liquid comes from respective holds liquid bath, at different levels to hold liquid baths by overflow pipe, downflow weir, anti-pouring cap and absorb nozzle for liquid etc. and constitute, circulation desulfurizations at different levels are held and have between liquid bath overflow pipe and connect, and flue gas desulfurization liquid-gas ratios at different levels are 1：1～300：1, L：m3, preferably 5：1～10：1, L：m3。
Step（2）In described desulfurizing tower in desulfurization unit, constituted by film mass transfer and spray mass transfer per first grade desulfurizing：Through liquid film, primary cycle spray liquid, the liquid film of secondary cycle spray liquid overflow generation and secondary cycle spray liquid that the flue gas of depth dedusting is produced successively with the overflow of primary cycle spray liquid, gas-liquid mass transfer desulfidation is completed, by the SO in flue gas2Absorb and be transferred to liquid phase.
Step（3）The liquid-gas ratio of described washing unit is 0.5：1～10：1, L：m3, filler can be loaded or directly gas-liquid mass transfer is carried out in spray form, preferred spray.
Step（3）Described solid-liquid separator be sedimentation basin, ceramic capillary filter, plate and frame filter press, vacuum filter or its combination, preferably ceramic millipore filter.
Step（3）Described demisting unit can be fiber mist eliminator, material filling type demister or mesh mist eliminator.
Step（4）Air addition is liquid phase in oxidation tank（Volume）3～10 times of amount, can also add KMnO4、O3, pure oxygen, H2O2Or Cl2Deng as cooxidant.
Step（5）In described regenerator after ion exchange resin adsorption saturation, the sulfuric acid in sulfuric acid storage tank is delivered to into regenerator, makes ion exchange resin activity recovery, the Fe after regeneration2(SO4)3Solution returns oxidation tank and recycles.Regenerator a preparation and a use, the two handover operation.
Present invention simultaneously provides a kind of flue gas desulfurization and the device of sulfuric acid is produced, including：Dedusting chilling tower（3）, desulfurizing tower（5）, connection flue（4）, regenerator（21A/B）, solid-liquid separator（10）, sulfuric acid storage tank（26）, heat-exchanging tube bundle（27）, oxidation tank（13）；Sulfuric acid storage tank（26）Heat-exchanging tube bundle（27）Jing pipelines connect dedusting chilling tower（3）Top, dedusting chilling tower（3）And desulfurizing tower（5）Between connecting flue（4）Connection, desulfurizing tower（5）Gaseous phase outlet connects air；Chilling water pump（2）Entrance Jing pipelines connect from dedusting chilling tower（3）Liquid bath is held at bottom, and outlet Jing pipelines are connected respectively to dedusting chilling tower（2）Circulating absorption solution entrance and solid-liquid separator（10）；Rich absorbing liquid pump（12）Entrance Jing pipelines and solid-liquid separator（10）Liquid-phase outlet is connected, and exports Jing pipelines and oxidation tank（13）Liquid phase entrance connects；Dilute sulfuric acid pump（14）Entrance Jing pipelines and oxidation tank（13）Liquid-phase outlet is connected, and exports Jing pipelines and regenerator（21A/B）Connection；Regenerator（21A/B）Liquid-phase outlet Jing pipelines respectively with sulfuric acid storage tank（26）And oxidation tank（13）It is connected；Sulfuric acid pump（24）Entrance Jing pipelines and sulfuric acid storage tank（26）It is connected, exports Jing pipelines and regenerator（21A/B）Regenerable absorbent liquid entrance is connected；Air blast（16）Outlet Jing pipelines are connected with oxidation tank gas phase mouth；Oxidation tank（13）Gas phase（31）Outlet and sulfuric acid storage tank gas phase（28）Outlet Jing pipelines are connected with flue；Depth dedusting slurries pump（6）Entrance Jing pipelines are held liquid bath liquid-phase outlet and are connected with desulfurizing tower bottom, export Jing pipelines and depth dust removing units（5-1）Spray liquid entrance connects；Desulfurization unit primary cycle pump（29）Liquid phase entrance Jing pipelines are held liquid bath and are connected with primary cycle desulfurization, and outlet Jing pipelines are connected with primary cycle desulphurization circulating absorbing liquid entrance；Desulfurization unit secondary cycle pump（30）Liquid phase entrance Jing pipelines are held liquid bath and are connected with secondary cycle desulfurization, and outlet Jing pipelines are connected with secondary cycle desulphurization circulating absorbing liquid entrance.
Compared with prior art, the invention has the advantages that：
（1）Absorbing liquid is water in dedusting chilling tower and desulfurizing tower, and fresh water then all by desulfurization tower top washing unit supplement, makes water be not fully exerted the strong absorption of SOx, and remnants SOx are all transferred to liquid phase in flue gas, and SOx can be reduced to 80mg/Nm in purifying smoke3Below.
（2）With Fe3+/Fe2+For catalyst, with air to concentration after containing H2SO3Acid water carries out oxidation processes, is aided with H2O2For oxidant, oxidant and catalyst utilization are higher.
（3）SO in flue gas2Sulfuric acid is converted to, without first making sulphur, then extracting sulfuric acid, is saved from SO2Production sulphur arrives again the plant investment expense of production sulfuric acid and storage freight, hydro-strong acidic cation exchange resin absorption Fe3+/Fe2+After saturation, resin is regenerated using byproduct sulfuric acid, realize gathering materials on the spot.
（4）One-level and secondary cycle desulfurization be provided with it is respective hold liquid bath, for processing the flue gas containing difference SOx concentration, realize classification process, desulfuration efficiency is higher.After processed by the invention, gained sulfuric acid product concentration can reach 60%～80%.
（5）Desulfurizing tower is at different levels to be held by overflow pipe UNICOM between liquid bath, and liquid phase produces liquid film in flooding process, and gas phase is flowed up, and is capable of achieving one-level spray, two-stage and is absorbed, and then increases gas-liquid mass transfer effect.
（6）Dedusting chilling tower and depth dust removing units are respectively used to remove the dust and fine dust of greater particle size in flue gas, dedusting chilling tower and depth dust removing units are provided with independent holds liquid bath, both are overflow UNICOM, it is to avoid slurry plugs packed tower containing a large amount of suspensions.
（7）The present invention also can select iron chloride when being oxidation catalyst, now will return boiler with gas phase after the oxidized tank aeration of the hydrogen chloride in solution and heat exchanger tube heating, without the need for arranging special cleaning equipment, reduce the purity of investment and guarantee sulfuric acid.
Description of the drawings
Fig. 1 is flue gas desulfurization of the present invention and produces the method and apparatus flow chart of sulfuric acid.
Fig. 2 is that liquid bath schematic diagram is held in desulfurizing tower desulfurization unit one-level/secondary cycle desulfurization.
Wherein：1st, flue gas；2nd, chilling water pump；3rd, dedusting chilling tower；4th, flue is connected；5th, desulfurizing tower；6th, depth dedusting slurries pump；7th, fresh water；8th, purifying smoke；9th, rich absorbing liquid；10th, solid-liquid separation unit；11st, solid waste；12nd, rich absorbing liquid pump；13rd, oxidation tank；14th, dilute sulfuric acid pump；15th, oxidation/catalyst；16th, air blast；17A/B, 18A/B, 19A/B, 20A/B, switch valve；21A/B, regenerator；22nd, the Fe after regenerating2(SO4)3Solution；23rd, dilute sulfuric acid；24th, sulfuric acid pump；25th, sulfuric acid product；26th, sulfuric acid storage tank；27th, heat exchanger tube（Flue gas）；28th, water vapour；29th, primary cycle pump；30th, secondary cycle pump；31st, air.
Desulfurizing tower 5 is followed successively by from the bottom to top：5-1, depth dedusting；5-2, primary cycle desulfurization；5-3, secondary cycle desulfurization；5-4, washing；5-5, demister.
One-level/secondary cycle desulfurization and washing unit are held liquid bath and are included：A, overflow pipe（Or gas/liquid phase passage）；B, liquid phase downflow weir；C, absorbing liquid；D, nozzle；E, anti-pouring cap.
Specific embodiment
The inventive method and device are described in more detail below by specific embodiment, but and are not so limited the present invention.
The flue gas desulfurization of the present invention and method for producing sulfuric acid is to carry out as follows：Flue gas（1）Jing sulfuric acid storage tanks（26）The heat-exchanging tube bundle of setting（27）Into dedusting chilling tower（3）With chilling water pump（2）The chilled water (chw) heat exchange cooling for coming, and realize after pre- desulfurization and the most dust of trapping, by connecting flue（4）Into desulfurizing tower（5）, Jing depth dust removing units successively（5-1）, primary cycle desulfurization（5-2）, secondary cycle desulfurization（5-3）Afterwards, into washing module（5-4）, with fresh water（7）Contact mass transfer, remnants SOx in removing flue gas, by demister（5-5）Air, washing module are entered after droplet in removing flue gas（5-4）The liquid phase of overflow is successively washing unit（5-4）, secondary cycle desulfurization（5-3）, primary cycle desulfurization（5-2）With depth dust removing units（5-1）, then overflow is to dedusting chilling tower（3）Liquid bath is held in bottom, forms rich absorbing liquid（9）, rich absorbing liquid（9）By chilling water pump（2）Enter solid-liquid separation unit（10）, after isolating solid waste, by rich absorbing liquid pump（12）Enter oxidation tank（13）.To oxidation tank（13）Interior addition ferrum sulfuricum oxydatum solutum（15）, and air is blasted, by H2SO3Oxidation is converted into H2SO4.By dilute sulfuric acid pump（14）Discharge unit contains Fe3+Dilute sulfuric acid passes through regenerator（21A/B）, remove the Fe in solution3+Dilute sulfuric acid afterwards（23）Enter sulfuric acid storage tank（26）.In sulfuric acid storage tank（26）Liquid phase region is provided with heat-exchanging tube bundle（27）, flue gas 1 is partly or entirely through heat-exchanging tube bundle（27）Dilute sulfuric acid is evaporated after concentration and water vapour（28）And air（31）Together enter dedusting chilling tower（3）, the sulfuric acid Jing sulfuric acid pumps after concentration（24）As sulfuric acid product（25）Outward transport.
Work as regenerator（21A/B）After interior hydro-strong acidic cation exchange resin adsorption saturation, valve 18A, 20A, 17B, 19B are closed, open valve 18B, 20B, 17A, 19A, the Fe after regeneration2(SO4)3Solution（22）Return oxidation tank（13）Recycle.Supplement fresh water（7）It is connected to washing module（5-4）, sequentially enter by overflow（5-3）、（5-2）、（5-1）With dedusting chilling tower（3）Hold liquid bath in bottom.
It is to ensure H in liquid phase in the present invention2SO3Or deliquescent SO2All oxidations are converted into H2SO4, also can add H in oxidation tank2O2、Cl2、KMnO4Or O3Deng oxidant.The property of the hydro-strong acidic cation exchange resin described in embodiment is as follows：0.3～1.2mm of particle diameter, mass exchange capacity >=4.80mmol/g, water content 50～70%, 1.10～1.30g/ml of wet true density.
Embodiment
1
：
Certain catalytic cracking catalyst regenerated flue gas composition is shown in Table 1.
Certain the catalytic cracking catalyst regenerated flue gas composition of table 1.
Operating condition of the present invention：（1）Dedusting chilling tower adopts venturi scrubber, liquid-gas ratio 3.0L/m3；（2）The built-in fillers of desulfurizing tower depth dust removing units 5-1, desulfurization unit is 2 grades, and using spray-absorption, liquid-gas ratio is 3.0L/m3；（3）To supplement fresh water, liquid-gas ratio is 5.0L/m to desulfurizing tower washing unit absorbent3；（4）Micro-pore aeration flexible pipe is disposed with oxidation tank, air is made and is scattered in liquid phase with cellular form, add air capacity to be liquid phase in oxidation tank（Volume）4 times of amount, while adding ferrum sulfuricum oxydatum solutum, wherein Fe in oxidation tank3+Mass concentration 3.0%；（5）Regenerator is two, handover operation, built-in commercially available D001 hydro-strong acidic cation exchange resins；（6）Heat exchanger exit sulfuric acid temperature 50 C.
After processed by the invention：SOx concentration 53mg/Nm in purified gas3, dust concentration 3mg/Nm3, sulfuric acid product concentration 60%.
Embodiment
2
：
Certain S zorb device adsorbent reactivations flue gas composition is shown in Table 2.
Certain the S-zorb device adsorbent reactivations flue gas composition of table 2.
Operating condition of the present invention：（1）Dedusting chilling tower is using rapid punching as mass transfer component, liquid-gas ratio 7.0L/m3；（2）The built-in fillers of desulfurizing tower depth dust removing units 5-1, desulfurization unit is 4 grades, and using spray-absorption, liquid-gas ratio is 5.0 L/m3；（3）To supplement fresh water, liquid-gas ratio is 3.0 to desulfurizing tower washing unit absorbent
L/m3；（4）Micro-pore aeration flexible pipe is disposed with oxidation tank, air is made and is scattered in liquid phase with cellular form, add air capacity to be liquid phase in oxidation tank（Volume）5 times of amount, while ferrum sulfuricum oxydatum solutum is added into oxidation tank, and cooxidant H2O2, wherein Fe3+Mass concentration 3.0%, H2O2Concentration 3.0%；（5）Regenerator is two, handover operation, built-in commercially available D003 types hydro-strong acidic cation exchange resin.
After processed by the invention：SOx concentration 65mg/Nm in purified gas3, dust do not detect, gained sulfuric acid concentration 85%.
Embodiment
3
：
Certain fire coal boiler fume composition is shown in Table 3.
Certain fire coal boiler fume composition of table 3.
Operating condition of the present invention：（1）Dedusting chilling tower is using rapid punching, the L/m of liquid-gas ratio 8.03；（2）The built-in fillers of desulfurizing tower depth dust removing units 5-1, desulfurization unit is 3 grades, and using spray-absorption, liquid-gas ratio is 3.0 L/m3；（3）To supplement fresh water, liquid-gas ratio is 5.0 to desulfurizing tower washing unit absorbent
L/m3；（4）Micro-pore aeration flexible pipe is disposed with oxidation tank, air is made and is scattered in liquid phase with cellular form, add air capacity to be liquid phase in oxidation tank（Volume）6 times of amount, while ferrum sulfuricum oxydatum solutum is added into oxidation tank, and cooxidant H2O2, wherein Fe3+Mass concentration 3.0%, H2O2Concentration 0.8%；（5）Regenerator is two, handover operation, built-in commercially available 732# hydrogen type strong acids styrene type cation exchange resin.
After processed by the invention：SOx concentration 52mg/Nm in purified gas3, gained sulfuric acid concentration 72%.
Claims (13)
1. a kind of flue gas desulfurization and the method that produces sulfuric acid, it is characterised in that including following content：（1）Flue gas is contacted into dedusting chilling tower Jing after sulfuric acid storage tank heat exchange with absorbing liquid, carries out rough dusting temperature-fall period, removes most of dust and part SO in flue gas2；（2）Step（1）The flue gas Jing for obtaining connects flue and sequentially passes through depth dust removing units, desulfurization unit, washing unit from the bottom to top into desulfurizing tower；Wherein the remaining fine dust in flue gas is trapped to desulfurization tower bottom and held in the absorbing liquid of liquid bath by depth dust removing units；Desulfurization unit passes through the gas-liquid mass transfer desulfidation of absorbing liquid and flue gas, further by the SO in flue gas2Absorb and be transferred to liquid phase；（3）In washing unit, the SO in flue gas is absorbed by fresh waterxLiquid phase overflow passes sequentially through desulfurization unit, depth dust removing units, then rich absorbing liquid is obtained into dedusting chilling tower by overflow Jing flues, rich absorbing liquid carries out separation of solid and liquid by dedusting chilling tower into solid-liquid separator, and gas phase enters air Jing after demister unit removes droplet；（4）The rich absorbing liquid for isolating solid waste enters oxidation tank, while adding ferrum sulfuricum oxydatum solutum, and air is passed through as oxidant, by the H in rich absorbing liquid2SO3Oxidation is converted into H2SO4, the liquid phase after oxidation enters regenerator；（5）Regenerator, by ion exchange, removes the Fe in liquid phase built with hydro-strong acidic cation exchange resin3+/Fe2+, sulfuric acid storage tank is entered in the form of dilute sulfuric acid.
2. in accordance with the method for claim 1, it is characterised in that：Described flue gas is one or more in fire coal boiler fume, catalytic cracking catalyst regenerated flue gas, Furnace flue gas, S-zorb adsorbent reactivation flue gases, wherein SO2100 ~ 150000mg/Nm of concentration3。
3. in accordance with the method for claim 1, it is characterised in that：Described absorbing liquid is water, and fresh water is supplemented by desulfurization tower top washing unit.
4. in accordance with the method for claim 1, it is characterised in that：Step（1）Be provided with the tube bank of DN25～DN500 flue gas heat exchanges in described sulfuric acid storage tank, flue gas partial or all flow through heat-exchanging tube bundle, water vapour is incorporated to flue, it is concentrated after obtain sulfuric acid as product.
5. in accordance with the method for claim 1, it is characterised in that：Step（1）Described dedusting chilling tower is from one or more in venturi scrubber, Tuan Chong, packed tower or spray column, absorbing liquid from the liquid bath of holding of dedusting chilling tower bottom, by desulfurization tower bottom hold liquid bath overflow and supplemented by the absorbing liquid held in liquid bath of dedusting chilling tower bottom；The ratio of absorbing liquid and flue gas is 1：1～30：1, L：m3。
6. in accordance with the method for claim 1, it is characterised in that：Step（2）Described depth dust removing units are filled with filler, and theoretical cam curve is 2～15 pieces；Depth dust removing units liquid-gas ratio 3：1～300：1, L：m3。
7. in accordance with the method for claim 1, it is characterised in that：Step（2）Desulfurization unit is followed successively by from the bottom to top firsts and seconds circulation desulfurization in described desulfurizing tower, is provided with per one-level circulation desulfurization and independent holds liquid bath；At different levels to hold liquid baths by overflow pipe, downflow weir, anti-pouring cap and absorb nozzle for liquid and constitute, circulation desulfurizations at different levels are held and have between liquid bath overflow pipe and connect, and flue gas desulfurization liquid-gas ratios at different levels are 1：1～300：1, L：m3。
8. in accordance with the method for claim 1, it is characterised in that：Step（2）In described desulfurizing tower in desulfurization unit, constituted by film mass transfer and spray mass transfer per first grade desulfurizing：Through liquid film, primary cycle spray liquid, the liquid film of secondary cycle spray liquid overflow generation and secondary cycle spray liquid that the flue gas of depth dedusting is produced successively with the overflow of primary cycle spray liquid, gas-liquid mass transfer desulfidation is completed, by the SO in flue gas2Absorb and be transferred to liquid phase.
9. in accordance with the method for claim 1, it is characterised in that：Step（3）The liquid-gas ratio of described washing unit is 0.5：1～10：1, L：m3。
10. in accordance with the method for claim 1, it is characterised in that：Step（4）The concentration of described ferrum sulfuricum oxydatum solutum is 0.1wt%～20wt%.
11. in accordance with the method for claim 1, it is characterised in that：Step（4）Air addition is 3～10 times of liquid phase volume amount in oxidation tank.
12. in accordance with the method for claim 1, it is characterised in that：Step（5）In described regenerator after ion exchange resin adsorption saturation, the sulfuric acid in sulfuric acid storage tank is delivered to into regenerator, makes ion exchange resin activity recovery, the Fe after regeneration2(SO4)3Solution returns oxidation tank and recycles.
A kind of 13. flue gas desulfurizations simultaneously produce the device of sulfuric acid, it is characterised in that include：Dedusting chilling tower（3）, desulfurizing tower（5）, connection flue（4）, regenerator（21A/B）, solid-liquid separator（10）, sulfuric acid storage tank（26）, heat-exchanging tube bundle（27）, oxidation tank（13）；Sulfuric acid storage tank（26）Heat-exchanging tube bundle（27）Jing pipelines connect dedusting chilling tower（3）Top, dedusting chilling tower（3）And desulfurizing tower（5）Between connecting flue（4）Connection, desulfurizing tower（5）Gaseous phase outlet connects air；Chilling water pump（2）Entrance Jing pipelines connect from dedusting chilling tower（3）Liquid bath is held at bottom, and outlet Jing pipelines are connected respectively to dedusting chilling tower（2）Circulating absorption solution entrance and solid-liquid separator（10）；Rich absorbing liquid pump（12）Entrance Jing pipelines and solid-liquid separator（10）Liquid-phase outlet is connected, and exports Jing pipelines and oxidation tank（13）Liquid phase entrance connects；Dilute sulfuric acid pump（14）Entrance Jing pipelines and oxidation tank（13）Liquid-phase outlet is connected, and exports Jing pipelines and regenerator（21A/B）Connection；Regenerator（21A/B）Liquid-phase outlet Jing pipelines respectively with sulfuric acid storage tank（26）And oxidation tank（13）It is connected；Sulfuric acid pump（24）Entrance Jing pipelines and sulfuric acid storage tank（26）It is connected, exports Jing pipelines and regenerator（21A/B）Regenerable absorbent liquid entrance is connected；Air blast（16）Outlet Jing pipelines are connected with oxidation tank gas phase mouth；Oxidation tank（13）Gas phase（31）Outlet and sulfuric acid storage tank gas phase（28）Outlet Jing pipelines are connected with flue；Depth dedusting slurries pump（6）Entrance Jing pipelines are held liquid bath liquid-phase outlet and are connected with desulfurizing tower bottom, export Jing pipelines and depth dust removing units（5-1）Spray liquid entrance connects；Desulfurization unit primary cycle pump（29）Liquid phase entrance Jing pipelines are held liquid bath and are connected with primary cycle desulfurization, and outlet Jing pipelines are connected with primary cycle desulphurization circulating absorbing liquid entrance；Desulfurization unit secondary cycle pump（30）Liquid phase entrance Jing pipelines are held liquid bath and are connected with secondary cycle desulfurization, and outlet Jing pipelines are connected with secondary cycle desulphurization circulating absorbing liquid entrance.
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| CN110237627B (en) * | 2019-04-25 | 2022-03-25 | 南京塔川化工设备有限公司 | Device and method for cooling and dedusting tail gas of marine diesel engine |
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