CN114682049B - Flue gas phase change SO 3 Dust treatment device and method - Google Patents
Flue gas phase change SO 3 Dust treatment device and method Download PDFInfo
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- CN114682049B CN114682049B CN202011603448.4A CN202011603448A CN114682049B CN 114682049 B CN114682049 B CN 114682049B CN 202011603448 A CN202011603448 A CN 202011603448A CN 114682049 B CN114682049 B CN 114682049B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 161
- 239000003546 flue gas Substances 0.000 title claims abstract description 161
- 239000000428 dust Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000008859 change Effects 0.000 title claims description 49
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000001816 cooling Methods 0.000 claims abstract description 68
- 239000000779 smoke Substances 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000003303 reheating Methods 0.000 claims abstract description 17
- 239000002253 acid Substances 0.000 claims abstract description 15
- 230000009471 action Effects 0.000 claims abstract description 14
- 239000003595 mist Substances 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 230000005484 gravity Effects 0.000 claims abstract description 5
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 238000005260 corrosion Methods 0.000 claims description 6
- GHVNFZFCNZKVNT-UHFFFAOYSA-N decanoic acid Chemical compound CCCCCCCCCC(O)=O GHVNFZFCNZKVNT-UHFFFAOYSA-N 0.000 claims description 6
- POULHZVOKOAJMA-UHFFFAOYSA-N dodecanoic acid Chemical compound CCCCCCCCCCCC(O)=O POULHZVOKOAJMA-UHFFFAOYSA-N 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- MFUVDXOKPBAHMC-UHFFFAOYSA-N magnesium;dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MFUVDXOKPBAHMC-UHFFFAOYSA-N 0.000 claims description 6
- XIOUDVJTOYVRTB-UHFFFAOYSA-N 1-(1-adamantyl)-3-aminothiourea Chemical compound C1C(C2)CC3CC2CC1(NC(=S)NN)C3 XIOUDVJTOYVRTB-UHFFFAOYSA-N 0.000 claims description 3
- 239000005632 Capric acid (CAS 334-48-5) Substances 0.000 claims description 3
- 239000004386 Erythritol Substances 0.000 claims description 3
- UNXHWFMMPAWVPI-UHFFFAOYSA-N Erythritol Natural products OCC(O)C(O)CO UNXHWFMMPAWVPI-UHFFFAOYSA-N 0.000 claims description 3
- 239000005639 Lauric acid Substances 0.000 claims description 3
- PWHXJNJAFHXYCX-UHFFFAOYSA-N O.O.O.O.O.O.O.O.B(O)(O)O Chemical group O.O.O.O.O.O.O.O.B(O)(O)O PWHXJNJAFHXYCX-UHFFFAOYSA-N 0.000 claims description 3
- QHFQAJHNDKBRBO-UHFFFAOYSA-L calcium chloride hexahydrate Chemical group O.O.O.O.O.O.[Cl-].[Cl-].[Ca+2] QHFQAJHNDKBRBO-UHFFFAOYSA-L 0.000 claims description 3
- 238000000576 coating method Methods 0.000 claims description 3
- UNXHWFMMPAWVPI-ZXZARUISSA-N erythritol Chemical compound OC[C@H](O)[C@H](O)CO UNXHWFMMPAWVPI-ZXZARUISSA-N 0.000 claims description 3
- 229940009714 erythritol Drugs 0.000 claims description 3
- 235000019414 erythritol Nutrition 0.000 claims description 3
- 229940050906 magnesium chloride hexahydrate Drugs 0.000 claims description 3
- DHRRIBDTHFBPNG-UHFFFAOYSA-L magnesium dichloride hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-] DHRRIBDTHFBPNG-UHFFFAOYSA-L 0.000 claims description 3
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 claims description 3
- 150000004691 decahydrates Chemical class 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 4
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 16
- 230000000694 effects Effects 0.000 description 7
- 230000002087 whitening effect Effects 0.000 description 7
- 239000000443 aerosol Substances 0.000 description 6
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 230000009286 beneficial effect Effects 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- HLZKNKRTKFSKGZ-UHFFFAOYSA-N tetradecan-1-ol Chemical compound CCCCCCCCCCCCCCO HLZKNKRTKFSKGZ-UHFFFAOYSA-N 0.000 description 4
- 238000009827 uniform distribution Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 230000002195 synergetic effect Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 230000006911 nucleation Effects 0.000 description 2
- 238000010899 nucleation Methods 0.000 description 2
- 239000012782 phase change material Substances 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000009856 non-ferrous metallurgy Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 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
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/20—Sulfur; Compounds thereof
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/14—Thermal energy storage
Abstract
The invention discloses a smoke phase-change SO 3 And dust treatment device, this device comprises outer barrel and the interior barrel of coaxial setting, forms an annular space between this outer barrel and the interior barrel, includes: a humidifying section which is positioned at the flue gas inlet and processes the flue gas into a supersaturated state through a humidifier; the cooling reheating section is used for primary cooling of the flue gas which enters the annular space after humidification and enters the rotational flow state, and the temperature of the flue gas after primary cooling is above the acid dew point; the cooling and reheating section heats the flue gas before the treated flue gas is discharged into the atmosphere; a deep cooling section for performing secondary cooling on the flue gas subjected to primary cooling, wherein the temperature of the flue gas subjected to secondary cooling is reduced to be below the acid dew point, SO that SO 3 Forms sulfuric acid mist drops with water vapor in the flue gas and/or forms SO on the outer surface of the deep cooling section component 3 And dust particles are combined with the liquid film to form dust-containing sulfuric acid, and sulfuric acid mist drops and/or dust-containing sulfuric acid are separated out under the centrifugal force and gravity action of rotational flow. The device and the method of the invention not only can effectively remove SO in the flue gas 3 And dust, and can effectively eliminate white smoke.
Description
Technical Field
The invention relates to the technical field of flue gas treatment, in particular to a flue gas phase-change SO 3 And a device and a method for dust treatment and whitening and demisting in a synergic way.
Background
In the operation process of a coal-fired power plant in the power industry, 0.5-1.5% of sulfur in a general boiler is oxidized into sulfur trioxide; in chemical production, the generated high-temperature flue gas generally contains 3.2-8.7% of sulfur dioxide; for heavy nonferrous metallurgy, the conversion rate is generally 6-10%; under the condition of oxygen-enriched regeneration, sulfur trioxide in catalytic cracking regenerated flue gas accounts for 5-10% of the total amount of sulfur oxides in the refining industry; the discharge amount of sulfur trioxide in sintering flue gas in the steel industry accounts for 1-2% of the discharge amount of total sulfur oxides.
SCR technology is commonly used for removing NO in flue gas during flue gas denitration x SCR catalyst contains an active component V 2 O 5 ，V 2 O 5 In the catalytic reduction of NO x At the same time will also convert SO 2 Oxidation to SO 3 About 0.5 to 1.5% SO in the SCR reactor 2 Conversion to SO 3 SO, especially when the SCR reactor is operated at low load 2 Conversion to SO 3 The conversion of (c) increases dramatically.
The sulfur trioxide has strong corrosiveness, part of the sulfur trioxide can be combined with water vapor in the flue gas to form sulfuric acid, and the sulfuric acid is condensed on the surface of a metal part at the dew point temperature, so that corrosion perforation of subsequent waste heat boilers, CO boilers, air pre-heaters and other equipment is caused, and long-period operation of the device is influenced. Sulfur trioxide can react with escaped ammonia of an SCR denitration system to generate ammonium bisulfate with viscosity, a large amount of generated ammonium bisulfate is deposited in a catalyst pore canal at low temperature, fly ash is adhered to the catalyst pore canal to easily cause blocking of the catalyst pore canal so as to reduce the activity of the catalyst, and the sulfur trioxide can enter downstream equipment such as a subsequent waste heat boiler, a CO boiler, an air preheater and the like along with flue gas and is adhered to the surface of a heat exchange element, so that ash deposition, scaling, blocking and corrosion are caused. In addition, in order to avoid dew point corrosion of sulfur trioxide in the flue gas, the exhaust gas temperature is generally higher, the exhaust gas temperature of the regenerated flue gas of the catalytic cracking device is even up to 180 ℃,causing great waste of flue gas heat. SO exiting the stack 3 Will form H with the water vapor in the atmosphere 2 SO 4 Aerosol, while H 2 SO 4 The aerosol is a precursor of the PM2.5 in the air pollution area, is one of the basic factors causing haze, can be inhaled into alveoli by a human body, is deposited in the human body and is difficult to discharge, so that the aerosol has great harm to the health of the human body.
When containing gaseous SO 3 When the flue gas passes through the wet flue gas desulfurization system, the flue gas is rapidly cooled to be below the acid dew point SO 3 Submicron H which is difficult to trap is rapidly formed through homogeneous nucleation and heterogeneous nucleation with particulate matters as condensation nuclei 2 SO 4 An aerosol. In general, larger droplets of particles in the flue gas are removable by the absorber, but for submicron levels of H 2 SO 4 Aerosol, absorption tower is unable to form H 2 SO 4 Submicron aerosol can only be discharged into the atmosphere through a chimney, and a blue smoke phenomenon is formed at the chimney opening.
Therefore, there is a need for a flue gas phase change SO 3 And dust treatment synergistic whitening and demisting device and method, SO that SO is removed from flue gas 3 And in the dust process, the effects of eliminating white smoke and demisting are achieved, and the requirements of emission standards are met.
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information forms the prior art already known to a person of ordinary skill in the art.
Disclosure of Invention
The invention aims to provide a flue gas phase change SO 3 And the dust treatment device and the dust treatment method not only can effectively remove SO in the flue gas 3 And dust, and can also effectively solve the technical problem of eliminating white smoke.
To achieve the above object, according to a first aspect of the present invention, there is provided a flue gas phase change SO 3 The dust treatment device consists of an outer cylinder and an inner cylinder which are coaxially arranged, an annular space is formed between the outer cylinder and the inner cylinder, and the dust treatment device comprises a dust treatment device bodyThe method comprises the following steps: a humidifying section which is positioned at the flue gas inlet and processes the flue gas into a supersaturated state through a humidifier; the cooling reheating section is used for primary cooling of the flue gas which enters the annular space after humidification and enters the rotational flow state, and the temperature of the flue gas after primary cooling is above the acid dew point; the cooling and reheating section heats the flue gas before the treated flue gas is discharged into the atmosphere; a deep cooling section for performing secondary cooling on the flue gas subjected to primary cooling, wherein the temperature of the flue gas subjected to secondary cooling is reduced to be below the acid dew point, SO that SO 3 Forms sulfuric acid mist drops with water vapor in the flue gas and/or forms SO on the outer surface of the deep cooling section component 3 And dust particles are combined with the liquid film to form dust-containing sulfuric acid, and sulfuric acid mist drops and/or dust-containing sulfuric acid are separated out under the centrifugal force and gravity action of rotational flow.
Further, in the above technical scheme, the device can also include the defogging section, and this defogging section is equipped with the defroster, and this defroster is located the entrance of inner tube body bottom.
Further, in the above technical solution, the cooling and reheating section may be provided with a plurality of layers of first heat pipes, a heat absorption end of the first heat pipe is located in the annular space, and a heat release end of the first heat pipe is located in the inner cylinder; the first heat pipe is annularly arranged along the axis of the outer cylinder body and is internally filled with a first phase change medium. The first phase change medium may be boron hydroxide octahydrate, magnesium nitrate hexahydrate, magnesium chloride hexahydrate, erythritol, or the like.
Further, in the above technical solution, the multiple layers of the first heat pipes may be arranged in a staggered manner or vertically along the longitudinal direction.
Further, in the above technical solution, the cryogenic section may be provided with a plurality of layers of second heat pipes, the heat absorption end of the second heat pipe is located in the annular space, and the heat release end of the second heat pipe is located outside the outer cylinder; the second heat pipe is annularly arranged along the axis of the outer cylinder body and is internally filled with a second phase change medium. The second phase change medium may be calcium chloride hexahydrate, capric acid, sodium sulfate decahydrate, zinc nitrate hexahydrate, tetradecanol, lauric acid, or the like.
Further, in the above technical solution, the multiple layers of the second heat pipes may be arranged in a staggered manner or vertically along the longitudinal direction.
Furthermore, in the technical scheme, the heat absorption end surface of the second heat pipe, the inner surface of the outer cylinder and the outer surface of the inner cylinder at the corresponding positions of the deep cooling section are coated with anti-corrosion coatings.
Further, in the technical scheme, the flue gas enters from the annular space at the top of the outer cylinder body and descends spirally, and the flue gas inlet of the outer cylinder body is tangentially arranged.
Further, in the above technical scheme, the bottom of the outer cylinder body can be provided with a trapping liquid outlet.
To achieve the above object, according to a second aspect of the present invention, there is provided a flue gas phase change SO 3 And a dust treatment method comprising the steps of: treating the flue gas at a flue gas inlet to be in a supersaturated state; primary cooling is carried out on the flue gas in a supersaturated and rotational flow state, and the temperature of the flue gas after primary cooling is above the acid dew point; secondary cooling is carried out on the flue gas after primary cooling, and the temperature of the flue gas after secondary cooling is reduced to be below the acid dew point, SO that SO 3 Forms sulfuric acid mist droplets with moisture in the flue gas, and/or causes SO 3 And dust particles are combined with the liquid film to form dust-containing sulfuric acid, and sulfuric acid fog drops and/or dust-containing sulfuric acid are separated out under the centrifugal force and gravity action of rotational flow; and heating the treated flue gas before the treated flue gas is discharged into the atmosphere to eliminate white smoke.
Further, in the above technical solution, a demisting step is further included before the flue gas is subjected to the heating treatment step.
Further, in the above technical solution, the supersaturation degree of the flue gas in the supersaturation state may be 1 to 1.5.
Further, in the technical scheme, the temperature of the flue gas after primary cooling can be reduced to 160-100 ℃.
Further, in the technical scheme, the temperature of the flue gas after secondary cooling can be reduced to 70-30 ℃.
Compared with the prior art, the invention has the following beneficial effects:
1) The flue gas phase change SO of the invention 3 And the dust treatment device and method are based on the phase change technology, and can realize the synergy of SO 3 And dust removal, whitening and defogging;
2) By humidification at the flue gas inletThe treatment of changing the flue gas state is more beneficial to the subsequent SO 3 And dust condensation;
3) The smoke spiral descends by entering the annular space of the inner cylinder body and the outer cylinder body tangentially, the heat transfer effect and the heat transfer efficiency can be enhanced under the action of the rotational flow, and the uniform distribution of the smoke is ensured;
4) The cooling and reheating section can not only cool the entering smoke once, but also heat and whiten the processed smoke which is ready to be discharged into the atmosphere, and has compact structure and strong practicability;
5) The flue gas enters from the annular space and spirally descends, and then enters from the bottom of the inner cylinder body and ascends, SO that the stroke of the flue gas is effectively increased in a compact space, and SO is more beneficial 3 And dust removal, whitening and demisting.
The foregoing description is only an overview of the present invention, and it is to be understood that it is intended to provide a more clear understanding of the technical means of the present invention and to enable the technical means to be carried out in accordance with the contents of the specification, while at the same time providing a more complete understanding of the above and other objects, features and advantages of the present invention, and one or more preferred embodiments thereof are set forth below, together with the detailed description given below, along with the accompanying drawings.
Drawings
FIG. 1 is a flue gas phase change SO of the present invention 3 A perspective view of the dust handling apparatus.
FIG. 2 is a flue gas phase change SO of the present invention 3 A front view of the dust handling apparatus.
FIG. 3 is a flue gas phase change SO of the present invention 3 A top view of an inner cylinder in a dust treatment device.
FIG. 4 is a flue gas phase change SO of the present invention 3 And a front view of an inner cylinder in the dust treatment device.
FIG. 5 is a flue gas phase change SO of the present invention 3 An outer cylinder body top view in a dust treatment device.
FIG. 6 is a flue gas phase change SO of the present invention 3 And an outer cylinder front view in the dust processing device.
The main reference numerals illustrate:
the device comprises a 1-smoke outlet, a 2-outer cylinder, a 3-smoke inlet, a 4-first heat pipe, a 5-humidifier, a 6-second heat pipe, a 61-cryogenic strengthening sleeve, a 7-trapped liquid outlet, an 8-demister and a 9-inner cylinder.
Detailed Description
The following detailed description of embodiments of the invention is, therefore, to be taken in conjunction with the accompanying drawings, and it is to be understood that the scope of the invention is not limited to the specific embodiments.
Throughout the specification and claims, unless explicitly stated otherwise, the term "comprise" or variations thereof such as "comprises" or "comprising", etc. will be understood to include the stated element or component without excluding other elements or other components.
Spatially relative terms, such as "below," "beneath," "lower," "above," "upper," and the like, may be used herein for ease of description to describe one element's or feature's relationship to another element's or feature's in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the article in use or operation in addition to the orientation depicted in the figures. For example, if the article in the figures is turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the elements or features. Thus, the exemplary term "below" may encompass both a direction of below and a direction of above. The article may have other orientations (rotated 90 degrees or other orientations) and the spatially relative descriptors used herein interpreted accordingly.
The terms "first," "second," and the like herein are used for distinguishing between two different elements or regions and are not intended to limit a particular position or relative relationship. In other words, in some embodiments, the terms "first," "second," etc. may also be interchanged with one another.
Device embodiment
As shown in fig. 1 to 5, the flue gas phase change SO of the invention 3 The dust treatment device consists of an outer cylinder body 2 and an inner cylinder body 9 which are coaxially arranged, an annular space is formed between the outer cylinder body 2 and the inner cylinder body 9, and smoke passes through the annular space and is tangentially arranged with the outer cylinder body 2The flue gas inlet 3 of (1) enters an annular space formed by the outer cylinder 2 and the inner cylinder 9, the humidifier 5 is arranged at the flue gas inlet 3 to humidify the flue gas, the humidified flue gas spirally descends, the heat transfer effect and the heat exchange efficiency can be enhanced under the action of swirling flow, and the uniform distribution of the flue gas is ensured. In the annular space, a cooling and reheating section and a cryogenic section are sequentially arranged from top to bottom.
As further shown in fig. 1, 2, 5 and 6, the humidifier 5 is used for changing the state of the flue gas, the humidifier 5 is arranged in the flue gas inlet 3, and the flue gas is humidified to make the supersaturation degree of the flue gas reach 1-1.5, preferably 1.1-1.2.
As further shown in fig. 1-4, the cooling and reheating stage primary cools the humidified, swirling flue gas entering the annular space, the temperature of the primary cooled flue gas being above the acid dew point, and specifically the primary cooling may reduce the flue gas temperature to 160-100 ℃, preferably 150-110 ℃, more preferably 140-120 ℃. As further shown in fig. 1-4, the cooling and reheating section is cooled by the first heat pipe 4, the first heat pipe 4 can be provided with multiple layers, and the heat absorbing end of the first heat pipe 4 is positioned in the annular space for primary cooling of the flue gas. The heat release end of the first heat pipe is positioned in the inner cylinder 9, and the heat release end is used for heating the treated flue gas, so that the flue gas can be heated before the treated flue gas is discharged into the atmosphere, and white smoke can be effectively eliminated. The first heat pipes 4 of the multiple layers are arranged in a staggered manner or vertically along the longitudinal direction (the staggered manner is adopted in the drawing of the invention). The first heat pipe 4 is annularly arranged along the axis of the outer cylinder 2 and is internally filled with a first phase change medium. Preferably, but not by way of limitation, the first phase change medium may be selected from boron hydroxide octahydrate, magnesium nitrate hexahydrate, magnesium chloride hexahydrate, erythritol, and the like.
As further shown in fig. 1, 2, 5 and 6, the flue gas after primary cooling enters a cryogenic section for secondary cooling, and the temperature of the flue gas after secondary cooling is reduced to below the acid dew point, specifically, the temperature of the flue gas is reduced to 70-30 ℃, preferably 60-40 ℃. SO at this stage 3 The dust and the dust are removed in two ways, one way is SO 3 Forms sulfuric acid fogdrops with water vapor in the flue gas, and the sulfuric acid fogdrops are condensed by taking dust particles as condensation materialsThe nuclei are condensed, coalesced, grown and removed under the action of spiral airflow; another way is that the water vapor in the flue gas condenses on the outer pipe wall of the deep cooling section component to form a uniform liquid film, SO 3 And the dust particles are combined with the liquid film to form dust-containing sulfuric acid. The sulfuric acid mist drops and the dust-containing sulfuric acid are removed under the cyclone action. The cryogenic section component is a second heat pipe 6 which is arranged in a multi-layer mode, the heat absorption end of the second heat pipe 6 is located in the annular space, and the heat release end of the second heat pipe 6 is located outside the outer cylinder 2. The layers of the second heat pipes 6 may also be arranged in a longitudinally offset manner or vertically (in an offset manner as shown in the present drawings). In order to achieve a better cooling effect, a deep cooling strengthening sleeve 61 is arranged at the heat release end of the second heat pipe 6 (namely, the heat pipe part outside the outer cylinder 2). The second heat pipe 6 is annularly arranged along the axis of the outer cylinder 2 and is internally filled with a second phase change medium. Preferably, and not by way of limitation, the second phase change medium may be selected from calcium chloride hexahydrate, capric acid, sodium sulfate decahydrate, zinc nitrate hexahydrate, tetradecanol, lauric acid, or the like. The outer tube wall of the second heat tube 6, the inner wall of the outer tube body 2 and the outer wall of the inner tube body 9 are coated with anti-corrosion coatings, and the dust-containing sulfuric acid is condensed at the positions and removed under the action of rotational flow. The separated trapping liquid (namely sulfuric acid mist drops and dust-containing sulfuric acid) is gathered at the bottom of the device and is discharged out of the device through a trapping liquid outlet 7.
As further shown in fig. 1 to 4, the flue gas phase change SO of the present invention 3 And dust treatment device still includes defogging section, and this defogging section is equipped with defroster 8, and defroster 8 is located interior barrel 9 bottom (the flue gas entrance of interior barrel 9). And the flue gas after secondary cooling enters a demister 8 to remove residual liquid. After the demisting operation, the flue gas continues to rise in the inner cylinder 9 and enters the cooling and reheating section again. The gas phase change material at the heat release end of the first heat pipe 4 is condensed and released heat after passing through the cooling and reheating section, so that the smoke is heated, and the smoke saturation is reduced, thereby achieving the purpose of eliminating white smoke. The heated flue gas is discharged into the atmosphere through a flue gas outlet 1 of the inner cylinder.
Method embodiment
The flue gas treatment method of the invention is flue gas phase change SO based on phase change technology 3 Dust treatment synergyThe whitening and demisting method comprises the following steps:
firstly, the flue gas is subjected to humidification treatment to enable the flue gas to be in a supersaturated state; the smoke gas spirally descends in an annular space formed by the outer cylinder body 2 and the inner cylinder body 9, the heat transfer effect and the heat exchange efficiency are enhanced under the action of rotational flow, and the uniform distribution of the smoke gas is ensured; then, the flue gas spirally enters a cooling and reheating section downwards, in the section, phase change substances in the heat absorption end of the first heat pipe 4 are subjected to phase change and heat absorption, the flue gas in a rotational flow state is cooled for the first time, and the temperature of the flue gas after the first cooling is above an acid dew point; then, the flue gas after primary cooling is subjected to secondary cooling, the temperature of the flue gas after secondary cooling is reduced to be below the acid dew point, and in the section, SO 3 And forming sulfuric acid mist drops with water vapor in the flue gas, wherein the sulfuric acid mist drops are condensed by taking dust particles as condensation nuclei, and are coalesced, grown and removed under the action of spiral airflow. At the same time, the water vapor in the flue gas condenses on the outer tube wall of the second heat tube 6 to form a uniform liquid film, SO 3 And dust particles are combined with the liquid film to form dust-containing sulfuric acid, and the sulfuric acid fog drops and the trapping liquid formed by the dust-containing sulfuric acid which is separated out under the swirling action of the flue gas are converged at the bottom of the device and discharged; then, removing entrained liquid drops from the deeply cooled flue gas through a demister 8 at a flue gas inlet at the bottom of an inner cylinder 9; then, the flue gas rises in the inner cylinder 9 and enters the cooling reheating section again, and at the moment, the flue gas contacts with the heat-releasing end of the first heat pipe 4. The gas phase change material at the heat release end of the first heat pipe 4 is subjected to condensation heat release, and the smoke is subjected to heating treatment to eliminate white smoke; finally, the treated flue gas is discharged into the atmosphere.
The flue gas phase change SO of the invention 3 And the dust treatment device and method can realize the synergistic SO removal 3 And dust, whitening and defogging. Changing the state of the flue gas through humidification at the flue gas inlet is more beneficial to the subsequent SO 3 And dust condensation. The flue gas tangentially enters the annular space, the spiral of the flue gas descends, the heat transfer effect and the heat exchange efficiency can be enhanced under the action of the rotational flow, and the uniform distribution of the flue gas is ensured. The cooling and reheating section not only can cool the entering smoke once, but also can heat and whiten the processed smoke to be discharged into the atmosphere, and has compact structureThe practicability is stronger. The flue gas enters from the annular space and spirally descends, and then enters from the bottom of the inner cylinder body and ascends, SO that the stroke of the flue gas is effectively increased in a compact space, and SO is more beneficial 3 And dust removal, whitening and defogging.
The foregoing descriptions of specific exemplary embodiments of the present invention are presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application to thereby enable one skilled in the art to make and utilize the invention in various exemplary embodiments and with various modifications as are suited to the particular use contemplated. Any simple modifications, equivalent variations and modifications of the above-described exemplary embodiments should fall within the scope of the present invention.
Claims (16)
1. Flue gas phase change SO 3 And the dust treatment device, characterized by, by outer barrel and the inner tube body that the coaxial setting is constituteed, form an annular space between this outer barrel and the inner tube body, include:
a humidification section located at the flue gas inlet and treating the flue gas to a supersaturated state by a humidifier;
the cooling and reheating section is used for carrying out primary cooling on the flue gas which enters the annular space in a rotational flow state after humidification, and the temperature of the flue gas after primary cooling is above an acid dew point; the cooling and reheating section heats the treated flue gas before the treated flue gas is discharged into the atmosphere;
the deep cooling section is used for carrying out secondary cooling on the flue gas subjected to primary cooling, a plurality of layers of second heat pipes are arranged in the deep cooling section, the heat absorption ends of the second heat pipes are positioned in the annular space, and the heat release ends of the second heat pipes are positioned outside the outer cylinder; the temperature of the flue gas after secondary cooling is reduced to be below the acid dew point, SO that SO 3 Forming sulfuric acid mist drops with water vapor in the flue gas, and/or at the outer surface of the deep cooling section component, the SO 3 Dust particlesThe particles and the liquid film are combined to form dust-containing sulfuric acid, and sulfuric acid fog drops and/or dust-containing sulfuric acid are separated out under the centrifugal force and gravity action of the rotational flow;
the flue gas enters from the annular space at the top of the outer cylinder body and descends spirally.
2. The flue gas phase change SO of claim 1 3 And the dust treatment device is characterized by further comprising a demisting section, wherein the demisting section is provided with a demister, and the demister is positioned at the inlet of the bottom of the inner cylinder.
3. The flue gas phase change SO of claim 1 3 The dust treatment device is characterized in that the cooling and reheating section is provided with a plurality of layers of first heat pipes, the heat absorption ends of the first heat pipes are positioned in the annular space, and the heat release ends of the first heat pipes are positioned in the inner cylinder; the first heat pipe is annularly arranged along the axis of the outer cylinder body and is internally filled with a first phase change medium.
4. A flue gas phase change SO according to claim 3 3 And the dust treatment device is characterized in that the first phase change medium is boron hydroxide octahydrate, magnesium nitrate hexahydrate, magnesium chloride hexahydrate or erythritol.
5. A flue gas phase change SO according to claim 3 3 And the dust treatment device is characterized in that a plurality of layers of the first heat pipes are arranged in a staggered manner or vertically along the longitudinal direction.
6. The flue gas phase change SO of claim 1 3 And the dust treatment device is characterized in that the second heat pipe is annularly arranged along the axis of the outer cylinder body and is internally filled with a second phase change medium.
7. The flue gas phase change SO of claim 6 3 And a dust treatment device, wherein the second phase change medium is calcium chloride hexahydrate, capric acid, sodium sulfate decahydrate, zinc nitrate hexahydrate, decahydrate, or a mixture thereofTetraol or lauric acid.
8. The flue gas phase change SO of claim 6 3 And the dust treatment device is characterized in that a plurality of layers of the second heat pipes are arranged in a staggered manner or vertically along the longitudinal direction.
9. The flue gas phase change SO of claim 6 3 And the dust treatment device is characterized in that the surface of the heat absorption end of the second heat pipe, the inner surface of the outer cylinder and the outer surface of the inner cylinder at the corresponding positions of the deep cooling section are coated with anti-corrosion coatings.
10. The flue gas phase change SO of claim 1 3 And the dust treatment device is characterized in that the flue gas inlet of the outer cylinder body is tangentially arranged.
11. The flue gas phase change SO of claim 1 3 And the dust treatment device is characterized in that a trapping liquid outlet is arranged at the bottom of the outer cylinder body.
12. Flue gas phase change SO 3 And a dust treatment method, characterized by applying the apparatus according to any one of claims 1 to 11, comprising the steps of:
treating the flue gas at a flue gas inlet to be in a supersaturated state;
primary cooling is carried out on the flue gas in a supersaturated and rotational flow state, and the temperature of the flue gas after primary cooling is above an acid dew point;
the flue gas after primary cooling is subjected to secondary cooling, and the temperature of the flue gas after secondary cooling is reduced to be below the acid dew point, SO that SO 3 Forming sulfuric acid mist droplets with moisture in the flue gas, and/or causing the SO 3 And dust particles are combined with the liquid film to form dust-containing sulfuric acid, and sulfuric acid mist drops and/or dust-containing sulfuric acid are separated out under the centrifugal force and gravity action of rotational flow;
the treated flue gas is subjected to a heat treatment to eliminate white smoke before being discharged into the atmosphere.
13. Flue gas phase change SO according to claim 12 3 And a dust treatment method, characterized in that the flue gas is further provided with a defogging step before the heating treatment step.
14. Flue gas phase change SO according to claim 12 3 And a dust treatment method, characterized in that the supersaturation degree of the flue gas in the supersaturation state is 1-1.5.
15. Flue gas phase change SO according to claim 12 3 And a dust treatment method, which is characterized in that the temperature of the flue gas after primary cooling is reduced to 160-100 ℃.
16. Flue gas phase change SO according to claim 12 3 And a dust treatment method, which is characterized in that the temperature of the flue gas after secondary cooling is reduced to 70-30 ℃.
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Effective date of registration: 20231205 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |