CN111167285A - Flue gas purification system and method - Google Patents
Flue gas purification system and method Download PDFInfo
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- CN111167285A CN111167285A CN202010015534.7A CN202010015534A CN111167285A CN 111167285 A CN111167285 A CN 111167285A CN 202010015534 A CN202010015534 A CN 202010015534A CN 111167285 A CN111167285 A CN 111167285A
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- flue gas
- reaction tower
- storage tank
- circulating fluidized
- gas purification
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- 239000003546 flue gas Substances 0.000 title claims abstract description 81
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000000746 purification Methods 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 53
- 239000000428 dust Substances 0.000 claims abstract description 47
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 37
- 238000003860 storage Methods 0.000 claims abstract description 37
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 33
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 235000011116 calcium hydroxide Nutrition 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims description 28
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 16
- 239000000843 powder Substances 0.000 claims description 12
- 238000005243 fluidization Methods 0.000 claims description 10
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 8
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 8
- 239000002253 acid Substances 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 239000012716 precipitator Substances 0.000 claims 1
- 238000004321 preservation Methods 0.000 claims 1
- 239000000779 smoke Substances 0.000 claims 1
- 238000006477 desulfuration reaction Methods 0.000 abstract description 7
- 230000023556 desulfurization Effects 0.000 abstract description 7
- 238000006115 defluorination reaction Methods 0.000 abstract description 6
- 239000002351 wastewater Substances 0.000 abstract description 5
- 239000002912 waste gas Substances 0.000 abstract description 2
- 239000007788 liquid Substances 0.000 description 35
- 239000007787 solid Substances 0.000 description 24
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 14
- 229910052925 anhydrite Inorganic materials 0.000 description 13
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 11
- 230000006872 improvement Effects 0.000 description 8
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 7
- 239000011575 calcium Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- 229910000029 sodium carbonate Inorganic materials 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 6
- CNLWCVNCHLKFHK-UHFFFAOYSA-N aluminum;lithium;dioxido(oxo)silane Chemical compound [Li+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O CNLWCVNCHLKFHK-UHFFFAOYSA-N 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 229910052642 spodumene Inorganic materials 0.000 description 5
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 238000001354 calcination Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-N hydrofluoric acid Substances F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000007790 solid phase Substances 0.000 description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 2
- 239000007832 Na2SO4 Substances 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
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 2
- 229910001634 calcium fluoride Inorganic materials 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 229910052744 lithium Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000020477 pH reduction Effects 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 241000482268 Zea mays subsp. mays Species 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000013078 crystal Substances 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
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000009751 slip forming Methods 0.000 description 1
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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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
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- 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
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- 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
- B01D53/68—Halogens or halogen compounds
-
- 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
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- 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
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2045—Hydrochloric acid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2047—Hydrofluoric acid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- 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)
Abstract
The invention belongs to the technical field of waste gas treatment, and particularly relates to a flue gas purification system which comprises a dry type reaction tower, a circulating fluidized reaction tower, a slaked lime storage tank, a water tank, a compressed air storage tank, a dust remover, an ash storage and an induced draft fan, wherein the circulating fluidized reaction tower sequentially comprises a Venturi tube and a circulating fluidized bed body from bottom to top, an air outlet of the dry type reaction tower is communicated with an air inlet of the Venturi tube, the slaked lime storage tank is communicated with the Venturi tube, the water tank and the compressed air storage tank are both communicated with the circulating fluidized bed body, the top of the circulating fluidized reaction tower is communicated with the dust remover, the dust remover is communicated with an outlet of the Venturi tube through an air chute, the dust remover is communicated with the ash storage. In addition, the invention also provides a flue gas purification method. Compared with the prior art, the invention improves the desulfurization and defluorination efficiency on the premise of not generating wastewater and secondary pollution.
Description
Technical Field
The invention belongs to the technical field of waste gas treatment, and particularly relates to a flue gas purification system and a flue gas purification method.
Background
The application of spodumene, an industrial ore from which lithium is a major source, in ceramics, metallurgy, porcelain removal, special glass, chemical engineering, and the like is rapidly developing and increasingly expanding. Spodumene is commonly used to produce lithium as a chemical feedstock, for example, by calcining spodumene in a rotary kiln and reacting it with sulfuric acid or the like in an acid kiln.
During the calcination of spodumene in a rotary kiln and the acidification in an acidification kiln, a large amount of tail gas is generated, and the main components of the tail gas are water vapor, oxygen, sulfuric acid mist and SO2Hydrofluoric acid, dust, etc. The temperature of the tail gas reaches about 200 ℃, and the tail gas contains 80kg/h of sulfuric acid mist and SO2The concentration is about 5000-10000 mg/Nm3The hydrogen fluoride concentration is about 400mg/Nm3Dust concentration of about 30mg/Nm3。
In the prior art, the treatment of the tail gas generally adopts a wet method or a dry method, wherein the wet method has the problems of treatment and discharge of waste water and dust-containing wet flue gas; the existing dry method has no problems of treatment and discharge of waste water and wet flue gas, but the contact time of a desulfurizer and tail gas is short, and the mixing is not uniform enough, so that the desulfurization and defluorination efficiency is not ideal.
In view of the above, it is necessary to provide a new flue gas purification system, which can improve the efficiency of desulfurization and defluorination without generating waste water and secondary pollution.
Disclosure of Invention
One of the objects of the present invention is: aiming at the defects of the prior art, the flue gas purification system is provided, and the desulfurization and defluorination efficiency is improved on the premise of not generating waste water and secondary pollution.
In order to achieve the purpose, the invention adopts the following technical scheme:
the utility model provides a flue gas purification system, includes dry-type reaction tower, circulation fluidization reaction tower, lime hydrate storage tank, water tank, compressed air storage tank, dust remover, ash storehouse and draught fan, circulation fluidization reaction tower is by including venturi and the circulation fluidization bed body in proper order on going, the gas outlet of dry-type reaction tower with venturi's air inlet intercommunication, the lime hydrate storage tank with venturi intercommunication, the water tank with the compressed air storage tank all with circulation fluidization bed body intercommunication, the top of circulation fluidization reaction tower with the dust remover intercommunication, the dust remover pass through the air chute with venturi's export intercommunication, the dust remover pass through the storehouse pump with ash storehouse intercommunication, the dust remover still with the draught fan intercommunication.
As an improvement of the flue gas purification system, a nozzle is arranged in the circulating fluidized reaction tower, and the output end of the water tank and the output end of the compressed air storage tank are both connected with the nozzle. The nozzle in the circulating fluidized reaction tower adopts an inlet atomizing nozzle, so that good humidifying and activating effects are ensured, and the device is anti-blocking and wear-resistant. The flue gas temperature is controlled flexibly, quickly and accurately.
As an improvement of the flue gas purification system, the dust remover comprises a settling chamber, a filter bag and a dust hopper, flue gas sequentially passes through the settling chamber and the filter bag, the dust hopper is positioned at the bottoms of the settling chamber and the filter bag, and a steam heating and heat insulation device is arranged on the dust hopper. The dust remover is internally provided with the pre-settling chamber, so that the dust removal load and the abrasion of the filter bag are reduced, and the service life of the filter bag is prolonged.
As an improvement of the flue gas purification system, the air chute is connected to the bottom of the ash hopper, a flow control valve is arranged on the air chute, and the air chute is also connected with a fan for providing fluidizing gas.
As an improvement of the flue gas purification system, the compressed air storage tank is also communicated with the output end of the Venturi tube.
As an improvement of the flue gas purification system of the present invention, the flue gas purification system further comprises an injection pump, and the slaked lime storage tank is connected with the venturi tube through the injection pump.
The second purpose of the invention is: a flue gas purification method is provided, which comprises the following steps:
s1, introducing the high-temperature flue gas into a dry reaction tower, and reacting the high-temperature flue gas with superfine sodium bicarbonate powder sprayed in the dry reaction tower to primarily remove acid gas in the flue gas; wherein, the superfine sodium bicarbonate powder is prepared by grinding sodium bicarbonate with the purity of about 95 percent into powder with the particle size of about 800 meshes by a grinder and then blowing the powder into a dry reaction tower through pneumatic conveying;
s2, introducing the flue gas obtained in the step S1 into the circulating fluidized bed body from the inlet of the venturi tube, and reacting the flue gas with slaked lime conveyed into the circulating fluidized bed body from a slaked lime storage tank to further remove acid gas in the flue gas;
and S3, feeding the flue gas obtained in the step S2 into a dust remover, feeding the flue gas subjected to dust removal into a chimney through a draught fan, discharging, returning part of ash to the circulating fluidized bed body through an air chute, and pumping part of ash to an ash silo through a bin.
As an improvement of the flue gas purification method, in step S2, the mass ratio of the slaked lime to the S in the flue gas is 1.3-1.5.
As an improvement of the flue gas purification method of the present invention, in step S2, during the reaction of the flue gas and the slaked lime, the water output from the water tank is atomized by the compressed air output from the compressed air storage tank and then sprayed into the circulating fluidized bed body to reduce the temperature in the circulating fluidized bed body.
As a modification of the flue gas cleaning method of the present invention, in step S3, the flow of flue gas in the dust collector is less than 0.8 m/min.
Compared with the prior art, the invention at least has the following beneficial effects:
1) in the invention, in the dry reaction tower, the sprayed superfine sodium bicarbonate powder is activated by high-temperature flue gas, the popcorn effect is exploded, the volume is increased, and the sponge-like product with strong activity is generatedOf the porous structure of (A) and simultaneously decomposed into Na2CO3、CO2And water with high reactivity and adsorption activity, and acidic Substances (SO) in the flue gas2HCl, HF, etc.) to perform rapid and efficient reaction, and has good desulfurization and defluorination efficiency. And the dry reaction tower runs in a full dry state, so that the problems of wastewater treatment and discharge, wet tailing and dust-containing wet flue gas discharge and the problems of treatment such as oxidation, dehydration and the like of the desulfurized gypsum and secondary pollution are solved.
2) In the invention, in a circulating fluidized reaction tower, flue gas enters a circulating fluidized bed body after being accelerated by a venturi tube, a gas-solid phase and a gas-solid phase are in violent turbulence and mixed under the action of airflow and are in full contact with each other, floccules are continuously formed and return downwards in the process of rising, and the floccules are continuously disintegrated and are lifted by the airflow again in the violent turbulence, so that the slip speed between the gas and the solid is as high as tens of times of the slip speed of single particles. Therefore, the gas-solid two-phase flow mechanism in the circulating fluidized bed greatly strengthens the mass transfer and heat transfer between gas and solid, and provides a fundamental guarantee for realizing high pollutant removal rate. The temperature in the circulating fluidized reaction tower is controlled to be at the optimal reaction temperature by spraying water, so that the best gas-solid turbulent mixing is achieved, and the new surface of the unreacted slaked lime is continuously exposed; in addition, in the rising process of the flue gas, one part of particles are taken out of the circulating fluidized reaction tower along with the flue gas, and one part of particles flow back into the circulating fluidized bed body again due to the self weight, so that the bed layer particle concentration of the fluidized bed body is further increased, and the reaction time of the absorbent (slaked lime) is prolonged. Thereby greatly improving the utilization rate and deacidification efficiency of the absorbent (slaked lime). In addition, the flow velocity of the flue gas in the tower above the Venturi tube is 5-6 m/s, the height of the tower above the Venturi tube is about 20m, so that the gas-solid contact time of the flue gas in the tower is about 4-5 seconds, and the deacidification efficiency is effectively ensured.
3) The invention has high desulfurization efficiency, can easily meet the current special emission limit value requirement and can realize stricter ultra-low emission requirement (SO) in the future2≤30mg/Nm3Dust is less than or equal to 10mg/Nm3) (ii) a And of the inventionThe purification system basically does not generate temperature drop, the exhaust gas temperature is high, the exhaust gas can be directly discharged from an original chimney, high-temperature dry flue gas is discharged, and the conditions of aerosol generation are avoided.
4) The purification system of the invention runs in a totally-closed way, has no dust generating point and is friendly to the surrounding environment.
5) The invention has simple process system, reliable and durable equipment, low failure rate, long service life and 100 percent of synchronous operation rate; the process flow is simple, the operation and the maintenance are convenient, the controllability is good, and the automation degree is high.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Wherein: 1-a dry reaction tower, 2-a circulating fluidized reaction tower, 3-a slaked lime storage tank, 4-a water tank, 5-a compressed air storage tank, 6-a dust remover, 7-an ash storehouse, 8-an induced draft fan, 9-an air chute, 10-a bin pump, 11-a nozzle, 12-a flow control valve, 13-a fan, 14-a jet pump, 21-a venturi tube and 22-a circulating fluidized bed body.
Detailed Description
The present invention will be described in further detail with reference to the following detailed description and the accompanying drawings, but the embodiments of the invention are not limited thereto.
Example 1
As shown in fig. 1, a flue gas purification system comprises a dry reaction tower 1, a circulating fluidized reaction tower 2, a slaked lime storage tank 3, a water tank 4, a compressed air storage tank 5, a dust remover 6, an ash storage 7 and an induced draft fan 8, wherein the circulating fluidized reaction tower 2 sequentially comprises a venturi tube 21 and a circulating fluidized bed 22 from bottom to top, an air outlet of the dry reaction tower 1 is communicated with an air inlet of the venturi tube 21, the slaked lime storage tank 3 is communicated with the venturi tube 21, the water tank 4 and the compressed air storage tank 5 are both communicated with the circulating fluidized bed 22, the top of the circulating fluidized reaction tower 2 is communicated with the dust remover 6, the dust remover 6 is communicated with an outlet of the venturi tube 21 through an air chute 9, the dust remover 6 is communicated with the ash storage 7 through a bin pump 10, and the dust remover 6 is.
Further, a nozzle 11 is arranged in the circulating fluidized reaction tower 2, and the output end of the water tank 4 and the output end of the compressed air storage tank 5 are both connected with the nozzle 11.
Further, the dust collector 6 comprises a settling chamber, a filter bag and a dust hopper, the flue gas sequentially passes through the settling chamber and the filter bag, the dust hopper is positioned at the bottoms of the settling chamber and the filter bag, and a steam heating and heat preserving device is arranged on the dust hopper.
Further, an air chute 9 is connected to the bottom of the ash hopper, a flow control valve 12 is arranged on the air chute 9, and a fan 13 for supplying fluidizing gas is connected to the air chute 9.
Further, the compressed air storage tank 5 is also in communication with the output of the venturi 21.
Further, the present embodiment further comprises an injection pump 14, and the slaked lime storage tank 3 is connected to the venturi tube 21 through the injection pump 14.
Example 2
A method of flue gas purification comprising the steps of:
s1, introducing the high-temperature flue gas into the dry reaction tower 1, and reacting the high-temperature flue gas with the superfine sodium bicarbonate powder sprayed in the dry reaction tower 1 to primarily remove acid gas in the flue gas; wherein, the superfine sodium bicarbonate powder is prepared by grinding sodium bicarbonate with the purity of about 95 percent into powder with the particle size of about 800 meshes by a grinder and then blowing the powder into the dry-type reaction tower 1 by pneumatic transmission;
s2, introducing the flue gas obtained in the step S1 into the circulating fluidized bed body 22 through the inlet of the venturi tube 21, and reacting the flue gas with the slaked lime conveyed into the circulating fluidized bed body 22 from the slaked lime storage tank 3 to further remove acid gas in the flue gas; the mass ratio of the slaked lime to S in the flue gas is 1.3-1.5; in the process of reacting the flue gas with the slaked lime, the water output from the water tank 4 is atomized by the compressed air output from the compressed air storage tank 5 and then sprayed into the circulating fluidized bed body 22, so as to reduce the temperature in the circulating fluidized bed body 22.
S3, enabling the flue gas obtained in the step S2 to enter a dust remover 6, enabling the flow of the flue gas in the dust remover 6 to be lower than 0.8m/min, sending the flue gas subjected to dust removal into a chimney through an induced draft fan 8 to be discharged, enabling part of ash materials to flow back to the circulating fluidized bed 22 through an air chute 9 again, and sending part of ash materials to an ash silo 7 through a silo pump 10.
In step S1, the reaction mechanism involved in the dry reaction column 1 is as follows:
the main reaction:
2NaHCO3(S)＝Na2CO3(s)+H2O(g)+CO2(g)；
SO2(g)+Na2CO3(s)＝Na2SO3(s)+CO2(g)；
partial reaction:
SO2(g)+Na2CO3(s)+O2＝Na2SO4(s)+CO2(g)；
side reaction:
SO3(g)+Na2CO3(s)＝Na2SO4(s)+CO2(g)；
2HCl(g)+Na2CO3(s)＝2NaCl(s)+CO2(g)；
2HF(g)+Na2CO3(s)＝2NaF(s)+CO2(g)。
in steps S2 and S3, the following chemistry is involved:
when the atomized water is atomized in the circulating fluidized reaction tower 2 through the nozzle 11 and fully contacts with the flue gas, the flue gas is cooled and humidified, and the calcium hydroxide powder particles are the same as HCL, HF and H2O、SO2、H2SO3The reaction generates a dry powder product, the whole reaction is divided into three states of gas phase, liquid phase and solid phase, and the reaction steps and the equation are as follows:
⑴SO2is absorbed by the liquid drops;
SO2(gas) + H2O→H2SO3(liquid)
SO of good absorption2Reacting with the absorbent of the solution to generate calcium sulfite, calcium chloride and calcium fluoride;
Ca(OH)2(liquid) + H2SO3(liquid) → CaSO3(liquid) +2H2O
Ca(OH)2(solid) + H2SO3 (liquid) → CaSO3(liquid) +2H2O
Ca(OH)2+2HCl＝CaCl2+2H2O
Ca(OH)2+2HF＝CaF2+2H2O
sample from the liquid drop CaSO3After saturation, crystallization begins
CaSO3(liquid) → CaSO3(solid)
part of CaSO in solution3Reacts with oxygen dissolved in the liquid drops and is oxidized into calcium sulfate
CaSO3(liquid) +1/2O2(liquid) → CaSO4(liquid)
⑸CaSO4Low (liquid) solubility, and thus, crystal precipitation
CaSO4(liquid) → CaSO4(solid)
sixthly, Ca (OH) which reacts to an unknown object2(solid), and as contained in CaSO3(solid), CaSO4Ca (OH) in (solid)2Humidifying and atomizing.
Ca(OH)2(solid) → Ca (OH)2(liquid)
SO2(gas) + H2O→H2SO3(liquid)
Ca(OH)2(liquid) + H2SO3(liquid) → CaSO3(liquid) +2H2O
CaSO3(liquid) → CaSO3(solid)
CaSO3(liquid) +1/2O2(liquid) → CaSO4(liquid)
CaSO4(liquid) → CaSO4(solid)
unreacted Ca (OH) in the soot removed by the dust separator 62(solid), and as contained in CaSO3(solid), CaSO4Ca (OH) in (solid)2The (solid) is recycled to the circulating fluidized reaction tower 2 for continuous reaction.
Ca(OH)2(solid) → Ca (OH)2(liquid)
SO2(gas) + H2O→H2SO3(liquid)
Ca(OH)2(liquid) + H2SO3(liquid) → CaSO3(liquid) +2H2O
CaSO3(liquid) → CaSO3(solid)
CaSO3(liquid) +1/2O2(liquid) → CaSO4(liquid)
CaSO4(liquid) → CaSO4(solid)
Ca(OH)2(solid), and as contained in CaSO3(solid), CaSO4Ca (OH) in (solid)2Humidifying and atomizing.
Performance testing
The purification system of example 1 and the purification method of example 2 were used to treat the spodumene calcination tail gas, and the content or concentration of each component in the tail gas before and after treatment was recorded to check the reliability of the purification system and the purification method. The test results are shown in table 1.
TABLE 1 test results
As can be seen from the test results in Table 1, the tail gas treated by the purification system and the purification method of the invention has dust and SO2And the removal rate of HF is high. That is, the purification system and the purification method of the present invention have a high desulfurization and defluorination rate.
Variations and modifications to the above-described embodiments may also occur to those skilled in the art, which fall within the scope of the invention as disclosed and taught herein. Therefore, the present invention is not limited to the above-mentioned embodiments, and any obvious improvement, replacement or modification made by those skilled in the art based on the present invention is within the protection scope of the present invention. Furthermore, although specific terms are employed herein, they are used in a generic and descriptive sense only and not for purposes of limitation.
Claims (10)
1. A flue gas purification system is characterized in that: including dry-type reaction tower, circulation fluidization reaction tower, lime hydrate storage tank, water tank, compressed air storage tank, dust remover, ash storehouse and draught fan, circulation fluidization reaction tower is by including venturi and circulation fluidization bed body on going in proper order, dry-type reaction tower's gas outlet with venturi's air inlet intercommunication, the lime hydrate storage tank with venturi intercommunication, the water tank with the compressed air storage tank all with circulation fluidization bed body intercommunication, circulation fluidization reaction tower's top with the dust remover intercommunication, the dust remover pass through the air chute with venturi's export intercommunication, the dust remover pass through the storehouse pump with ash storehouse intercommunication, the dust remover still with the draught fan intercommunication.
2. The flue gas purification system according to claim 1, wherein: and a nozzle is arranged in the circulating fluidized reaction tower, and the output end of the water tank and the output end of the compressed air storage tank are connected with the nozzle.
3. The flue gas purification system according to claim 1, wherein: the dust remover comprises a settling chamber, a filter bag and an ash bucket, smoke passes through the settling chamber and the filter bag in sequence, the ash bucket is positioned at the bottom of the settling chamber and the filter bag, and a steam heating and heat preservation device is arranged on the ash bucket.
4. The flue gas purification system according to claim 3, wherein: the air chute is connected to the bottom of the ash bucket, a flow control valve is arranged on the air chute, and the air chute is further connected with a fan used for providing fluidizing gas.
5. The flue gas purification system according to claim 1, wherein: the compressed air storage tank is also communicated with the output end of the Venturi tube.
6. The flue gas purification system according to claim 1, wherein: the slaked lime storage tank is connected with the Venturi tube through the jet pump.
7. A flue gas purification method using the flue gas purification device according to any one of claims 1 to 6, comprising the steps of:
s1, introducing the high-temperature flue gas into a dry reaction tower, and reacting the high-temperature flue gas with superfine sodium bicarbonate powder sprayed in the dry reaction tower to primarily remove acid gas in the flue gas;
s2, introducing the flue gas obtained in the step S1 into the circulating fluidized bed body from the inlet of the venturi tube, and reacting the flue gas with slaked lime conveyed into the circulating fluidized bed body from a slaked lime storage tank to further remove acid gas in the flue gas;
and S3, feeding the flue gas obtained in the step S2 into a dust remover, feeding the flue gas subjected to dust removal into a chimney through a draught fan, discharging, returning part of ash to the circulating fluidized bed body through an air chute, and pumping part of ash to an ash silo through a bin.
8. The flue gas purification method according to claim 7, wherein: in step S2, the mass ratio of the slaked lime to the S in the flue gas is 1.3-1.5.
9. The flue gas purification method according to claim 7, wherein: in step S2, during the reaction between the flue gas and the slaked lime, the water output from the water tank is atomized by the compressed air output from the compressed air storage tank and then sprayed into the circulating fluidized bed to lower the temperature in the circulating fluidized bed.
10. The flue gas purification method according to claim 7, wherein: in step S3, the flow of flue gas in the precipitator is less than 0.8 m/min.
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| CN109621646A (en) * | 2019-01-31 | 2019-04-16 | 王脯胜 | A kind of kiln gas defluorinate desulfurization and dust-removal method and equipment |
| CN209271156U (en) * | 2018-12-06 | 2019-08-20 | 邵嫩飞 | A kind of flue gas purification system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4590046A (en) * | 1983-06-14 | 1986-05-20 | Sydkraft Ab | Method for the purification of flue gases |
| CN101628201A (en) * | 2009-08-19 | 2010-01-20 | 福建龙净脱硫脱硝工程有限公司 | Clearing device for smoke pollutants of glass kiln and clearing method thereof |
| CN205650074U (en) * | 2016-05-24 | 2016-10-19 | 绿色动力环保集团股份有限公司 | Domestic waste burns combination deacidification dust pelletizing system of flue gas |
| CN209271156U (en) * | 2018-12-06 | 2019-08-20 | 邵嫩飞 | A kind of flue gas purification system |
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