CN212575977U - Sintering flue gas ultra-clean system - Google Patents
Sintering flue gas ultra-clean system Download PDFInfo
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- CN212575977U CN212575977U CN202020334359.3U CN202020334359U CN212575977U CN 212575977 U CN212575977 U CN 212575977U CN 202020334359 U CN202020334359 U CN 202020334359U CN 212575977 U CN212575977 U CN 212575977U
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- 239000003546 flue gas Substances 0.000 title claims abstract description 238
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 228
- 238000005245 sintering Methods 0.000 title claims abstract description 55
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 72
- 230000023556 desulfurization Effects 0.000 claims abstract description 70
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- 239000004071 soot Substances 0.000 claims abstract description 4
- 238000004140 cleaning Methods 0.000 claims abstract 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 55
- 238000005406 washing Methods 0.000 claims description 53
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 46
- 238000010438 heat treatment Methods 0.000 claims description 43
- 238000001816 cooling Methods 0.000 claims description 36
- 229910021529 ammonia Inorganic materials 0.000 claims description 20
- 238000002156 mixing Methods 0.000 claims description 17
- 239000002994 raw material Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 11
- 238000012546 transfer Methods 0.000 claims description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 9
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical group O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 8
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 7
- 239000010440 gypsum Substances 0.000 claims description 7
- 229910052602 gypsum Inorganic materials 0.000 claims description 7
- 235000019738 Limestone Nutrition 0.000 claims description 6
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 6
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 6
- 239000000571 coke Substances 0.000 claims description 6
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 239000006028 limestone Substances 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 claims description 4
- 229910052720 vanadium Inorganic materials 0.000 claims description 4
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 3
- 239000000395 magnesium oxide Substances 0.000 claims description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 3
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 3
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 2
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 2
- 239000004571 lime Substances 0.000 claims description 2
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims description 2
- 239000001095 magnesium carbonate Substances 0.000 claims description 2
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims description 2
- 235000014380 magnesium carbonate Nutrition 0.000 claims description 2
- 235000012245 magnesium oxide Nutrition 0.000 claims description 2
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 235000017550 sodium carbonate Nutrition 0.000 claims description 2
- 229910010413 TiO 2 Inorganic materials 0.000 claims 1
- 238000002347 injection Methods 0.000 claims 1
- 239000007924 injection Substances 0.000 claims 1
- 230000001404 mediated effect Effects 0.000 claims 1
- 239000004408 titanium dioxide Substances 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 abstract description 3
- -1 SO 2 Chemical compound 0.000 abstract 1
- 238000000034 method Methods 0.000 description 48
- 230000003009 desulfurizing effect Effects 0.000 description 25
- 230000000630 rising effect Effects 0.000 description 18
- 239000000779 smoke Substances 0.000 description 18
- 239000000428 dust Substances 0.000 description 15
- 230000008569 process Effects 0.000 description 14
- 239000000047 product Substances 0.000 description 11
- 230000007613 environmental effect Effects 0.000 description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 230000007797 corrosion Effects 0.000 description 7
- 238000005260 corrosion Methods 0.000 description 7
- 230000009467 reduction Effects 0.000 description 7
- 238000006722 reduction reaction Methods 0.000 description 7
- 238000005507 spraying Methods 0.000 description 7
- 229910000831 Steel Inorganic materials 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 6
- 239000010959 steel Substances 0.000 description 6
- 239000003153 chemical reaction reagent Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical group [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 3
- 239000012752 auxiliary agent Substances 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Inorganic materials O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000000979 retarding effect Effects 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- 235000010215 titanium dioxide Nutrition 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 210000004911 serous fluid Anatomy 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L sulfate group Chemical group S(=O)(=O)([O-])[O-] QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-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
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000010446 mirabilite Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000010148 water-pollination Effects 0.000 description 1
Images
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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- 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
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- 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
- B01D2258/0283—Flue gases
-
- 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
- Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Engineering & Computer Science (AREA)
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- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
本实用新型提供了一种效率高、投资低、无二次废弃物，且运行稳定可靠的烧结烟气综合超净治理系统。本实用新型的烧结烟气超净系统包括脱硫塔和脱硝反应器。其中，脱硫塔为湿法脱硫塔，用于脱除烧结烟气中的SO2和烟尘；脱硝反应器用于脱除烧结烟气中的NOx，位于脱硫塔的下游。本实用新型采用先脱硫后脱硝的技术方案，可以避免烟气其他杂质，例如SO2、SO3、NH4HSO4和烟尘等对脱硝催化剂的影响，提高运行可靠性和稳定性。
The utility model provides a comprehensive ultra-clean treatment system for sintering flue gas with high efficiency, low investment, no secondary waste and stable and reliable operation. The sintering flue gas ultra-cleaning system of the utility model comprises a desulfurization tower and a denitration reactor. Among them, the desulfurization tower is a wet desulfurization tower, which is used to remove SO 2 and soot from the sintering flue gas; the denitration reactor is used to remove NO x from the sintering flue gas, and is located downstream of the desulfurization tower. The utility model adopts the technical scheme of first desulfurization and then denitrification, which can avoid the influence of other impurities in flue gas, such as SO 2 , SO 3 , NH 4 HSO 4 and soot, on the denitration catalyst, and improve the operation reliability and stability.
Description
Technical Field
The utility model belongs to the technical field of steelmaking and environmental protection, in particular to sintering flue gas ultra-clean system.
Background
The main pollutant of exhaust gas pollution is SO2、NOxDust and the most prominent industries in which exhaust gas is discharged firstly promote the coal-fired power generation industry and secondly the steel industry. At present, SO2The dust-mixing treatment technology is relatively mature in various industries and can reach 35mg/Nm3And 10mg/Nm3Ultra-low emission levels of (a). For denitration of flue gas, Selective Catalytic Reduction (SCR) method consuming ammonia or urea is generally used. However, some industries have great difficulty in SCR due to the limitation of production process, and it is difficult to reach strict environmental protection standard.
A large amount of waste gas is also generated in the steel production process, mainly comes from sintering flue gas of a sintering machine, and NO of the waste gasxThe content is generally 150-450mg/Nm3And slightly lower than the emission level of coal-fired boilers. Different from the operation process of a coal-fired boiler, the temperature of the flue gas discharged by a sintering machine is lower, generally lower than 200 ℃, and the flue gas denitration technology mature in the prior art cannot be adopted. Because the conventional flue gas denitration process is influenced by SO in the flue gas2The condensation and corrosion effects of ammonium bisulfite caused by the method require the operation temperature to be more than 300 ℃ and 350 ℃ to avoid catalyst deactivation and equipment corrosion.
At present, the method for solving the problem of low-temperature denitration of sintering machine flue gas comprises two schemes: (1) the method adopts a low-temperature denitration method of active coke, the reaction temperature is 80-150 ℃, and the method is called as an active coke method; (2) a medium-temperature denitration method of flue gas heat compensation and a flue gas/flue gas heat exchanger (GGH) is adopted, the heat compensation and heat exchange method is abbreviated, and the reaction temperature is 300-350 ℃.
The activated coke method can simultaneously treat SO by utilizing good adsorption and oxidation characteristics of the activated coke method2、NOxDust and other pollutants, the flue gas can be higher than dew point temperature and discharges moreover, does not have the white smoke influence problem of wet process emission, has better development prospect, but the investment is high, and the energy consumption is high, and is with high costs to have certain flammable and explosive's safety risk.
In the aspect of denitration, in order to utilize the SCR technology, a flue gas external heating method of coal gas or natural gas is mainly adopted, flue gas with the temperature of about 150 ℃ is heated to be more than 320 ℃, the flue gas is sent into an SCR reactor, and the high-temperature flue gas passes through a gas-gas heat exchanger to recover heat, so that the investment is undoubtedly large, and the energy consumption is high. For example, the document "shang bin et al," discussion of denitration technique of sintering flue gas ", proceedings of the eighth annual meeting of china iron and steel, 2011", "zhou lirong," discussion of application of SCR denitration technique of sintering flue gas in iron and steel works, and "2014" report methods in the industry of environmental protection in china. Patent CN104195326A discloses a sintering energy-saving process and a system for removing various pollutants, wherein flue gas is heated by a two-stage gas-gas heat exchanger (GGH), then a burner for burning gas is adopted for heat compensation heating, denitration is carried out firstly, and then desulfurization is carried out, namely, the denitration and desulfurization processes are carried out firstly, and the denitration reaction temperature is more than 300 ℃. Patents CN107983155A and CN108786455A disclose a sintering flue gas desulfurization and denitration system, which also adopts the process of heating GGH, heating and denitration by supplementary heating of coal gas for combustion, and then desulfurization, wherein the temperature of the denitration reactor is 300-320 ℃.
However, the existing intermediate-temperature SCR method with heat exchange has a problem of influencing the operation stability and the denitration efficiency. Because the denitration is carried out firstly, SO in the flue gas2Will be oxidized to SO3Although the oxidation rate is lower than 1%, because the inside of the flue gas heat exchanger has the problem of cold and hot alternation, the condensed ammonium bisulfate is bound to appear, and the heat exchange channel in the heat exchanger is scaled and blockedAnd corroding. In particular, the GGHs used in industry are all rotary heat exchangers, and the flue gas at the hot side and the flue gas at the cold side pass through the same flue, so that the blocking frequency is generally higher, especially under the condition of higher dust content of the flue gas. To solve this problem, the industry has been equipped with high pressure flush water systems, with frequent periodic flushes, which further exacerbates the corrosion problem of the equipment. In addition, the process of denitration and desulfuration is adopted, the limestone-gypsum and ammonia method is adopted for desulfuration, the moisture content of flue gas is large, the temperature is low, and the problems of flue gas tailing and white smoke pollution caused by the fact that the flue gas emission is close to the dew point temperature are easy to occur. Patent CN108837677A discloses a pre-desulfurization and post-denitrification process for semi-dry desulfurization, wherein lime slurry and sodium bicarbonate are used as raw materials in the semi-dry desulfurization process, the cost is high, and secondary waste is discharged.
In a word, the existing sintering flue gas denitration technology has the defects, the development of the environmental protection work is restricted, and the development of a new comprehensive treatment technology suitable for sintering machine flue gas has important value.
SUMMERY OF THE UTILITY MODEL
In view of the above-mentioned defects of the prior art, the present invention aims to provide a sintering flue gas comprehensive ultra-clean treatment system and method with high efficiency, low investment, no secondary waste and stable and reliable operation.
In order to achieve the above object, on the one hand, the utility model provides a sintering flue gas ultra-clean system, including desulfurizing tower and denitration reactor. Wherein, the desulfurizing tower is used for removing SO in the sintering flue gas2And smoke dust, wherein the desulfurizing tower is a wet desulfurizing tower; denitration reactor for removing NO in sintering flue gasxAnd the denitration reactor is positioned at the downstream of the desulfurization tower. The utility model discloses a denitration's after desulfurization technical scheme earlier can avoid other impurity of flue gas, for example SO2、SO3、NH4HSO4And the influence of smoke dust and the like on the denitration catalyst, and the operation reliability and stability are improved.
Further, the utility model discloses a sintering flue gas ultra-clean system still includes first heat exchanger and second heat exchanger, includes cooling section and intensification section respectively. The cooling section of the first heat exchanger is positioned on an inlet flue of the desulfurizing tower and used for cooling and heating the raw flue gas; the temperature rising section of the first heat exchanger is positioned on the flue between the outlet of the desulfurizing tower and the inlet of the temperature rising section of the second heat exchanger and used for heating the desulfurized flue gas. The temperature rising section of the second heat exchanger is used for further heating the desulfurized flue gas, the inlet of the temperature rising section of the second heat exchanger is connected with the outlet of the temperature rising section of the first heat exchanger, and the outlet of the temperature rising section of the second heat exchanger is connected with the inlet flue of the denitration reactor; the cooling section of the second heat exchanger is used for cooling and heating the denitrated flue gas, an inlet of the cooling section is connected with an outlet of the denitration reactor, and an outlet of the cooling section is connected with downstream equipment.
Further, the first heat exchanger is preferably a water-borne flue gas heat exchanger, and the second heat exchanger is preferably a rotary flue gas heat exchanger, and each heat exchanger comprises a cooling section and a heating section.
Furthermore, the cooling section of the water-borne flue gas heat exchanger is arranged on the inlet flue of the desulfurizing tower, and the heating section is arranged on the flue between the outlet of the desulfurizing tower and the inlet of the rotary flue gas heat exchanger, so that the problems of corrosion and blockage of the rotary flue gas heat exchanger can be solved, and the running stability of the rotary flue gas heat exchanger is improved. The water medium type heat exchanger takes desalted hot water as a working medium, hot water is conveyed to flow between the temperature reduction section and the temperature rise section through the circulating pump, heat is taken out of hot raw flue gas in the temperature reduction section, the hot raw flue gas is conveyed to the temperature rise section to heat desulfurized flue gas, the heat of the flue gas is utilized, and the heat transfer element is a fin heat transfer pipe, so that the energy is saved, and the efficiency is high.
Furthermore, the rotary flue gas heat exchanger is positioned above the denitration reactor, so that the structure is compact, the occupied area is small, and the flue gas resistance is small. An inlet of a temperature rising section of the rotary flue gas heat exchanger is connected with an outlet of a temperature rising section of the hydrophily flue gas heat exchanger, and an outlet of the temperature rising section of the rotary flue gas heat exchanger is connected with an inlet flue of the denitration reactor; the inlet of the cooling section of the rotary flue gas heat exchanger is connected with the outlet of the denitration reactor, and the outlet of the cooling section of the rotary flue gas heat exchanger is connected with downstream equipment, so that the efficiency of the denitration reactor can be improved, and good heat transfer performance is ensured.
Further, the desulfurization tower comprises at least two circulating spray water washing sections, typically, for example, two, three, four or five water washing sections, each of which comprises a spray member, a flue gas dehydration member, a circulating pump and a circulating tank, respectively. Wherein, according to the flow direction of the flue gas, the first washing section that the flue gas passes through is the preceding washing section, and the last washing section is the back washing section. The front washing section is connected with a flue gas inlet of the desulfurizing tower, and the rear washing section is connected with a flue gas outlet of the desulfurizing tower. The front washing section can obviously reduce the content of salt and dust in the rear washing section, so that the rear washing section is basically clear water, the discharged flue gas does not corrode and block a subsequent heat exchanger, and the ultralow dust index is guaranteed.
Further, water enters the desulfurizing tower from the rear water washing section, flows through the rear water washing section firstly, and then enters the front water washing section; the desulfurization raw material and the oxidation air enter the desulfurization tower from the front washing section, and the desulfurization product is taken out from the front washing section, SO that SO in the flue gas at the outlet of the desulfurization tower can be ensured2And the smoke content can reach the ultra-low emission index, and subsequent equipment is not blocked or corroded.
Further, the desulfurization raw material of the present invention may be any alkaline material, such as limestone (CaCO)3) Or lime (CaO), magnesium carbonate (MgCO)3) Or magnesium oxide (MgO), sodium carbonate (Na)2CO3) Or caustic soda (NaOH), ammonia (including ammonia gas, ammonia water or liquid ammonia), the corresponding desulfurization techniques are called calcium method, magnesium method, sodium method and ammonia method, respectively, and the desulfurization products are gypsum, magnesium sulfate, sodium sulfate (mirabilite) and ammonium sulfate, respectively. Preferably, the calcium method and the ammonia method are adopted for desulfurization, for example, limestone or ammonia water is adopted as a desulfurization raw material, and the obtained desulfurization product is gypsum or ammonium sulfate which can be respectively sold as a retarding additive and a fertilizer of building cement, so that the method has good economic benefit.
Further, the denitration reactor is filled with a honeycomb denitration catalyst, and a high-temperature hot air generation member and an ammonia mixing member are arranged on an inlet flue of the denitration reactor.
Further, the denitration catalyst is a vanadium-titanium catalyst, and the active component of the catalyst is V2O5And also an auxiliary agent WO3And MoO3The carrier is titanium white TiO2The catalyst can be a commercial honeycomb catalyst, the honeycomb holes of the catalyst are square, and the equivalent pore diameter is 3-5 mm. Because the utility model discloses a denitration method after desulfurization earlier, do not worry SO2The side reaction effect of oxidation, the vanadium content in the catalyst can be higher, between 1 and 2 percent; the SCR reaction temperature can be lower, for example, less than 300 ℃, preferably between 200 ℃ and 300 ℃, so that the design requirement and the manufacturing cost of the rotary flue gas heat exchanger can be reduced.
Furthermore, the high-temperature hot air generating member is preferably a blast furnace burning blast furnace gas or coke oven gas, and can be directly installed on a flue, or can form high-temperature hot air of about 1000 ℃ to be conveyed into the flue. The high-temperature hot air generation component supplements heat to the flue gas, so that the efficiency of the denitration reactor is improved, and good heat transfer performance and higher flue gas emission temperature are ensured.
Further, the ammonia mixing component is preferably a multi-nozzle jet mixing element, and the nozzle is generally a compressed air two-fluid atomization nozzle, so that the efficiency is high, and the mixing effect is good. The ammonia mixing component can carry out intensive mixing and atomizing to denitration reagent ammonia, further improves denitration reactor efficiency to guarantee better heat transfer performance.
On the other hand, the utility model also provides a method for adopt above-mentioned sintering flue gas ultra-clean system to handle sintering flue gas, including following step:
(1) cooling and heating flue gas: will contain SO2、NOxIntroducing high-temperature raw flue gas of the flue dust and the smoke dust into a cooling section of the first heat exchanger, and performing countercurrent heat exchange with a heating medium of the first heat exchanger, so that the temperature of the flue gas is reduced, and the temperature of the heating medium is increased;
preferably, the temperature reduction amplitude of the flue gas is 20-50 ℃;
(2) flue gas desulfurization: introducing the cooled and heated flue gas into a desulfurizing tower, wherein the desulfurizing tower is provided with at least two circulating spray washing sections, and the flue gas is subjected to washing, dust removal and absorption desulfurization in the circulating spray washing sections;
preferably; the relative density of the circulating water of the final water washing section is less than 1.01, the desulfurization product is sulfate, and SO of the desulfurized flue gas2The content is less than 35mg/Nm3The smoke content is less than 10mg/Nm3The ultra-low emission index is met; the temperature of the flue gas is 45-60 ℃, and is close to the water dew point of the flue gas;
(3) heating flue gas and raising temperature: introducing the desulfurized flue gas into a temperature rising section of the first heat exchanger, and carrying out countercurrent heat exchange with a heating medium from the temperature falling section of the first heat exchanger, so that the temperature of the flue gas is raised, and the temperature of the heating medium is lowered;
preferably, the temperature rise amplitude of the flue gas is 20-50 ℃ which is 20 ℃ higher than the water dew point of the flue gas, so as to prevent the corrosion of subsequent equipment;
(4) heating flue gas and raising temperature: introducing the flue gas from the step (3) into a temperature rising section of a second heat exchanger, and exchanging heat with a heat exchange element of the second heat exchanger to rise the temperature so as to enable the temperature of the flue gas to reach the reaction activity temperature required by the subsequent denitration step;
preferably, the temperature rise range of the flue gas is 100-200 ℃;
(5) flue gas heat supplementing and temperature rising: mixing the flue gas from the step (4) with hot air generated by a high-temperature hot air generating component, and then further heating the flue gas to provide a necessary heat transfer temperature difference for a second heat exchanger;
preferably, the temperature rise amplitude of the flue gas is 20-30 ℃;
(6) flue gas denitration: introducing the flue gas from the step (5) into a denitration reactor, wherein NO in the flue gasxThe ammonia reacts with a denitration reagent ammonia introduced by the ammonia mixing component to be converted into nitrogen and water, so that the flue gas denitration is realized;
preferably, NO in denitrated flue gasxThe content is less than 50mg/Nm3The ultra-low emission index is met;
(7) cooling and heat recovery of flue gas: introducing the flue gas from the step (6) into a cooling section of a second heat exchanger, absorbing heat by a heat exchange element of the second heat exchanger, and reducing the temperature of the flue gas;
preferably, the temperature reduction amplitude of the flue gas is 100-;
(8) and (3) discharging flue gas: introducing the flue gas from the step (7) into a draught fan, and then sending the flue gas into a chimney to be discharged into the atmosphere;
preferably, the emission temperature of the flue gas is greater than 90 ℃ to meet the requirement of white smoke-free emission of the flue gas.
The utility model discloses a sintering flue gas ultra-clean system's beneficial technological effect shows in following aspect at least:
(1) eliminate SO2、SO3The influence of ammonium bisulfate and smoke dust on the denitration reactor and the catalyst improves the service life of the reactor and the catalyst;
(2) the influence of ammonium bisulfate and desulfurization entrained slurry on the blockage and corrosion of the rotary heat exchanger is eliminated, and the operation stability and efficiency of the heat exchanger are improved;
(3) calcium carbonate or ammonia is used as a raw material in the desulfurization process, so that the desulfurization product has better application and the problem of secondary waste is solved;
(4) the temperature of the discharged flue gas is more than 100 ℃, so that white smoke pollution can be eliminated;
(5) can realize the ultralow emission index of the sintering flue gas and has good environmental protection benefit.
In a word, the sintering flue gas ultra-clean system and the method of the utility model have comprehensive performance superior to the prior art, and have obvious environmental protection, social and economic benefits.
Drawings
Fig. 1 is a schematic diagram of the structure and flow of a sintering flue gas ultra-clean system according to a preferred embodiment of the present invention.
Detailed Description
The following embodiments of the present invention will be described in detail, and the following embodiments are implemented on the premise of the technical solution of the present invention, and detailed embodiments and specific operation procedures are given, but the scope of the present invention is not limited to the following embodiments.
Example 1
A certain iron and steel plant has a sintering machine with the scale of 265m2Annual production of 200 ten thousand tons of agglomerate and 72 ten thousand Nm of smoke gas3Hr, raw flue gas temperature 160 deg.C, in which SO2＝2000mg/Nm3，NOx＝300mg/Nm3Smoke dust 50mg/Nm3The sintering flue gas ultra-clean system of the embodiment is applied to implement the environmental protection target of ultra-low emission.
As shown in fig. 1, the sintering flue gas ultra-clean system of the embodiment includes a desulfurization tower 100 and a denitration reactor 300, and the denitration reactor 300 is located downstream of the desulfurization tower 100, SO as to avoid other impurities in the flue gas, including SO2、SO3、NH4HSO4And the influence of smoke dust and the like on the denitration catalyst, and the operation reliability and stability are improved.
The sintering flue gas ultra-clean system also comprises a rotary flue gas heat exchanger 200 and a water-borne flue gas heat exchanger 400. The rotary flue gas heat exchanger 200 is located above the denitration reactor 300, and has the advantages of compact structure, small floor area and small flue gas resistance.
The water-borne flue gas heat exchanger 400 comprises a cooling section 401 and a heating section 402. Wherein, the cooling section 401 is arranged on the inlet flue of the desulfurizing tower 100, and the heating section 402 is arranged on the flue between the outlet of the desulfurizing tower 100 and the inlet of the rotary flue gas heat exchanger 200. The water-borne flue gas heat exchanger 400 takes desalted hot water as a working medium, the hot water is conveyed to flow between the temperature reduction section 401 and the temperature rise section 402 through the circulating pump 403, heat is taken out of hot raw flue gas in the temperature reduction section 401, the hot raw flue gas is conveyed to the temperature rise section 402 to heat desulfurized flue gas coming out of the desulfurization tower 100, the heat of the flue gas is fully utilized, and the heat transfer elements are fin heat transfer tubes, so that the energy is saved, and the efficiency is high.
The desulfurization tower 100 comprises at least two circulating spray washing sections, wherein the front washing section 101 is connected with a flue gas inlet of the desulfurization tower 100, and the rear washing section 102 is connected with a flue gas outlet of the desulfurization tower 100. Wherein, the front washing section 101 comprises a spraying component 1011, a flue gas dewatering component 1012, a circulating pump 1013 and a first circulating pool 1014, and the rear washing section 102 comprises a first spraying component 1021, a first flue gas dewatering component 1022, a first circulating pump 1023 and a first circulating pool 1024. The process water required by desulfurization enters from the rear washing section 102, flows through the rear washing section 102 first, and then enters the front washing section 101, the desulfurization raw material and the oxidizing air enter the front washing section 101, and the desulfurization product is taken out from the front washing section 101.
The desulfurization in this example was carried out by the calcium method using limestone (CaCO) as the raw material3) The desulfurization product is gypsum which can be used as building material cementThe retarding additive is used, and is a wet desulphurization process. After the combined action of the first spraying component 1011, the first flue gas dehydration component 1012, the first circulating pump 1013 and the first circulating tank 1014 of the front water washing section 101, the flue gas contains SO2Is 30mg/Nm3. The circulating water of the front washing section 101 is a slurry containing gypsum, sodium chloride and other salts, the content of the slurry is 30 wt% in terms of solid content, and the flue gas contains 40-60mg/Nm of desulfurization slurry3. The flue gas passes through the post-washing section 102 and passes through the combined action of the second spraying component 1021, the second flue gas dehydration component 1022, the second circulating pump 1023 and the second circulating pool 1024, and the flue gas contains SO2Is 20mg/Nm3. The circulating water in the post-washing section 102 is substantially clear water, wherein the solid content is less than 0.05 percent, and the water content in the flue gas is 50mg/Nm3And is basically clear water, has no influence on subsequent equipment, namely the temperature rising section 402 of the water medium heat exchanger 400, and cannot cause the problems of scaling and blockage.
The rotary flue gas heat exchanger 200 comprises a cooling section 201 and a heating section 202, wherein an inlet of the heating section 202 is connected with an outlet of a heating section 402 of the water-borne flue gas heat exchanger 400, an outlet of the heating section 202 is connected with an inlet flue of the denitration reactor 300, an outlet of the denitration reactor 300 is connected with an inlet of the cooling section 201, and an outlet of the cooling section 201 is connected with downstream equipment.
The flue gas denitration reactor 300 is filled with a honeycomb SCR denitration catalyst 301, and a mixing member 302 of denitration reagent ammonia and a high-temperature hot air generation member 303 are provided in an inlet flue of the denitration reactor 300.
The denitration catalyst is a vanadium-titanium catalyst, and the active component of the catalyst is V2O5And also an auxiliary agent WO3And MoO3The carrier is titanium white TiO2The commercial honeycomb catalyst is adopted, the honeycomb holes of the catalyst are square, the equivalent pore diameter is 4.0mm, and the method of firstly desulfurizing and then denitrating does not need to worry about SO2The side reaction influence of oxidation, the vanadium content in the catalyst is 2 percent, and the reaction temperature is 280 ℃.
The mixing component 302 of the denitration reagent ammonia is a multi-nozzle spraying mixing element, and the nozzle is a two-fluid atomization nozzle of compressed air, so that the efficiency is high, and the mixing effect is good.
The high-temperature hot air generating member 303 is a hot air furnace burning blast furnace gas, and is directly installed on an inlet flue of the denitration reactor 300.
The method for treating the sintering flue gas by adopting the sintering flue gas ultra-clean system comprises the following steps:
(1) cooling and heating flue gas: will contain SO2、NOxIntroducing the high-temperature raw flue gas with dust into a cooling section 401 of a water medium heat exchanger 400, carrying out countercurrent heat exchange with hot water conveyed by a circulating pump 403, cooling the flue gas, wherein the cooling amplitude is 20-50 ℃, and heat is stored in the heat medium water;
(2) flue gas desulfurization: introducing the flue gas subjected to temperature reduction and heat extraction into the desulfurizing tower 100, wherein the desulfurizing tower 100 is provided with two washing sections 101 and 102, the flue gas is washed, dedusted and absorbed and desulfurized in the front washing section 101, and is further washed, dedusted and absorbed and desulfurized in the rear washing section 102, the density of the rear washing section is less than 1.01, the desulfurization product is sulfate, and SO of the desulfurized flue gas is less than that of the desulfurized flue gas2The content is less than 35mg/Nm3The smoke content is less than 10mg/Nm3The ultra-low emission index is met; the temperature is 45-60 ℃, and the temperature is close to the water dew point of the flue gas;
(3) heating flue gas and raising temperature: introducing the desulfurized flue gas into a heating section 402 of a water medium heat exchanger 400, carrying out countercurrent heat exchange with heat medium water from a cooling section 401, heating the flue gas, wherein the heating amplitude is 20-50 ℃, the heating amplitude is 20 ℃ higher than the water dew point of the flue gas, and the corrosion of subsequent equipment is prevented;
(4) heating flue gas and raising temperature: introducing the flue gas from the step (3) into a temperature rising section 202 of a rotary heat exchanger 200, exchanging heat with a continuously rotating heat exchange element, and rising the temperature, wherein the temperature rising amplitude is 100-;
(5) flue gas heat supplementing and temperature rising: after the flue gas from the step (4) is mixed with the hot air generated by the high-temperature hot air generating component 303, the temperature of the flue gas is further increased by 20-30 ℃, and a necessary heat transfer temperature difference is provided for the rotary heat exchanger;
(6) flue gas denitration: introducing the flue gas from step (5) into a denitration reactor 300, wherein NO in the flue gasxReacts with denitration reagent ammonia introduced by the ammonia mixing component 302 to become nitrogen and water, realizes flue gas denitration, and NO in the denitrated flue gasxThe content is less than 50mg/Nm3The ultra-low emission index is met;
(7) cooling and heat recovery of flue gas: introducing the flue gas from the step (7) into a cooling section 201 of a rotary heat exchanger 200, absorbing heat by a rotary heat exchange element, reducing the temperature of the flue gas by 100-200 ℃, and fully recovering the heat;
(8) and (3) discharging flue gas: and (4) introducing the flue gas from the step (7) into an induced draft fan 500, and then sending the flue gas into a chimney 600 to be discharged into the atmosphere, wherein the temperature of the flue gas is more than 100 ℃, and the requirement of white smoke-free emission of the flue gas is met.
The ultra-clean system of the embodiment is used for treating sintering flue gas, and SO is contained in flue gas discharged from the flue gas outlet of the desulfurizing tower 1002Content 20mg/Nm3Dust content 4.1mg/Nm3The inlet flue gas temperature of the rotary flue gas heat exchanger 200 is 78 ℃, the flue gas outlet temperature of the rotary flue gas heat exchanger 200 is 105 ℃, NOxContent 36mg/Nm3The comprehensive environmental protection index is excellent, and the smoke emission is free from white smoke. In addition, the desulfurization tower 100 adopts limestone as a desulfurization raw material, and the obtained desulfurization product is gypsum which has good economical efficiency as a retarding additive of building cement.
Example 2
A certain iron and steel plant has a sintering machine with the scale of 360m 2400 ten thousand tons of annual sinter and 120 ten thousand Nm smoke volume3Hr, raw flue gas temperature 170 deg.C, SO2＝1500mg/Nm3，NOx＝250mg/Nm3Soot rate of 40mg/Nm3The sintering flue gas ultra-clean system of the embodiment is applied to implement the environmental protection target of ultra-low emission.
The sintering flue gas ultra-clean system of this embodiment is roughly the same as embodiment 1, and the difference is that, the flue gas desulfurization of this embodiment adopts the ammonia process, and the desulfurization raw materials is the aqueous ammonia, and aqueous ammonia concentration is 15%, and the desulfurization product is ammonium sulfate, can regard as the chemical fertilizer to use, also is a wet flue gas desulfurization process. The first spraying component 1011, the first flue gas dehydration component 1012 and the first circulating pump which pass through the front water washing section 1011013 and the first circulation tank 1014, the flue gas contains SO2Is 25mg/Nm3. The circulating water of the front water washing section is serous fluid containing ammonium sulfate, which is 20 percent by weight of the solid content, and the flue gas contains 40 to 60mg/Nm of desulfurized serous fluid3. The flue gas passes through the post-washing section 102 and passes through the combined action of the second spraying component 1021, the second flue gas dehydration component 1022, the second circulating pump 1023 and the second circulating pool 1024, and the flue gas contains SO2Is 12mg/Nm3. The circulating water in the post-washing section 102 is substantially clear water, wherein the solid content is less than 0.05 percent, and the water content in the flue gas is 50mg/Nm3And is basically clear water, has no influence on subsequent equipment, namely the temperature rising section 402 of the water medium heat exchanger 400, and cannot cause the problems of scaling and blockage.
In addition, the denitration catalyst is a vanadium-titanium catalyst, and the active component of the catalyst is V2O5And also an auxiliary agent WO3And MoO3The carrier is titanium white TiO2The commercial honeycomb catalyst is adopted, the honeycomb holes of the catalyst are square, the equivalent pore diameter is 3.2mm, and the method of firstly desulfurizing and then denitrating does not need to worry about SO2The side reaction influence of oxidation, vanadium content in the catalyst is 1.8%, and reaction temperature is 250 ℃.
The ultra-clean system of the embodiment is used for treating sintering flue gas, and SO is contained in flue gas discharged from the flue gas outlet of the desulfurizing tower 1002Content 12mg/Nm3Dust content 3.1mg/Nm3The inlet flue gas temperature of the rotary flue gas heat exchanger 200 is 75 ℃, the flue gas outlet temperature of the rotary flue gas heat exchanger 200 is 103 ℃, NOxContent 24mg/Nm3The comprehensive environmental protection index is excellent, and the smoke emission is free from white smoke. In addition, the desulfurizing tower 100 adopts ammonia water as a desulfurizing raw material, and the obtained desulfurizing product is ammonium sulfate which can be used as a chemical fertilizer, so that the desulfurizing tower has good economical efficiency.
The foregoing has described in detail preferred embodiments of the present invention. It should be understood that numerous modifications and variations could be devised by those skilled in the art in light of the teachings of this invention without undue experimentation. Therefore, the technical solutions that can be obtained by a person skilled in the art through logic analysis, reasoning or limited experiments based on the prior art according to the concepts of the present invention should be within the scope of protection defined by the claims.
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| CN105597513A (en) * | 2016-01-29 | 2016-05-25 | 石家庄宇清环保科技有限公司 | Flue gas desulfurizing and dust removing device of coal-fired boiler |
| CN108499350A (en) * | 2017-02-24 | 2018-09-07 | 天津华赛尔传热设备有限公司 | A kind of flue gas of wet desulphurization disappears white system and method |
| EP3421115A3 (en) * | 2017-09-22 | 2019-05-01 | Jiangnan Environmental Protection Group Inc. | Apparatus and method for ammonia-based desulfurization |
| CN108479332A (en) * | 2018-04-16 | 2018-09-04 | 天津华赛尔传热设备有限公司 | A kind of low-temperature flue gas desulphurization denitration disappears white system |
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| CN109381990A (en) * | 2018-10-17 | 2019-02-26 | 北京国电龙源环保工程有限公司 | A kind of steel sintering flue gas denitrification system and the method for denitration using system progress |
| CN212575977U (en) * | 2019-03-18 | 2021-02-23 | 上海申欣川环保工程技术有限公司 | Sintering flue gas ultra-clean system |
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