CN116531932A - Ammonia-ammonium sulfite combined desulfurization and denitrification system - Google Patents
Ammonia-ammonium sulfite combined desulfurization and denitrification system Download PDFInfo
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- CN116531932A CN116531932A CN202310411796.9A CN202310411796A CN116531932A CN 116531932 A CN116531932 A CN 116531932A CN 202310411796 A CN202310411796 A CN 202310411796A CN 116531932 A CN116531932 A CN 116531932A
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- ammonium sulfite
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 31
- 230000023556 desulfurization Effects 0.000 title claims abstract description 31
- NSQOWYPJQKUQEJ-UHFFFAOYSA-N N.S(=O)([O-])[O-].[NH4+].[NH4+] Chemical compound N.S(=O)([O-])[O-].[NH4+].[NH4+] NSQOWYPJQKUQEJ-UHFFFAOYSA-N 0.000 title claims abstract description 19
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims abstract description 110
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000003546 flue gas Substances 0.000 claims abstract description 61
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 60
- 238000006243 chemical reaction Methods 0.000 claims abstract description 52
- 239000000428 dust Substances 0.000 claims abstract description 34
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 28
- 239000002245 particle Substances 0.000 claims abstract description 27
- 238000009833 condensation Methods 0.000 claims abstract description 25
- 230000005494 condensation Effects 0.000 claims abstract description 25
- 239000007787 solid Substances 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 15
- 238000001556 precipitation Methods 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 48
- 230000001105 regulatory effect Effects 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 238000001816 cooling Methods 0.000 claims description 18
- 239000013078 crystal Substances 0.000 claims description 18
- 238000001914 filtration Methods 0.000 claims description 17
- 239000000843 powder Substances 0.000 claims description 17
- 238000000227 grinding Methods 0.000 claims description 14
- 230000008569 process Effects 0.000 claims description 13
- 238000001035 drying Methods 0.000 claims description 12
- 230000000295 complement effect Effects 0.000 claims description 6
- 239000000706 filtrate Substances 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 5
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 6
- 239000006227 byproduct Substances 0.000 abstract description 5
- 230000008929 regeneration Effects 0.000 abstract description 3
- 238000011069 regeneration method Methods 0.000 abstract description 3
- 230000009469 supplementation Effects 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 abstract description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 5
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 5
- 235000011130 ammonium sulphate Nutrition 0.000 description 5
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- 239000001284 azanium sulfanide Substances 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
Classifications
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- 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
- B01D53/81—Solid phase processes
-
- 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
- B01D53/002—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 condensation
-
- 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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- 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
- B01D53/76—Gas phase processes, e.g. by using aerosols
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- 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
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- 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
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- 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
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- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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Abstract
The invention relates to an ammonia-ammonium sulfite combined desulfurization and denitrification system which comprises a reaction tower, a solid particle supplementary device, a condensation dust remover, a flue gas post-treatment device, an adjusting tank, an ammonium sulfite precipitation system and an ammonium sulfite treatment system, wherein the reaction tower is connected with an ammonia adding device, a flue gas outlet of the reaction tower is connected with a flue gas inlet of the solid particle supplementary device, a flue gas outlet of the solid particle supplementary device is connected with an inlet of the condensation dust remover, an outlet of the condensation dust remover is connected with a flue gas inlet of the flue gas post-treatment device, a condensate outlet of the condensation dust remover is connected with the adjusting tank, and the adjusting tank is connected with the ammonium sulfite precipitation system. The advantages are that: the method adopts ammonium sulfite and ammonia as raw materials to realize the purposes of desulfurization and denitrification, and the regeneration cycle of reaction materials and the supplementation of ammonium sulfite generated by desulfurization to the reaction raw materials, so that the material operation cost of the system is greatly reduced, a catalyst is not needed, a high-temperature reaction temperature window is not needed, desulfurization waste water is not needed to be treated, and the problems of low-value byproduct disposal and the like are avoided.
Description
Technical Field
The invention relates to the technical field of flue gas treatment equipment, in particular to an ammonia-ammonium sulfite combined desulfurization and denitrification system.
Background
In industrial processes, many industries require the combustion of coal to provide heat energy, and the flue gas produced by such processes contains significant amounts of SO 2 And NOx, if left untreated, can cause very serious environmental pollution. At present, the emission standard in the atmospheric aspect is specific to SO 2 And the emission concentration of NOx are stringent.
The process types in the aspect of desulfurization are more, the types are tens, and the flue gas desulfurization is divided into: wet, semi-dry and dry desulfurization processes. The wet desulfurization technology is mature, high in efficiency and simple in operation. The traditional limestone/lime-gypsum flue gas desulfurization process adopts calcium sulfite and calcium sulfate generated after absorbing sulfur dioxide by a calcium-based desulfurizing agent, and scaling and blocking phenomena are easily formed in a desulfurizing tower and a pipeline due to the low solubility of the calcium sulfite and the calcium sulfate. In the aspect of denitration, the main stream mainly comprises two types of SCR and SNCR, wherein the SCR and the SNCR can be carried out by a catalyst, the SNCR does not need the catalyst, but the SNCR is more harsh in reaction temperature window and is often easily restricted by a hearth structure.
Therefore, there is a need to develop a new desulfurization and denitrification system to solve the above technical problems.
Disclosure of Invention
The invention aims to provide an ammonia-ammonium sulfite combined desulfurization and denitrification system, which effectively overcomes the defects of the prior art.
The technical scheme for solving the technical problems is as follows:
the utility model provides an ammonia-ammonium sulfite combines SOx/NOx control system, including the reaction tower, solid particle complement device, the condensation dust remover, flue gas aftertreatment device, the equalizing basin, ammonium sulfite separates out system and ammonium sulfite processing system, the above-mentioned reaction tower is connected with the ammonia adding device, the flue gas export of above-mentioned reaction tower is connected the flue gas import of above-mentioned solid particle complement device, the flue gas export of above-mentioned solid particle complement device is connected the import of above-mentioned condensation dust remover, the export of above-mentioned condensation dust remover is connected the flue gas import of above-mentioned flue gas aftertreatment device, the condensate outlet of above-mentioned condensation dust remover is connected the equalizing basin, the above-mentioned equalizing basin is connected the above-mentioned ammonium sulfite separates out system, the above-mentioned ammonium sulfite separates out system and is used for separating out the sulfurous acid crystal, the above-mentioned ammonium sulfite processing system is used for with the ammonium sulfite crystal that the above-mentioned ammonium sulfite separates out system separates out and handles into dry and loose powder, the bottom of above-mentioned reaction tower is equipped with the ammonium sulfite powder entry.
On the basis of the technical scheme, the invention can be improved as follows.
Further, the solid particle supplementary collection device is a bag-type dust collector.
Further, the flue gas aftertreatment device is a water scrubber, and a liquid outlet of the water scrubber is connected with the regulating tank.
Further, the bottom of the regulating tank is connected with an ammonia adding pipeline with a valve, and the ammonia adding pipeline is connected with an ammonia source.
Further, the ammonium sulfite precipitation system comprises a liquid concentration device, a cooling crystallizer and a liquid filtering device, wherein an inlet of the liquid concentration device is connected with the regulating tank, an outlet of the liquid concentration device is connected with an inlet of the cooling crystallizer, a crystal slurry outlet of the cooling crystallizer is connected with an inlet of the liquid filtering device, and a filtrate discharge port of the liquid filtering device is connected with an inlet of the liquid concentration device.
Further, the liquid concentrating device is a flash tank.
Further, the liquid filtering device is a vacuum belt or a plate-and-frame filter press.
Further, the ammonium sulfite treatment system comprises an anaerobic drying device and a grinding device, wherein the discharge end of the anaerobic drying device is connected with the feed end of the grinding device through a material conveying device, the discharge end of the grinding device is connected with an ammonium sulfite storage bin, a discharge port is arranged on the ammonium sulfite storage bin, and the discharge port of the ammonium sulfite storage bin is connected with the ammonium sulfite powder inlet through a feeding machine.
Further, the anaerobic dryer is an anaerobic dryer, and the feeding machine is an induced draft feeding machine.
Further, the ammonia adding device is a liquid ammonia tank.
The beneficial effects of the invention are as follows: the method adopts ammonium sulfite and ammonia as raw materials to realize the purposes of desulfurization and denitrification, and the regeneration cycle of reaction materials and the supplementation of ammonium sulfite generated by desulfurization to the reaction raw materials, so that the material operation cost of the system is greatly reduced, a catalyst is not needed, a high-temperature reaction temperature window is not needed, desulfurization waste water is not needed to be treated, and the problems of low-value byproduct disposal and the like are avoided.
Drawings
FIG. 1 is a schematic diagram of the ammonia-ammonium sulfite combined desulfurization and denitrification system.
In the drawings, the list of components represented by the various numbers is as follows:
1. a reaction tower; 2. solid particle supplementary collection device; 3. condensing dust remover; 4. a flue gas post-treatment device; 5. an adjusting tank; 6. an ammonia adding device; 71. a liquid concentrating device; 72. cooling the crystallizer; 73. a liquid filtration device; 81. an anaerobic drying device; 82. a grinding device; 83. ammonium sulfite storage bin; 84. and a feeding machine.
Detailed Description
The principles and features of the present invention are described below with reference to the drawings, the examples are illustrated for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention.
Examples: as shown in fig. 1, the ammonia-ammonium sulfite combined desulfurization and denitrification system of this embodiment includes a reaction tower 1, a solid particle supplementary device 2, a condensation dust remover 3, a flue gas post-treatment device 4, a regulating tank 5, an ammonium sulfite precipitation system and an ammonium sulfite treatment system, wherein the reaction tower 1 is connected with an ammonia adding device 6, a flue gas outlet of the reaction tower 1 is connected with a flue gas inlet of the solid particle supplementary device 2, a flue gas outlet of the solid particle supplementary device 2 is connected with an inlet of the condensation dust remover 3, an outlet of the condensation dust remover 3 is connected with a flue gas inlet of the flue gas post-treatment device 4, a condensed water outlet of the condensation dust remover 3 is connected with the regulating tank 5, the regulating tank 5 is connected with the ammonium sulfite precipitation system, the ammonium sulfite precipitation system is used for precipitating ammonium sulfite crystals, the ammonium sulfite treatment system is used for treating the ammonium sulfite crystals precipitated by the ammonium sulfite precipitation system into dry and loose powder, and an ammonium sulfite powder inlet is arranged at the bottom of the reaction tower 1.
The ammonia-ammonium sulfite combined desulfurization and denitrification system of the embodiment is suitable for the discharge of flue gas of boilers, steelmaking, aluminum smelting, ships and other chemical and non-electric factories with coal, and the specific treatment process is as follows:
ammonia gas is quantitatively added into the reaction tower 1 through the ammonia adding device 6, and in the use process, raw flue gas enters from the lower part of the reaction tower 1, SO in the flue gas 2 And NOx is first treated with an ammonium sulfite treatment system to obtain fine particulate ammonium sulfite and fed into the reaction tower 1 and an ammonia adding device 6 is fed into NH in the reaction tower 1 3 And (3) reacting to respectively generate ammonium sulfite, ammonium bisulfate and ammonium sulfate. In this process, since the ammonium sulfite powder raw material particles are small, the specific surface area in contact with the flue gas entering the reaction tower 1 is large, and thus the denitration efficiency is high. On the other hand, fine-grained ammonium sulfite is more sensitive to temperature, and when the temperature is too high, the fine-grained ammonium sulfite is rapidly decomposed into SO 2 And NH 3 Therefore, the temperature in the reaction column 1 is generally controlled to 60 to 90 ℃. The flue gas at the outlet of the reaction tower 1 is mixed with solid powdery materials of ammonium sulfate and ammonium bisulfate generated by reaction and SO generated by decomposing ammonium sulfite 2 And NH 3 And SO carried by the raw flue gas 2 And NH added by ammonia adding device 6 3 The former solid particles are one of the denitrification byproducts and cannot be recycled, so that the former solid particles need to be collected by a later solid particle collecting device 2. While the latter component is mainly SO 2 And NH 3 After the temperature of the two gaseous substances is lower than 70 ℃, the two gaseous substances start to react to generate ammonium sulfite. Therefore, after the flue gas discharged from the reaction tower 1 passes through the solid particle supplementary collection device 2, the flue gas enters the condensation dust remover 3, low-temperature circulating water or other low-temperature refrigerants are led into the coil pipe in the condensation dust remover 3, after the flue gas contacts with the flue gas, the refrigerating capacity can be reduced to be lower than 60 ℃ so that a large amount of ammonium sulfite particles are generated, meanwhile, because of supersaturation of water vapor, condensation water is separated out on the inner wall surface of the whole condensation dust remover 3 to form a liquid film, the solubility of ammonium sulfite is extremely high, once the liquid film contacts, the liquid film is dissolved into the liquid film, and the rotating motion of the flue gas in the condensation dust remover 3 also enables the particles to be capable of being adhered to the wall surface due to centrifugation, so that the trapping of the ammonium sulfite particles is accelerated. The condensate flowing out of the bottom of the condensate dust collector 3 contains a large amount of ammonium sulfite components and part of ammonium bisulfide, and both components can be recycled, so that the components are converged into the subsequent regulating tank 5. In the flue gas passing through the condensing dust separator 3, there may also be small fugitive ammonium sulfite particles and excess NH 3 This part of the components cannot be directly discharged, and thus, the components are treated by the subsequent flue gas post-treatment device 4 and then discharged normally. Wherein, the regulating tank 5 is used as a collecting, storing and component regulating unit of the ammonium sulfite aqueous solution, and when the content of the ammonium bisulfate component is excessive in Chi Naya, the ammonium bisulfate is regenerated into ammonium sulfite by supplementing ammonia into the regulating tank 5. When the liquid level of the regulating tank 5 reaches the highest liquid level, the extraction of the ammonium sulfite component is started, and the specific steps are as follows: firstly, relatively dilute solution in the regulating tank 5 enters an ammonium sulfite precipitation system to process precipitated crystals (ammonium sulfite), then is dried and processed into loose fine particle powder through the ammonium sulfite processing system, and then is sent into a reaction tower 1 as ammonium sulfite raw material to continue reaction, so that the ammonium sulfite is recoveredAnd regenerating. It should be noted that: in the raw flue gas SO 2 When the concentration is low, ammonia and SO 2 The amount of ammonium sulfite produced by the reaction is relatively small, and the ammonium sulfite denitration product is ammonium sulfate, so that the component loses the capacity of regeneration again, and therefore, a small amount of ammonium sulfite needs to be additionally supplemented into the reaction tower 1 in the running process of the system so as to maintain the denitration reaction. But in raw flue gas SO 2 At high concentration, NH 3 With SO in flue gas 2 The reaction produces a large amount of ammonium sulfite, and the part of ammonium sulfite not only can meet the amount of ammonium sulfite required by denitration, but also can remain, and at the moment, part of ammonium sulfite can be removed from a storage bin at regular time. This portion of the ammonium sulfite can be used as a high value byproduct for other industrial uses.
The supplementary ones are: in this example, the equation involved in the reaction process in the reaction column 1 is as follows:
the reaction equation is as follows:
1)SO 2 with NH 3 Reaction to give (NH) 4 ) 2 SO 4 The reaction equation is as follows:
SO 2 +2NH 3 +H 2 O＝(NH4) 2 SO 3
2)(NH4) 2 SO 3 with SO 2 The further reaction:
(NH 4 ) 2 SO 3 +SO 2 +H 2 O＝2(NH 4 )HSO 3
3) Section (NH 4) 2 SO 3 By O in flue gas 2 Oxidizing:
2(NH 4 )2SO 3 +O 2 ＝2(NH 4 ) 2 SO 4
4) Part (NH) 4 )HSO 3 By O in flue gas 2 Oxidizing:
2NH 4 HSO 3 +O 2 ＝2NH 4 HSO 4
the denitration part adopts ammonium sulfite to react with NOx to generate N 2 The reaction is designed as follows:
1) NO is replaced by O in flue gas 2 Oxidation to NO 2
2NO+O 2 ＝2NO 2
2) Reacting (NH 4) 2SO3 with NO under the action of catalyst to generate N 2
2(NH 4 ) 2 SO 3 +2NO＝(NH 4 ) 2 SO 4 +N 2
3)(NH4) 2 SO 3 With NO 2 Reacting under the action of catalyst to generate N 2
4(NH 4 ) 2 SO 3 +2NO 2 ＝4(NH 4 ) 2 SO 4 +N 2
4)(NH 4 ) 2 SO 3 Pyrolysis of
(NH 4 ) 2 SO 3 .H 2 O＝2NH 3 +SO 2 +H 2 O
Therefore, the flue gas outlet of the reaction tower 1 contains both ammonium sulfate and ammonium bisulfate solid powder generated by the reaction and NH generated by decomposition of ammonium sulfite 3 And SO 2 And SO carried by the raw flue gas 2 And NH added by ammonia adding device 3 。
In this embodiment, in order to ensure uniform gas-solid mixing in the reaction tower 1 and prevent the phenomena of drift and short flow of materials and flue gas, a pore plate, a hood and other tower internals beneficial to gas-solid mixing can be added in the tower.
In this embodiment, the solid particle supplementary collection device 2 is a bag-type dust collector, and the specific model is flexibly and reasonably selected according to actual use requirements. The bag-type dust collector is used for removing ammonium sulfate generated by denitration in the reaction tower 1, and the internal temperature is required to be higher than 60 ℃, so that on one hand, the problem of pasting a bag caused by water vapor condensation is avoided, and on the other hand, the huge specific surface area of the bag-type dust collector can be used as a second place for desulfurization and denitration reaction.
In the embodiment, the condensing dust collector 3 is formed by optimizing common cyclone dust collection, and has the functions of cooling a heat exchanger and cyclone dust collection. On the one hand, by inputting the refrigerant, the temperature is loweredLow flue gas temperature, SO that SO in flue gas 2 And NH 3 And on the other hand, the flue gas generates rotary centrifugation when passing through the device, so that the generated ammonium sulfite particles are enriched on the outer wall surface of the condensation dust remover 3 and are fused into a condensate liquid film formed by cooling of the condensation dust remover 3, and flow into a subsequent regulating tank 5 after being collected.
In this embodiment, the flue gas post-treatment device 4 is a water scrubber, and a liquid outlet of the water scrubber is connected to the adjusting tank 5. Wherein the flue gases coming out of the condensation scrubber 3 (possibly with small fugitive ammonium sulfite particles and excess NH 3 ) And the flue gas enters a water washing tower and is sprayed by the water washing tower or is subjected to gas-liquid contact washing by a packing layer, so that the final purification is realized, and the emission requirement is met. The circulating liquid in the water scrubber can be maintained at a constant concentration while controlling a constant discharge flow rate and a constant amount of water to be replenished. This part of the circulating liquid is also finally led into the regulating reservoir 5.
It should be noted that: the water scrubber belongs to the equipment in the prior art, and specific models are flexibly and reasonably selected according to actual use requirements, and are not described in detail herein.
In this embodiment, the adjusting tank 5 is used for collecting the condensate of the condensing dust collector 3 and the ammonium sulfite solution from the water scrubber, and generally requires a volume capable of continuously collecting the collected solution for more than 4 hours, so as to avoid continuous low-load operation or frequent intermittent start-stop of the subsequent processing unit.
In this embodiment, the bottom of the adjusting tank 5 is connected with an ammonia adding pipe with a valve, and the ammonia adding pipe is connected with an ammonia source. When the proportion of ammonium bisulfate in solution ions in the regulating tank 5 exceeds 10 percent (which can be set by itself) in the analysis and assay, ammonia can be introduced into the regulating tank 5 through an ammonia adding pipeline, and the ammonium bisulfate in the solution in the regulating tank 5 can be reacted to generate ammonium sulfite by supplementing the ammonia.
In a preferred embodiment, the ammonium sulfite precipitation system includes a liquid concentrating device 71, a cooling crystallizer 72, and a liquid filtering device 73, wherein an inlet of the liquid concentrating device 71 is connected to the regulating tank 5, an outlet thereof is connected to an inlet of the cooling crystallizer 72, a slurry outlet of the cooling crystallizer 72 is connected to an inlet of the liquid filtering device 73, and a filtrate discharge port of the liquid filtering device 73 is connected to an inlet of the liquid concentrating device 71.
In the above embodiment, the concentrated solution from the liquid concentration device 71 is introduced into the cooling crystallizer 72, cooled and crystallized in the cooling crystallizer 72, specifically, the ammonium sulfite is supersaturated in the cooling crystallizer 72 to precipitate in a crystal form, the cooling crystallizer 72 can lower the saturated solution or supersaturated mixed solution of 50 ℃ or more of the low-temperature evaporation Duan Erlai to room temperature or lower, so that the supersaturated ammonium sulfite crystals are sufficiently precipitated, the crystal slurry is introduced into the liquid filtering device 73, the ammonium sulfite crystals are filtered from the crystal slurry, and the filtrate generated in the filtering process needs to be returned to the liquid concentration device 71 for re-concentration. The whole system is simple and reasonable in design, and ammonium sulfite in liquid from the regulating tank 5 can be effectively and rapidly separated out and reused.
In this embodiment, the liquid concentrating apparatus 71 is a flash tank. And after the liquid in the regulating tank 5 enters the flash tank, evaporating and concentrating the slurry which is collected in the regulating tank 5 and is rich in ammonium sulfite by controlling the vacuum degree of the flash tank, wherein the concentration process ensures that the temperature of the concentrated solution in the flash tank is between 50 and 70 ℃. When the concentrate is saturated or supersaturated, the concentrate is discharged into a cooling crystallizer 72 for crystallization, the temperature of the concentrate is gradually reduced from above 50 ℃ to room temperature or forced cooling is adopted to a temperature lower than the room temperature, and a large amount of ammonium sulfite crystals are precipitated in the concentrate in the process. Then enters a liquid filtering device 73 for filtering, the filtrate returns to the flash tank, and the filter residues enter a subsequent ammonium sulfite treatment system for treatment.
In this embodiment, the liquid filtering device 73 is a vacuum belt or a plate-and-frame filter press, and the specific model is flexibly and reasonably selected according to the actual use requirement. The filtrate obtained is returned to the liquid concentration device 71 through a pipeline, and the filtered filter cake enters a subsequent drying system.
As a preferred embodiment, the ammonium sulfite treatment system includes an anaerobic drying device 81 and a grinding device 82, wherein a discharge end of the anaerobic drying device 81 is connected to a feed end of the grinding device 82 through a material feeding device, a discharge end of the grinding device 82 is connected to an ammonium sulfite storage bin 83, a discharge port is provided in the ammonium sulfite storage bin 83, and a discharge port of the ammonium sulfite storage bin 83 is connected to the ammonium sulfite powder inlet through a feeder 84.
In the above embodiment, ammonium sulfite crystals are fed to the anaerobic drying apparatus 81 for drying, and the anaerobic drying apparatus 81 should strictly control the internal oxygen content to prevent oxidation of ammonium sulfite. The dried powder is sent into a grinding device 82 to be ground into loose powder and then enters an ammonium sulfite storage bin 83 to be stored, and the ammonium sulfite powder in the ammonium sulfite storage bin 83 is sent into a reaction tower 1 through an ammonium sulfite powder inlet by a feeding machine 84 when needed, so that the complete procedures of drying, grinding and feeding crystals are realized.
It is emphasized that: SO in flue gas 2 In the case of higher content, the ammonium sulfite produced by adding ammonia gas is sufficient to support the amount of ammonium sulfite required for denitration, and even has balance, so that depending on the flue gas conditions, part of ammonium sulfite material needs to be periodically replenished into the ammonium sulfite storage bin 83, or part of high-value byproduct of ammonium sulfite needs to be output outwards.
In this embodiment, the anaerobic dryer 81 is an anaerobic dryer, and the specific model is selected flexibly and reasonably according to the actual use requirement. The filtered ammonium sulfite crystals are dried by adopting an anaerobic dryer, and are dried in an anaerobic environment below 60 ℃, so that not only is the decomposition of ammonium sulfite avoided, but also the oxidation of ammonium sulfite by oxygen in the air is avoided. The anaerobic dryer is not required to dry the materials to a completely anhydrous state, and only needs to ensure that the water attached to the materials is lower than 5 percent and the materials are loose and not agglomerated. The grinding device 82 can be a Raymond mill or other grinding devices suitable for the property of ammonium sulfite in the market, and the specific model can be flexibly and reasonably selected according to the actual use requirement. The feeder 84 may be an air suction feeder, and pumps the ammonium sulfite powder in the ammonium sulfite bin 83 into the reaction tower 1 along with the air flow.
In this embodiment, the ammonia adding device 6 is a liquid ammonia tank with a valve.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.
In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention.
Claims (10)
1. An ammonia-ammonium sulfite combined desulfurization and denitrification system is characterized in that: including reaction tower (1), solid particle complement device (2), condensation dust remover (3), flue gas aftertreatment device (4), equalizing basin (5), ammonium sulfite educes system and ammonium sulfite processing system, reaction tower (1) is connected with ammonia adding device (6), the flue gas outlet connection of reaction tower (1) the flue gas import of solid particle complement device (2), the flue gas outlet connection of solid particle complement device (2) the import of condensation dust remover (3), the exit linkage of condensation dust remover (3) flue gas inlet of flue gas aftertreatment device (4), condensation dust remover (3) condensate water exit linkage equalizing basin (5), equalizing basin (5) are connected ammonium sulfite educes the system, ammonium sulfite educes the system and is used for separating out the sulfurous acid crystal, ammonium sulfite processing system is used for with the ammonium sulfite crystal that the ammonium sulfite educes the system and processes into dry and loose powder, the bottom of reaction tower (1) is equipped with ammonium sulfite powder entry.
2. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 1, wherein: the solid particle supplementary collection device (2) is a bag-type dust collector.
3. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 1, wherein: the flue gas aftertreatment device (4) is a water scrubber, and a liquid outlet of the water scrubber is connected with the regulating tank (5).
4. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 1, wherein: the bottom of the regulating tank (5) is connected with an ammonia adding pipeline with a valve, and the ammonia adding pipeline is connected with an ammonia source.
5. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 1, wherein: the ammonium sulfite precipitation system comprises a liquid concentration device (71), a cooling crystallizer (72) and a liquid filtering device (73), wherein an inlet of the liquid concentration device (71) is connected with the regulating tank (5), an outlet of the liquid concentration device is connected with an inlet of the cooling crystallizer (72), a crystal slurry outlet of the cooling crystallizer (72) is connected with an inlet of the liquid filtering device (73), and a filtrate discharge port of the liquid filtering device (73) is connected with an inlet of the liquid concentration device (71).
6. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 5, wherein: the liquid concentration device (71) is a flash tank.
7. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 5, wherein: the liquid filtering device (73) is a vacuum belt or a plate-and-frame filter press.
8. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 1, wherein: the ammonium sulfite treatment system comprises an anaerobic drying device (81) and a grinding device (82), wherein the discharge end of the anaerobic drying device (81) is connected with the feed end of the grinding device (82) through a material conveying device, the discharge end of the grinding device (82) is connected with an ammonium sulfite storage bin (83), a discharge hole is formed in the ammonium sulfite storage bin (83), and the discharge hole of the ammonium sulfite storage bin (83) is connected with an ammonium sulfite powder inlet through a feeding machine (84).
9. The ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 8, wherein: the anaerobic dryer (81) is an anaerobic dryer, and the feeding machine (84) is an induced draft feeding machine.
10. An ammonia-ammonium sulfite combined desulfurization and denitrification system according to claim 1, wherein: the ammonia adding device (6) is a liquid ammonia tank.
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