CN220677256U - PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 Is a device of (2) - Google Patents
PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 Is a device of (2) Download PDFInfo
- Publication number
- CN220677256U CN220677256U CN202322291737.0U CN202322291737U CN220677256U CN 220677256 U CN220677256 U CN 220677256U CN 202322291737 U CN202322291737 U CN 202322291737U CN 220677256 U CN220677256 U CN 220677256U
- Authority
- CN
- China
- Prior art keywords
- flue gas
- particles
- shell
- area
- heat exchange
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 239000003546 flue gas Substances 0.000 title claims abstract description 43
- 239000002245 particle Substances 0.000 claims abstract description 39
- 230000002776 aggregation Effects 0.000 claims abstract description 35
- 230000005494 condensation Effects 0.000 claims abstract description 30
- 238000009833 condensation Methods 0.000 claims abstract description 30
- 238000005054 agglomeration Methods 0.000 claims abstract description 29
- 230000012010 growth Effects 0.000 claims abstract description 23
- 239000003595 mist Substances 0.000 claims abstract description 23
- 239000000428 dust Substances 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000002351 wastewater Substances 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000000034 method Methods 0.000 claims abstract description 13
- 238000000889 atomisation Methods 0.000 claims abstract description 12
- 239000000498 cooling water Substances 0.000 claims description 20
- 239000012530 fluid Substances 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 238000004220 aggregation Methods 0.000 claims description 6
- 239000013618 particulate matter Substances 0.000 claims description 5
- 230000001502 supplementing effect Effects 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 230000007797 corrosion Effects 0.000 claims description 2
- 238000005260 corrosion Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 238000005507 spraying Methods 0.000 claims 1
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 abstract description 52
- 239000010419 fine particle Substances 0.000 abstract description 23
- 230000009471 action Effects 0.000 abstract description 5
- 239000002253 acid Substances 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 4
- 230000007704 transition Effects 0.000 abstract description 4
- 239000012808 vapor phase Substances 0.000 abstract description 4
- 230000001808 coupling effect Effects 0.000 abstract description 2
- 230000005484 gravity Effects 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 230000002195 synergetic effect Effects 0.000 abstract 1
- 239000003344 environmental pollutant Substances 0.000 description 7
- 231100000719 pollutant Toxicity 0.000 description 7
- 238000005345 coagulation Methods 0.000 description 6
- 230000015271 coagulation Effects 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000002243 precursor Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000009182 swimming Effects 0.000 description 2
- 238000001089 thermophoresis Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 241000700605 Viruses Species 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 239000005427 atmospheric aerosol Substances 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a method for deeply removing PM2.5/CPM/SO from flue gas after wet dust removal 3 The device comprises a condensation agglomeration growth system and a cyclone separator, wherein fine particles, condensable particles and sulfur trioxide in the flue gas after the wet dust removal system sequentially pass through an ultrafine mist atomization area, a condensation heat exchange area and a turbulent agglomeration area, and in the process, the gaseous condensable particles and the sulfur trioxide are cooled and condensed to form small liquid drops, and the fine particles, the particulate condensable particles and the sulfur trioxide are cooled and condensed to form small liquid dropsThe acid mist is condensed and grown under the coupling action of liquid drop trapping, water vapor phase transition and collision agglomeration, part of liquid drops and grown particles are trapped by a liquid film on the surface of the heat exchanger, enter a wastewater recycling device under the action of gravity, and the rest liquid drops and the grown particles enter a cyclone separator to be removed, so that the high-efficiency synergistic removal of fine particles, condensable particles and sulfur trioxide after a wet dust removal system is realized.
Description
Technical Field
The utility model relates to the technical field of dust removal equipment, in particular to a method for deeply removing PM2.5/CPM/SO from flue gas after wet dust removal 3 Is provided.
Background
Fine particulate matter (PM 2.5), condensable Particulate Matter (CPM) and sulfur trioxide (SO) 3 ) Is considered as an important air pollutant in China. The fine particles have small particle size and light weight, can suspend in the atmosphere for a long time, absorb toxic substances such as viruses, heavy metals and the like, and cause serious harm to the atmosphere environment and human health; the condensable particles are gas phase in the flue environment, but leave the flue and enter the atmosphere for cooling and dilution, and then are quickly condensed into a large number of submicron-level fine particles, which are secondary aerosol precursors in the ambient air; the sulfur trioxide is combined with water along with the temperature reduction to form submicron sulfuric acid mist which is difficult to effectively remove, the acid dew point of the flue gas is improved, downstream equipment is corroded, a colored smoke plume phenomenon is caused, the sulfur trioxide is also one of important precursors of atmospheric aerosol, and the safety of the equipment and the atmospheric environment are seriously endangered. In the chemical production processes of metallurgy, petrochemical industry and the like, wet dust collectors (such as spray washing towers, dynamic wave washers and the like) are widely used for controlling the emission of particulate matters. After passing through the wet dust collector, the flue gas reaches a near-saturated high-humidity state and carries pollutants such as non-trapped fine particles, condensable particles, sulfur trioxide and entrained liquid drops. Currently, pollutant emissions are further reduced, mainly by installing a wet electrostatic mist eliminator (WESP) downstream. However, the conventional WESP has the problem of poor charging effect on 0.1-1 mu m particulate pollutants, so that the removal efficiency of fine particles is only 70%; the removal efficiency of the condensable particulates and sulfur trioxide is only about 30-50%.
Patent CN 104258683 discloses a wet electric precipitation system and process based on phase-change coagulation flow equalization technology, which is characterized in that a phase-change coagulation chamber is arranged between a desulfurizing tower and a WESP to cool desulfurized clean flue gas, so that phase-change coagulation growth of fine particles is promoted, and the charging capacity of the fine particles in the subsequent WESP is improved, and high-efficiency removal is realized. However, the condensable water amount obtained by cooling the flue gas is limited, and when the concentration of the particulate matters is high, the particulate matters cannot grow up sufficiently, so that the system can only be applied to clean flue gas after wet flue gas desulfurization of a coal-fired power plant, and the concentration of the particulate matters is only tens of milligrams per cubic meter.
Furthermore, WESP imposes stringent demands on inlet particulate concentration when particulate concentration exceeds 100mg/Nm 3 It is difficult to reach the ultra-low emission standard (10-20 mg/Nm) 3 ) When SO 3 Concentration exceeding 50mg/Nm 3 During the process, the corona electrode discharge is affected, so that the removal efficiency of the system is greatly reduced. The pollution concentration of fine particles, condensable particles, sulfur trioxide and the like after wet dust removal can reach hundreds of milligrams per cubic meter, and can be fluctuant along with the change of working conditions, so that when the ultra-low emission modification in the non-electric industry is comprehensively implemented, a technology for deeply removing the fine particles, the condensable particles and the sulfur trioxide from the flue gas after wet dust removal is necessary to be developed so as to ensure that the flue gas reaches the standard.
Disclosure of Invention
The utility model aims to provide a method for deeply removing PM2.5/CPM/SO from flue gas after wet dust removal 3 Aiming at fine particles, condensable particles and sulfur trioxide discharged after wet dust removal, the technology adopts methods of ultrafine mist atomization, condensation heat exchange, turbulent agglomeration and the like, utilizes the coupling actions of liquid drop trapping, vapor phase transition and collision agglomeration to promote the condensation and growth of the particles, and finally collects dust through a rotating flow field in a cyclone separator to realize the deep removal of the fine particles, the condensable particles and the sulfur trioxide.
In order to achieve the above purpose, the present utility model provides the following technical solutions: PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 The device comprises a condensation agglomeration growth system, wherein the cross section of the main body of the condensation agglomeration growth system is a square shell, the left side of the shell is an inlet, the right side of the shell is an outlet, the inlet and the outlet are both in a horn-shaped structure, the large opening end of the inlet is connected with the shell, and an ultrafine mist atomization area, a condensation heat exchange area and a turbulent agglomeration area are sequentially arranged inside the shell from left to right;
the superfine mist atomization area is internally provided with a plurality of double-fluid atomization nozzles and a cooling water conveying pipeline, the double-fluid atomization nozzles are connected in series by the cooling water conveying pipeline and are uniformly distributed in the superfine mist atomization area side by side, and the spray directions of the double-fluid atomization nozzles are consistent with the flow direction of the flue gas;
the condensing heat exchange area is provided with condensing heat exchange pipes, the condensing heat exchange pipes are uniformly arranged in a plurality of PFA capillaries of the condensing heat exchange area in an S-shaped arrangement mode as a main body, the inlets of the PFA capillaries are connected with cooling water inlets, the outlets of the PFA capillaries are connected with cooling water outlets, the cooling water outlets are positioned at the upstream of the cooling water inlets, the lower parts of the capillaries are provided with wastewater recovery tanks, the wastewater recovery tanks are connected with wastewater tanks, and the wastewater tanks are connected with a water supplementing tank of the wet dust removal system;
a plurality of turbulence generating vortex sheets are arranged in the turbulence agglomeration area, the plurality of turbulence generating vortex sheets are distributed in x rows and y columns, wherein the turbulence generating vortex sheets in x rows and y columns are not less than three, the turbulence generating vortex sheets are of vortex sheet structures with cross sections, the side lengths of the turbulence generating vortex sheets are equal, one side of each cross shape is opposite to the flue gas incoming flow direction, rectangular notches are uniformly arranged on the other three sides of each cross shape, and the height of each turbulence generating vortex sheet is equal to the height of a shell of the agglomeration growth system;
the device also comprises a cyclone separator, wherein the cyclone separator is in a conical cylinder structure, a gas inlet pipe is arranged in the tangential direction of the upper section of the cylinder, the gas inlet pipe of the cyclone separator is tangentially connected with a flue gas outlet of a condensation agglomeration growth system, the top of the cyclone separator is provided with a flow escape pipe, and the bottom of the cyclone separator is provided with a particulate matter collecting bin.
As a preferable mode of the utility model, the median particle diameter of the atomized liquid drops of the two-fluid atomizing nozzles is not more than 10 mu m, the distance between two adjacent two-fluid atomizing nozzles is 100mm-200mm, and the distance between the two-fluid atomizing nozzles positioned at the outermost side and the surface of the shell is 100mm-150mm.
As a preferable mode of the utility model, the pipe diameter of the condensing heat exchange pipe is 6mm-12mm, and the center distance between every two adjacent PFA capillaries is 16mm-30mm.
As a preferred mode of the utility model, the shell liner is a corrosion resistant low surface energy material.
As a preferable mode of the utility model, the single side of the turbulence generating vortex sheet is 30mm-70mm long, the thickness of the plate is 2mm-4mm, the opening depth of the rectangular notch is half of the single side length and the width is 15mm-35mm, the distance between two adjacent rectangular notches is 20mm-40mm, the line distance of the center point of the turbulence generating vortex sheet (10) is 150mm-250mm, and the line distance is 200mm-650mm.
Compared with the prior art, the utility model has the following beneficial effects:
(1) According to the utility model, the double-fluid atomizing nozzle is adopted to generate superfine cold fog drops, the superfine cold fog drops collide with adjacent fine particles to be agglomerated and grow up, and meanwhile, the coating of the liquid film improves the surface wettability of the particles, so that the particles are more easily activated into condensation cores in a supersaturated water vapor environment formed by subsequent heat exchange and cooling; in the turbulent flow agglomeration area, the cold fog drops can be used as agglomeration cores to participate in collision agglomeration of various fine particle pollutants, so that the fine particles are continuously coagulated and grown, the problem that the condensable water amount generated by cooling flue gas is limited is solved by introducing the superfine cold fog drops, and the particle concentration range applicable to the system is improved.
(2) The heat exchanger is adopted to cool saturated wet flue gas, so that a supersaturated water vapor environment can be created, and various fine particle pollutants are caused to undergo phase change condensation and grow; part of granular pollutants can be diffused and deposited to the condensation wall surface under the actions of inertia force, diffusion swimming force, thermophoresis force and the like to be trapped by a condensate film, and flow into a wastewater recycling device along the inner surface of a condensation heat exchange pipe or a condensation agglomeration growth system shell, and the problem of poor trapping agglomeration effect of mist drops on fine particles of 0.1-1 mu m is solved by the occurrence of water vapor phase transition.
(3) According to the utility model, turbulence generating vortex sheets are adopted to generate vortex with different dimensions and dimensions, so that the collision probability among cold fog drops with different masses, fine particulate matters, particulate condensable particulate matters and sulfuric acid trioxide mist is improved.
(4) The utility model uses the heat exchange of the superfine cold fog drops and the condensing pipe to humidify and cool the flue gas, promotes the gaseous condensable particulate matters and sulfur trioxide to generate homogeneous coagulation or the heterogeneous coagulation taking the fine particulate matters and the cold fog drops as the coagulation nuclei to be converted into the particulate state, and the particulate matters are condensed and grown together with the fine particulate matters under the coupling of various actions of liquid drop capturing, water vapor phase transition and collision agglomeration, thereby being beneficial to the removal of the follow-up cyclone separator.
(5) The cyclone separator is adopted to collect the particles after growth, has strong adaptability to the temperature, humidity and dust concentration of the flue gas, and is suitable for the fluctuating high-humidity dust-containing flue gas after wet dust removal. Meanwhile, the particle size and the mass of the particles passing through the agglomeration and growth system are obviously increased, and the defect of poor trapping effect on the fine particles by the traditional cyclone separator is overcome.
Drawings
FIG. 1 is a block diagram of the overall apparatus of the present utility model;
FIG. 2 is a view showing the structure of a turbulence generating vortex sheet according to the present utility model;
FIG. 3 is a front view of a turbulence generating vortex sheet according to the present utility model;
fig. 4 is a right side view of the turbulence generating vortex sheet of the present utility model.
In the figure, 1, a agglomeration growth system; 2. a housing; 3. a two-fluid atomizing nozzle; 4. condensing the heat exchange tube; 5. a cooling water outlet; 6. a cooling water inlet; 7. a wastewater recovery tank; 8. a waste water tank; 9. a water supplementing tank of the wet dust removing system; 10. turbulence generating vortex sheet; 11. a cyclone separator.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Referring to fig. 1-4, the present utility model provides a technical solution: PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 The device comprises a agglomeration growth system 1, and the agglomeration growth systemThe main body of the system 1 is a square shell 2, the left side of the shell 2 is an inlet, the right side of the shell 2 is an outlet, the inlet and the outlet are both in a horn-shaped structure, the large opening end of the inlet is connected with the shell 2, and an ultrafine mist atomization area, a condensation heat exchange area and a turbulent flow agglomeration area are sequentially arranged in the shell 2 from left to right;
a plurality of double-fluid atomizing nozzles 3 and a cooling water conveying pipeline are arranged in the superfine mist atomizing area, the double-fluid atomizing nozzles 3 are connected in series by the cooling water conveying pipeline and are uniformly distributed in the superfine mist atomizing area side by side, and the spray directions of the double-fluid atomizing nozzles 3 are consistent with the flow direction of the flue gas;
the condensing heat exchange area is provided with condensing heat exchange pipes 4, the condensing heat exchange pipes 4 are uniformly arranged in a plurality of PFA capillaries of the condensing heat exchange area in an S-shaped arrangement mode as a main body, the inlets of the capillaries are connected with cooling water inlets 6, the outlets of the capillaries are connected with cooling water outlets 5, the cooling water outlets 5 are positioned at the upstream of the cooling water inlets 6, the lower parts of the capillaries are provided with wastewater recovery tanks 7, the lower parts of the wastewater recovery tanks 7 are connected with wastewater tanks 8, and the wastewater tanks 8 are connected with a wet dust removal system water supplementing tank 9;
a plurality of turbulence generating vortex sheets 10 are arranged in the turbulence aggregation area, the plurality of turbulence generating vortex sheets 10 are distributed in x rows and y columns, wherein the number of the turbulence generating vortex sheets 10 in x rows and y columns is not less than three, each turbulence generating vortex sheet 10 is of a vortex sheet structure with a cross-shaped cross section, the lengths of all sides of the turbulence generating vortex sheets 10 are equal, one side of the cross is opposite to the direction of flue gas incoming flow, rectangular notches are uniformly arranged on the other three sides of the cross, and the height of the turbulence generating vortex sheets 10 is equal to the height of a shell 2 of the aggregation growth system 1;
the device also comprises a cyclone separator 11, wherein the cyclone separator 11 is in a conical cylinder, a gas inlet pipe is arranged in the tangential direction of the upper section of the cylinder, the gas inlet pipe of the cyclone separator 11 is tangentially connected with a flue gas outlet of the condensation agglomeration growth system 1, a flow escape pipe is arranged at the top of the cyclone separator 11, and a particulate matter collecting bin is arranged at the bottom of the cyclone separator 11.
The wastewater tank 8 collects condensate collected by the wastewater recovery tank 7 and waste liquid separated by the cyclone separator 11, and particles in the water are deposited at the bottom of the wastewater tank 8 under the action of gravity sedimentation, so that rare metal raw materials in the condensate and the waste liquid are periodically recovered; the supernatant flows into a water supplementing tank 9 of the wet dust removing system through a baffle plate.
When the device designed according to the scheme is used, the method comprises the following steps: the high-humidity flue gas which is discharged after being treated by the wet dust collector enters a condensation agglomeration growth system 1, firstly, the flue gas is cooled and humidified by partial evaporation of cold fog drops through an ultrafine fog atomization area, gaseous condensable particles and sulfur trioxide are homogeneously coagulated or heterogeneous coagulated by using fine particles and cold fog drops as condensation nuclei, and are converted into a particle state, and meanwhile, the cold fog drops collide with adjacent fine particles, the particle state condensable particles and sulfur trioxide acid mist and are agglomerated and grown under the action of liquid bridging force; in addition, the coating of the liquid film improves the wettability of the particle surface, so that the particles are more easily activated into condensation cores in the subsequent condensation heat exchange area;
step two: the flue gas enters a condensation heat exchange area after passing through an ultrafine mist atomization area, the water quantity of circulating water is controlled, so that the temperature of saturated wet flue gas is reduced, the partial pressure of saturated water vapor is reduced, a supersaturated water vapor environment is formed, gaseous condensable particles and sulfur trioxide in the flue gas are further condensed, heterogeneous condensation occurs on the water vapor by taking fine particles, granular condensable particles and sulfur trioxide mist as condensation nuclei, the particle size is increased, the mass is increased, part of cold mist drops and granular pollutants can migrate to the wall surface of a low-temperature heat exchange pipe under the effects of thermophoresis and diffusion swimming and are trapped by a condensate film, the water quantity of the condensate film on the wall surface is increased by the convergence of the cold mist drops, and the self-cleaning capability of the system is improved;
step three: the flue gas enters a turbulence aggregation area after passing through a condensation heat exchange area, and because of different particle sizes and masses, the movement tracks of the cold fog drops, fine particles, particulate condensable particles and sulfur trioxide acid mist in the flue gas in different scales of vortex flow generated by the turbulence generating vortex sheet 10 are different, so that the collision probability among the particles is improved, and the aggregation and growth of the particles are further promoted;
step four: the flue gas enters the cyclone separator after the condensation, agglomeration and growth system, the fluid drag force suffered by the particles after the condensation and growth is obviously reduced in the rotating flow field, the centrifugal force is improved, the particles are effectively separated and removed, meanwhile, the mist drops are converged on the inner wall of the cyclone separator to form a liquid film, the pressure drop of the system is reduced, the secondary dust emission is reduced, and the particle capturing capacity of the cyclone separator is further enhanced.
Finally, it should be noted that: the foregoing description is only a preferred embodiment of the present utility model, and the present utility model is not limited thereto, but it is to be understood that modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art, although the present utility model has been described in detail with reference to the foregoing embodiments. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (5)
1. PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 Is characterized in that: the device comprises a condensation agglomeration growth system (1), wherein the main body section of the condensation agglomeration growth system (1) is a square shell (2), the left side of the shell (2) is an inlet, the right side of the shell is an outlet, the inlet and the outlet are both in a horn-shaped structure, the large opening end of the inlet is connected with the shell (2), and an ultrafine mist atomization area, a condensation heat exchange area and a turbulent agglomeration area are sequentially arranged inside the shell (2) from left to right;
a plurality of double-fluid atomizing nozzles (3) and a cooling water conveying pipeline are arranged in the superfine mist atomizing area, the double-fluid atomizing nozzles (3) are connected in series by the cooling water conveying pipeline and are uniformly distributed in the superfine mist atomizing area side by side, and the spraying direction of the double-fluid atomizing nozzles (3) is consistent with the flowing direction of the flue gas;
the condensing heat exchange area is provided with condensing heat exchange pipes (4), the condensing heat exchange pipes (4) are uniformly arranged in the condensing heat exchange area in an S-shaped arrangement mode, the inlets of the PFA capillaries are connected with cooling water inlets (6), the outlets of the PFA capillaries are connected with cooling water outlets (5), the cooling water outlets (5) are positioned at the upstream of the cooling water inlets (6), the lower parts of the PFA capillaries are provided with wastewater recovery tanks (7), the lower parts of the wastewater recovery tanks (7) are connected with wastewater tanks (8), and the wastewater tanks (8) are connected with wet dust removal system water supplementing tanks (9);
a plurality of turbulence generation vortex sheets (10) are arranged in the turbulence aggregation area, the turbulence generation vortex sheets (10) are distributed in x rows and y columns, wherein the turbulence generation vortex sheets (10) in x rows and y columns are not less than three, the turbulence generation vortex sheets (10) are of vortex sheet structures with cross sections in cross shapes, the side lengths of the turbulence generation vortex sheets (10) are equal, one side of each cross shape is opposite to the flue gas inflow direction, rectangular notches are uniformly arranged on the other three sides of each cross shape, and the height of the turbulence generation vortex sheets (10) is equal to the height of a shell (2) of the aggregation growth system (1);
the device also comprises a cyclone separator (11), wherein the cyclone separator (11) is in a conical cylinder, a gas inlet pipe is arranged in the tangential direction of the upper section of the cylinder, the gas inlet pipe of the cyclone separator (11) is tangentially connected with a flue gas outlet of the condensation agglomeration growth system (1), a flow escape pipe is arranged at the top of the cyclone separator (11), and a particulate matter collecting bin is arranged at the bottom of the cyclone separator.
2. A method for deeply removing PM2.5/CPM/SO from wet dedusted flue gas according to claim 1 3 Is characterized in that: the median particle size of atomized liquid drops of the two-fluid atomizing nozzles (3) is not more than 10 mu m, the distance between two adjacent two-fluid atomizing nozzles (3) is 100mm-200mm, and the distance between the two-fluid atomizing nozzles (3) located at the outermost side and the surface of the shell (2) is 100mm-150mm.
3. A method for deeply removing PM2.5/CPM/SO from wet dedusted flue gas according to claim 1 3 Is characterized in that: the pipe diameter of the condensation heat exchange pipe (4) is 6mm-12mm, and the center distance between every two adjacent PFA capillaries is 16mm-30mm.
4. A method for deeply removing PM2.5/CPM/SO from wet dedusted flue gas according to claim 2 3 Is characterized in that: the lining of the shell (2) is made of a corrosion-resistant low-surface-energy material.
5. According to claim 1The method is used for deeply removing PM2.5/CPM/SO from the wet dust-removed flue gas 3 Is characterized in that: the single side of the turbulence generation vortex sheet (10) is 30mm-70mm long, the thickness of the plate is 2mm-4mm, the opening depth of the rectangular notch is half of the single side length and the width is 15mm-35mm, the distance between two adjacent rectangular notches is 20mm-40mm, the line distance between the center points of the turbulence generation vortex sheet (10) is 150mm-250mm, and the column distance is 200mm-650mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322291737.0U CN220677256U (en) | 2023-08-24 | 2023-08-24 | PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 Is a device of (2) |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322291737.0U CN220677256U (en) | 2023-08-24 | 2023-08-24 | PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 Is a device of (2) |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220677256U true CN220677256U (en) | 2024-03-29 |
Family
ID=90373515
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322291737.0U Active CN220677256U (en) | 2023-08-24 | 2023-08-24 | PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 Is a device of (2) |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220677256U (en) |
-
2023
- 2023-08-24 CN CN202322291737.0U patent/CN220677256U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105597477B (en) | Remove the device and method of superfine particulate matter in fire coal boiler fume | |
| CN105727669B (en) | Dedusting demister and its application process | |
| WO2016058141A1 (en) | Method and device for dedusting and desulphurizing flue gas | |
| CN205392083U (en) | Ultrafine particle's device in desorption coal fired boiler flue gas | |
| CN106582248B (en) | flue gas wet desulphurization and dust removal integrated device and process | |
| CN104226479A (en) | Efficient wet type electric dedusting and purifying device and method for smoke obtained after wet desulphurization | |
| CN105561776A (en) | Industrial coal-fired boiler flue gas multi-pollutant ultra-low emission and removal cooperated system | |
| CN106621680A (en) | Method and system for deeply removing dust from flue gas after wet desulfurization | |
| CN104667687B (en) | Passive plate rotating vane type dedusting demister and its handling process | |
| CN204582862U (en) | Wet type cyclone electric cleaner and be provided with the desulfurizer of wet type cyclone electric cleaner | |
| CN110652807B (en) | Non-uniform film falling pipe, unit and device applied to falling film dust removal | |
| CN205517261U (en) | Minimum discharge of many pollutants of industry coal fired boiler flue gas is desorption system in coordination | |
| CN109821654B (en) | System and method for deeply removing fine particulate matters/soluble salt/sulfur trioxide in flue gas after wet desulphurization | |
| CN205461770U (en) | Quick circulation of coaxial short distance is semidry method gas cleaning equipment of desorption pollutant in coordination | |
| CN209714650U (en) | The baffle plate type demisting deduster of built-in cooling | |
| CN201105202Y (en) | Device for synergetic removing fine grains in flue gas wet desulfurization | |
| CN108144383A (en) | Flue gas pollutant processing system and processing method, chimney | |
| CN213492812U (en) | Flue gas treatment system | |
| CN204018028U (en) | A kind of high-efficient wet-type electric precipitation purifier of wet-method desulfurized fume | |
| CN203469746U (en) | Wet-process desulphurization system with multi-stage humidifying demisting device | |
| CN210765381U (en) | LT dry dedusting system | |
| CN220677256U (en) | PM2.5/CPM/SO deep removal for wet dedusting flue gas 3 Is a device of (2) | |
| CN104874252B (en) | Multistage multi-cyclone demisting and dedusting device | |
| CN203507747U (en) | Wet-process desulfurization system provided with electrostatic humidifying device | |
| CN110090519A (en) | A kind of flue gas end dehydration refined dedusting device based on phase transformation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |