CN118079630B - Flue gas treatment equipment for garbage incineration - Google Patents
Flue gas treatment equipment for garbage incineration Download PDFInfo
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- CN118079630B CN118079630B CN202410374481.6A CN202410374481A CN118079630B CN 118079630 B CN118079630 B CN 118079630B CN 202410374481 A CN202410374481 A CN 202410374481A CN 118079630 B CN118079630 B CN 118079630B
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- flue gas
- reaction tower
- vortex
- plate
- tower body
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 239000003546 flue gas Substances 0.000 title claims abstract description 103
- 238000006243 chemical reaction Methods 0.000 claims abstract description 83
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 51
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 239000007921 spray Substances 0.000 claims abstract description 18
- 238000005507 spraying Methods 0.000 claims abstract description 13
- 238000004056 waste incineration Methods 0.000 claims abstract description 6
- 230000008602 contraction Effects 0.000 claims description 9
- 239000003595 mist Substances 0.000 claims description 3
- 208000002925 dental caries Diseases 0.000 claims description 2
- 239000003517 fume Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 8
- 238000001704 evaporation Methods 0.000 abstract description 7
- 230000008020 evaporation Effects 0.000 abstract description 7
- 230000015572 biosynthetic process Effects 0.000 abstract description 5
- 239000002699 waste material Substances 0.000 abstract description 3
- 230000000694 effects Effects 0.000 description 16
- 239000007789 gas Substances 0.000 description 15
- 239000002002 slurry Substances 0.000 description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 7
- 239000000779 smoke Substances 0.000 description 7
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 6
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 5
- 239000002250 absorbent Substances 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/79—Injecting reactants
-
- 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
-
- 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
- B01D2258/0291—Flue gases from waste incineration plants
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a flue gas treatment device for waste incineration, which relates to the technical field of waste incineration flue gas treatment and comprises a reaction tower body, a flue gas pipe with a downward outlet and a vortex plate, wherein an arc-shaped first guide plate and an arc-shaped second guide plate are arranged above the flue gas pipe, a spray head connected with a deacidification agent pipe and an exhaust pipe are arranged above the two guide plates, the flue gas is sprayed on the arc-shaped vortex plate through spraying the flue gas from the flue gas pipe with the downward outlet, so that the flow direction and the speed of original flue gas are changed, when the flow direction of the original flue gas is changed to be upward, the first guide plate and the second guide plate conduct drainage on the flue gas to form a plurality of small air flow vortices, the contact area and the contact time between the air flow vortices and the deacidification agent are increased, so that the full progress of deacidification reaction is promoted, the formation of the air flow vortices can accelerate the evaporation speed of water molecules in the deacidification agent, and the evaporation process of the deacidification agent is accelerated, and new process waste liquid can not be generated.
Description
Technical Field
The invention relates to the technical field of waste incineration flue gas treatment, in particular to flue gas treatment equipment for waste incineration.
Background
The garbage incineration technology has become an important measure for solving the increasingly serious problem of garbage pollution and relieving the energy crisis at present. However, a great deal of acid gas (such as SO 2, HCl and the like) is generated in the incineration process, SO that research on the waste incineration flue gas purification technology and equipment optimization are paid attention to.
The flue gas purification technology mainly uses a coal-fired flue gas purification method, and generally adopts a semi-dry spray drying absorption method, in the process, waste gas is contacted with a liquid phase absorbent (such as limestone paste) with partial humidity through a deacidification tower, usually a cyclone separator or a sprayer, and the liquid phase absorbent in the deacidification tower is sprayed into the waste gas through a spraying or sprinkling system to react with acid gas to form corresponding salts or water.
Spraying liquid phase absorbent from the top of deacidification tower, in the flue gas is discharged into the deacidification tower from the top of deacidification tower, because the effect of flue gas reflux zone, partial absorbent thick liquid drop that does not evaporate completely is blown to the deacidification tower wall, causes the slagging and the corruption of deacidification tower wall easily, leads to the thermal stress increase that the deacidification tower wall received, is unfavorable for the long-term steady operation of deacidification tower.
Disclosure of Invention
First) solving the technical problems
The invention aims to make up the defects of the prior art and provides a flue gas treatment device for garbage incineration.
Two) technical scheme
In order to achieve the above purpose, the present invention provides the following technical solutions: the utility model provides a fume treatment equipment for msw incineration, includes the reaction tower body, the reaction tower body divide into two cavitys, and one of them cavity is cylindricly, spray deacidification reaction in the cylindric cavity, another cavity is located cylindric cavity directly over to be connected with the blast pipe, include:
the flue gas pipe is arranged at the lower part of the cylindrical cavity of the reaction tower body, and the air inlet direction of the flue gas pipe is vertical to the horizontal plane and downward;
The vortex plate is hemispherical, is fixedly arranged in the reaction tower body and is positioned below the flue gas pipe, the central axis of the vortex plate coincides with the central axis of the cylindrical cavity of the reaction tower body, the spherical center of the vortex plate is close to the air inlet direction of the flue gas pipe, and when the flue gas pipe sprays flue gas downwards in a vertical horizontal plane, the flow direction and the speed of the flue gas are changed after the flue gas is sprayed to the vortex plate;
The second guide plate is fixedly arranged on the inner wall of the cylindrical cavity of the reaction tower body and positioned above the flue gas pipe, and is used for guiding the flue gas to form an airflow vortex in the reaction tower;
the first guide plate is fixedly arranged on the inner wall of the cylindrical cavity of the reaction tower body, is positioned above the second guide plate, is opposite to the direction of the first guide plate, and is used for guiding the flue gas to form an airflow vortex in the reaction tower;
The deacidification agent pipes are symmetrically arranged at the upper part of the reaction tower body;
The spray head is connected to the deacidification agent pipe and positioned inside the reaction tower body and is used for spraying the deacidification agent in the deacidification agent pipe in the reaction tower body in a mist form.
Further, the shortest distance from the central axis of the section of flue pipe perpendicular to the horizontal plane to the inner wall of the cylindrical cavity of the reaction tower body is la, the shortest distance from the central axis of the vortex plate to the inner wall of the cylindrical cavity of the reaction tower body is lb, and in the direction parallel to the horizontal plane, the farthest distance from the central axis of the vortex plate to the boundary of the vortex plate is lc, the value range of lc/lb is 0.45-0.75, and the value range of la/lb is 0.5-0.8.
Further, the first guide plate is located at one end close to the flue gas pipe, and the second guide plate is located at one end far away from the flue gas pipe.
Further, in the direction perpendicular to the horizontal plane, the distance from the first guide plate to the vortex plate is na, and the distance from the second guide plate to the vortex plate is nb, and the value range of nb/na is 0.65-0.8.
Further, at least two V-shaped guide holes are uniformly formed in the edge of the vortex plate, and the V-shaped opening direction of the guide holes is far away from the center of the vortex plate.
Further, four V-shaped guide holes are uniformly formed in the edge of the vortex plate, the central angle of each guide hole is thetaa, the central angle of an arc formed by the surrounding of any two adjacent V-shaped guide holes is thetab, the angle range of thetaa is 8-18 degrees, and the angle range of thetab is 72-82 degrees.
Further, the first guide plate is an arc plate, the central angle of the first guide plate is thetac, the angle range of thetac is 80-100 degrees, the second guide plate is an arc plate, the central angle of the second guide plate is thetad, the angle range of thetad is 80-100 degrees, and a plurality of through holes are respectively formed in the first guide plate and the second guide plate.
Further, the shower nozzle includes pressure pump and nozzle, be connected with three nozzle on the pressure pump, every the nozzle is the slope of angle and sets up on the pressure pump, and the pressure pump is used for getting into three nozzle after pressurizing the deacidification agent in the deacidification agent pipe, and the nozzle sprays the deacidification agent in the reaction tower body, and the deacidification agent carries out deacidification reaction with the flue gas in the reaction tower body.
Further, each nozzle is internally provided with a first conical cavity and a second conical cavity, the central axis of the first conical cavity is coincident with the central axis of the second conical cavity, the height of the first conical cavity is larger than that of the second conical cavity, the central angle of the first conical cavity is smaller than that of the second conical cavity, an expansion section of the first conical cavity is communicated with the pressure pump, a contraction section of the second conical cavity is communicated with a contraction section of the first conical cavity, an expansion section of the second conical cavity is communicated with the end face of the nozzle, away from the pressure pump, when deacidification agent flows through the contraction section of the first conical cavity, the pressure of liquid is increased, and spray is formed in the expansion section of the second conical cavity to be sprayed in the reaction tower body.
Third), beneficial effects:
Compared with the prior art, the invention has the following beneficial effects:
according to the invention, the flue gas is sprayed from the flue gas pipe with the downward outlet, the flue gas is sprayed on the arc-shaped vortex plate, the flow direction and the speed of the original flue gas are changed by limiting the spraying position of the flue gas on the vortex plate and the structure of the vortex plate, when the flow direction of the original flue gas is changed to be upward, the first guide plate and the second guide plate conduct drainage on the flue gas to form a plurality of small air flow eddies, the contact area and the contact time of the air flow eddies with the deacidification agent are increased, so that the full progress of the deacidification reaction is promoted, the evaporation speed of water molecules in the deacidification agent can be accelerated by the formation of the air flow eddies, the evaporation process of the deacidification agent is accelerated, and new process waste liquid can not be generated.
Drawings
FIG. 1 is a front cross-sectional view of the present invention;
FIG. 2 is a schematic view of the gas flow vortex in the body of the reaction column of the present invention;
FIG. 3 is a partial perspective cross-sectional view of the present invention;
FIG. 4 is a top cross-sectional view at A-A of FIG. 1;
FIG. 5 is a top view of a scroll plate according to the present invention;
FIG. 6 is a perspective view of a first baffle according to the present invention;
FIG. 7 is a perspective view of a second baffle according to the present invention;
FIG. 8 is a perspective view of a spray head according to the present invention;
FIG. 9 is a partial perspective cross-sectional view of a sprinkler head according to the present invention;
FIG. 10 is a schematic diagram of a Ca (OH) 2 slurry model;
in the figure: 1. a flue pipe; 2. a reaction tower body; 3. a swirl plate; 4. a support frame; 5. a guide hole; 6. a first deflector; 7. a second deflector; 8. a deacidification agent pipe; 9. a spray head; 10. an exhaust pipe; 11. a pressure pump; 12. a nozzle; 13. a first tapered cavity; 14. a second tapered cavity.
Detailed Description
The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments, and all other embodiments obtained by those skilled in the art without making creative efforts based on the embodiments of the present invention are included in the protection scope of the present invention.
In the description of the present invention, it should be understood that the terms "longitudinal", "transverse", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. indicate orientations or positional relationships based on the drawings, are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
The flue gas treatment equipment for garbage incineration shown in combination with fig. 1 to 9 comprises a reaction tower body 2, wherein the reaction tower body 2 is divided into two cavities, one cavity is cylindrical, spraying deacidification reaction is carried out in the cylindrical cavity, the other cavity is positioned right above the cylindrical cavity and is in a semicircle sphere shape, the central axis of the semicircle sphere cavity is coincident with the central axis of the cylindrical cavity, the semicircle sphere cavity is connected with an exhaust pipe 10, and flue gas after deacidification reaction in the reaction tower body 2 is discharged into a subsequent dust remover from the exhaust pipe 10 above.
Specifically, as shown in fig. 1 to 4, a flue gas pipe 1 is connected to the lower part of the cylindrical cavity of the reaction tower body 2, the gas inlet direction of the flue gas pipe 1 in the reaction tower is vertical to the horizontal plane, and flue gas formed after the garbage incineration treatment is discharged into the reaction tower body 2 from the flue gas pipe 1 for deacidification reaction, wherein the main components of the flue gas are sulfur dioxide (SO 2) and hydrogen chloride (HCl).
As shown in fig. 1 to 5, the vortex plate 3 is in a semicircle sphere shape, a support frame 4 is fixed at the central axis of the inside of the reaction tower body 2, the vortex plate 3 is fixedly connected above the support frame 4, the vortex plate 3 is positioned below the flue gas pipe 1, the central axis of the vortex plate 3 coincides with the central axis of the cylindrical cavity of the reaction tower body 2, the sphere center of the vortex plate 3 is close to the air inlet direction of the flue gas pipe 1, namely, the curved arc end of the vortex plate 3 faces the air inlet direction of the flue gas pipe 1, when the flue gas pipe 1 sprays flue gas downwards in a vertical horizontal plane, and after the flue gas is sprayed to the vortex plate 3, the flow direction and the speed of the flue gas are changed.
It should be noted that the angle formed by the connection line of any two points on the vortex plate 3 and the sphere center is smaller than 180 degrees, namely, the circular arc formed by the vortex plate 3 is smaller than the semicircular arc with the same radius size, so that the flue gas sprayed onto the vortex plate 3 can conveniently overflow from the circular arc boundary.
As shown in fig. 1 and 2, the second deflector 7 is fixedly arranged on the inner wall of the cylindrical cavity of the reaction tower body 2 and is positioned above the flue pipe 1 to drain the flue gas so as to form airflow vortex in the reaction tower.
As shown in fig. 1 and 2, the first deflector 6 is fixedly disposed on the inner wall of the cylindrical cavity of the reaction tower body 2, above the second deflector 7, and opposite to the direction of the first deflector 6, and is used for guiding the flue gas to form an airflow vortex in the reaction tower.
As shown in fig. 1 to 3, the deacidification agent pipe 8 is symmetrically arranged at the upper part of the cylindrical cavity of the reaction tower body 2, the spray head 9 is connected to the deacidification agent pipe 8 and is positioned inside the reaction tower body 2, and is used for spraying the deacidification agent in the deacidification agent pipe 8 in the reaction tower body 2 in a mist form, wherein the main component of the deacidification agent is Ca (OH) 2, and the following reaction occurs with the acid gas in the flue gas:
2HCl(g)+Ca(OH)2→CaCl2+2H2O
As shown in fig. 10, the atomized Ca (OH) 2 slurry has an initial state in which the deacidification agent particles are dissolved in the liquid phase, is in a saturated state in the slurry, and has a dissolution equilibrium that complies with henry's law, ca (OH) 2 has a dissolution limit, and Ca (OH) 2 diffuses toward the liquid film; the water forms a liquid film on the surface of the particles, the deacidification reaction only occurs in the liquid phase, when the slurry enters the reaction tower, the water begins to evaporate rapidly on the surface of the particles, meanwhile SO 2 and HCl in the flue gas diffuse to the liquid film and are absorbed on the surface of the liquid drops, the volume of the liquid phase is reduced along with the evaporation, the reaction rate is increased, and when most of the water in the slurry evaporates, the chemical reaction is terminated.
As shown in fig. 1, the shortest distance from the central axis of a section of flue gas pipe 1 perpendicular to the horizontal plane to the inner wall of the cylindrical cavity of the reaction tower body 2 is la, namely, in the direction parallel to the horizontal plane, the shortest distance from the central axis of the flue gas pipe 1 to the inner wall of the reaction tower body 2 is la, the shortest distance from the central axis of the vortex plate 3 to the inner wall of the cylindrical cavity of the reaction tower body 2 is lb, namely, in the direction parallel to the horizontal plane, the shortest distance from the central axis of the vortex plate 3 to the inner wall of the reaction tower body 2 is lc, the value range of lc/lb is 0.45-0.75, and in the value range of the value interval, the distribution of air flow around the vortex plate 3 is ensured to be uniform, the air flow is promoted to form stronger turbulence, if the diameter of the vortex plate 3 is too large, the air flow is caused to flow to be concentrated in the interior of the vortex plate 3, the air flow is sparse outside the vortex plate 3, the air flow distribution is caused, and the deacidification effect is affected; the range of la/lb is 0.5-0.8, which can be understood as that the smoke pipe 1 is deviated from the central axis of the vortex plate 3, and smoke is guaranteed to enter from the circular arc slope of the vortex plate 3, and in the interval of la/lb ranging from 0.5-0.8, according to Bernoulli principle, when gas passes through the vortex plate 3 in the flowing process, the pressure is reduced when the speed is increased, and the smoke enters at one side of the vortex plate 3, so that the smoke speed at the side is higher, the pressure is lower, and the smoke speed is lower at the other side of the vortex plate 3, the pressure is higher, and the pressure difference can cause the airflow to rotate.
More specifically, since the vortex plate 3 is of a hemispherical design, when flue gas enters from one side of the vortex plate 3, the air flow can flow along the curve path of the vortex plate 3 due to the action of inertia force and viscosity force, so as to form a rotating vortex, namely, the shape and angle of the vortex plate 3 influence the rotating direction and strength of the vortex, and the shape and bending angle of the vortex plate 3 are limited in the range of values lc/lb of 0.45-0.75.
Therefore, the position of the flue gas entering the vortex plate 3 is changed, the flue gas enters from one side of the vortex plate 3, and the gas flow can generate larger pressure difference on one side of the vortex plate 3, so that rotary flow is formed, a rotary gas flow mode can be generated, a turbulence effect is enhanced, the turbulence intensity of the gas flow can be increased by the gas flow dynamic effect, and the reaction of acid gas in the flue gas and the deacidification agent is promoted.
As shown in fig. 1 and 2, the first baffle 6 is located at one end close to the flue gas pipe 1, the second baffle 7 is located at one end far away from the flue gas pipe 1, that is, the first baffle 6 is opposite to the second baffle 7, in the direction perpendicular to the horizontal plane, the distance from the first baffle 6 to the vortex plate 3 is na, the distance from the second baffle 7 to the vortex plate 3 is nb, and then the value range of nb/na is 0.65-0.8.
In the above structure, it is known that the flue gas in the flue gas pipe 1 enters the vortex plate 3 from one side of the vortex plate 3, so as to form a rotating edge vortex, the vortex can enhance turbulence effect, so that the flue gas and the deacidification agent are better mixed and contacted, the increase of the turbulence is helpful to improve mass transfer rate and reaction efficiency, so that the deacidification process is enhanced, the distribution of the vortex in the reaction tower can be optimized by fixedly installing the arc-shaped first deflector 6 and the arc-shaped second deflector 7 on the inner wall of the reaction tower, and in the interval of the value of nb/na of 0.65-0.8, namely, the first deflector 6 is higher than the second deflector 7, the height of the first deflector 6 is relatively higher, and the flue gas flow can be guided upwards, so that the flue gas can be promoted to form a rotating vortex above the vortex, and the rising airflow direction is helpful to enhance turbulence effect, and the strength and mixing effect of the vortex are improved; the second flow guide plate 7 has relatively low height, so that the diffusion degree of the vortex can be controlled, the lower second flow guide plate 7 can limit the rising height of the vortex and prevent the vortex from excessively diffusing, and the vortex can be kept in a proper area, so that the vortex is more concentrated and strong; if the height of the second baffle 7 is too high or is at the same height as the first baffle 6, the vortex is excessively concentrated above the plate, resulting in increased energy loss and instability of the vortex, and by setting the second baffle 7 to a lower height, the vortex is prevented from being excessively concentrated, maintaining stability and effectiveness of the vortex.
Therefore, the lower second guide plate 7 is beneficial to optimizing the reaction effect, can uniformly distribute vortex flow in the reaction tower, avoids local flow and uneven air flow distribution, can ensure that the deacidification agent is fully mixed and contacted with the flue gas, and improves the reaction efficiency and deacidification effect.
In some embodiments, as shown in fig. 1 to 5, four V-shaped guide holes 5 are uniformly arranged at the edge of the vortex plate 3, the V-shaped opening direction of the guide holes 5 is far away from the center of the vortex plate 3, the central angle of the guide holes 5 is θa, the central angle of a circular arc enclosed by any two adjacent V-shaped guide holes 5 is θb, the angle range of θa is 8 ° -18 °, and the angle range of θb is 72 ° -82 °.
In the above structure, four V-shaped guide holes 5 are uniformly arranged at the edge of the vortex plate, when the flue gas passes through the V-shaped guide holes 5 according to the principle of mass conservation and momentum conservation in fluid dynamics, the gas flow is influenced by the shape and direction of the guide holes 5, so that the speed and direction of the gas flow are changed, the change can generate rotation force and vortex formation, thereby forming a rotating vortex, the angle range of the central angle thetaa of the guide holes 5 is defined to be 8-18 degrees, because the smaller angle of the guide holes 5 can generate smaller vortex, the vortex is more concentrated and stable, and the size, the rotation speed and the distribution of the vortex are controlled based on the vortex control theory, namely, the rotation speed and the uniformity of the vortex are improved by controlling the angle of the guide holes 5, and the smaller angle is beneficial to ensure the full mixing and contact of the deacidification agent and the flue gas; in addition, based on the principle of energy conservation in fluid dynamics, the smaller angle of the guide hole 5 can enable the smoke to pass through the notch of the guide hole 5 more smoothly, so that flow resistance and pressure loss are reduced, and when the angle of the guide hole 5 is too large, the smoke can generate countercurrent or leakage at the guide hole 5 to influence the formation and stability of vortex, and the problems can be avoided by limiting the angle of the guide hole 5 to be in the range of 8-18 degrees, so that the normal operation and effect of the vortex are ensured.
In some embodiments, as shown in fig. 2, 4, 6 and 7, the first baffle 6 and the second baffle 7 are arc plates, the central angle of the first baffle 6 is θc, the angle range of θc is 80 ° -100 °, the central angle of the second baffle 7 is θd, the angle range of θd is 80 ° -100 °, and a plurality of through holes are disposed on each of the first baffle 6 and the second baffle 7.
In the structure, the angles of the circular arc central angles of the first guide plate 6 and the second guide plate 7 are larger, but the two guide plates do not completely surround the reaction tower from the overlook perspective, the larger circular arc central angle can reduce the pressure loss when the flue gas passes through the guide plates, when the flue gas flows through the guide plates, the larger circular arc central angle can enable the flue gas to flow more smoothly, reduce the resistance and the pressure loss, and the larger circular arc central angle can guide the air flow to generate rotation and vortex phenomena, so that stable rotation flow is formed on the guide plates, and the mixing effect and the turbulence intensity are increased; by limiting the circular arc central angle to be between 80 degrees and 100 degrees, the rotation speed and uniformity of vortex on the guide plate can be increased, the mixing and contact effect of the deacidification agent and the flue gas can be improved, the efficiency and thoroughness of the deacidification reaction can be enhanced, the contact area and the contact times of Ca (OH) 2 slurry and SO 2 and HCl in the flue gas can be increased by combining the rotating vortex flue gas formed at the guide plate, the contact area and the contact times of Ca (OH) 2 slurry and SO 2 and HCl in the flue gas can be increased, the Ca (OH) 2 slurry and the SO 2 and HCl in the flue gas can be continuously reacted, the SO 2 and the HCl can be continuously diffused to the liquid film of the Ca (OH) 2 slurry until the water in the slurry is completely evaporated, the effect of accelerating the evaporation speed of water molecules in the deacidification agent can be achieved, the evaporation process of the deacidification agent can be accelerated, and new process waste liquid can not be generated.
As shown in fig. 8 and 9, the spray head 9 includes a pressure pump 11 and a nozzle 12, three nozzles 12 are communicated with the pressure pump 11, each nozzle 12 is obliquely arranged on the pressure pump 11 at an angle, namely, the three nozzles 12 are in an expanding state at one side far away from the pressure pump 11, and are obliquely arranged, so that the sprayed liquid has a larger spraying distance and range, the spraying efficiency and the coverage area are improved, the pressure pump 11 can enable the deacidification agent particles to have higher speed and kinetic energy by increasing the pressure, the spraying distance is increased, the pressure pump 11 pressurizes the deacidification agent in the deacidification agent pipe 8 and then enters the three nozzles 12, the nozzles 12 spray the deacidification agent in the reaction tower body 2, and the deacidification agent performs deacidification reaction with flue gas in the reaction tower body 2.
Specifically, as shown in fig. 8 and fig. 9, a first conical cavity 13 and a second conical cavity 14 are disposed in each nozzle 12, the central axis of the first conical cavity 13 coincides with the central axis of the second conical cavity 14, the height of the first conical cavity 13 is larger than that of the second conical cavity 14, the central angle of the first conical cavity 13 is smaller than that of the second conical cavity 14, the expansion section of the first conical cavity 13 is communicated with the pressure pump 11, the contraction section of the second conical cavity 14 is communicated with the contraction section of the first conical cavity 13, the expansion section of the second conical cavity 14 is communicated with the end face of the nozzle 12 away from the pressure pump 11, and it can be understood that the deacidification agent enters from the bottom end of the first conical cavity 13 of the nozzle 12 after being pressurized by the pressure pump 11, passes through the contraction section connected with the first conical cavity 13 and the second conical cavity 14, and then is sprayed from the expansion section of the second conical cavity 14.
In the above structure, because the central angle of the first conical cavity 13 is smaller, the liquid is more constrained when entering the first conical cavity 13, so that the flow velocity of the liquid is accelerated, and the acceleration effect can enable the liquid deacidification agent to obtain higher velocity and kinetic energy before entering the second conical cavity 14; when liquid deacidification agent gets into second cone cavity 14 from the shrink section, liquid can be fully mixed with gas around, because the central angle of second cone cavity 14 is great, the liquid deacidification agent of spraying out can form vaporific granule, area of contact between liquid and the gas has been increased, thereby improved the mixing effect, the central angle of second cone cavity 14 is great, make the liquid deacidification agent of spraying out can form the atomizing state better, vaporific granule's formation can increase liquid surface area, make the reaction between deacidification agent and the flue gas more abundant, improve the deacidification effect.
The above description is only a preferred embodiment of the present invention, and the patent protection scope of the present invention is defined by the claims, and all equivalent structural changes made by the specification and the drawings of the present invention should be included in the protection scope of the present invention.
Claims (3)
1. The utility model provides a fume treatment equipment for msw incineration, includes reaction tower body (2), reaction tower body (2) divide into two cavitys, and one of them cavity is cylindricly, sprays deacidification reaction in the cylindric cavity, and another cavity is located cylindric cavity directly over to be connected with blast pipe (10), a serial communication port, include:
the flue gas pipe (1) is arranged at the lower part of the cylindrical cavity of the reaction tower body (2), and the air inlet direction of the flue gas pipe (1) is vertical to the horizontal plane and downward;
The vortex plate (3) is hemispherical, is fixedly arranged in the reaction tower body (2) and is positioned below the flue gas pipe (1), the central axis of the vortex plate (3) coincides with the central axis of the cylindrical cavity of the reaction tower body (2), the spherical center of the vortex plate (3) is close to the air inlet direction of the flue gas pipe (1), and when the flue gas pipe (1) sprays flue gas downwards in a vertical horizontal plane, the flow direction and the speed of the flue gas are changed after the flue gas is sprayed to the vortex plate (3);
the second guide plate (7) is fixedly arranged on the inner wall of the cylindrical cavity of the reaction tower body (2) and positioned above the flue gas pipe (1) to guide flue gas so as to form airflow vortex in the reaction tower;
The first guide plate (6) is fixedly arranged on the inner wall of the cylindrical cavity of the reaction tower body (2), is positioned above the second guide plate (7), is opposite to the direction of the first guide plate (6), and is used for guiding the flue gas to form an airflow vortex in the reaction tower;
The deacidification agent pipes (8) are symmetrically arranged at the upper part of the reaction tower body (2);
The spray head (9) is connected to the deacidification agent pipe (8) and positioned in the reaction tower body (2) and is used for spraying the deacidification agent in the deacidification agent pipe (8) in the reaction tower body (2) in a mist form;
The shortest distance from the central axis of a section of flue gas pipe (1) vertical to the horizontal plane to the inner wall of the cylindrical cavity of the reaction tower body (2) is la, the shortest distance from the central axis of the vortex plate (3) to the inner wall of the cylindrical cavity of the reaction tower body (2) is lb, and in the direction parallel to the horizontal plane, the farthest distance from the central axis of the vortex plate (3) to the boundary of the vortex plate (3) is lc, the value range of lc/lb is 0.45-0.75, and the value range of la/lb is 0.5-0.8;
The first guide plate (6) is positioned at one end close to the flue gas pipe (1), and the second guide plate (7) is positioned at one end far away from the flue gas pipe (1);
In the direction vertical to the horizontal plane, the distance from the first guide plate (6) to the vortex plate (3) is na, the distance from the second guide plate (7) to the vortex plate (3) is nb, and the value range of nb/na is 0.65-0.8;
At least two V-shaped guide holes (5) are uniformly formed in the edge of the vortex plate (3), and the V-shaped opening direction of the guide holes (5) is far away from the center of the vortex plate (3);
Four V-shaped guide holes (5) are uniformly formed in the edge of the vortex plate (3), the central angle of each guide hole (5) is theta a, the central angle of an arc formed by the surrounding of any two adjacent V-shaped guide holes (5) is theta b, the angle range of theta a is 8-18 degrees, and the angle range of theta b is 72-82 degrees;
The first guide plate (6) is an arc plate, the central angle of the first guide plate (6) is thetac, the angle range of thetac is 80-100 degrees, the second guide plate (7) is an arc plate, the central angle of the second guide plate (7) is thetad, the angle range of thetad is 80-100 degrees, and a plurality of through holes are respectively formed in the first guide plate (6) and the second guide plate (7).
2. The flue gas treatment device for garbage incineration according to claim 1, wherein the spray head (9) comprises a pressure pump (11) and nozzles (12), three nozzles (12) are connected to the pressure pump (11), each nozzle (12) is arranged on the pressure pump (11) in an inclined angle manner, the pressure pump (11) is used for pressurizing the deacidification agent in the deacidification agent pipe (8) and then enabling the deacidification agent to enter the three nozzles (12), the nozzles (12) spray the deacidification agent in the reaction tower body (2), and the deacidification agent performs deacidification reaction with flue gas in the reaction tower body (2).
3. A flue gas treatment device for waste incineration according to claim 2, characterized in that a first conical cavity (13) and a second conical cavity (14) are arranged in each nozzle (12), the central axis of the first conical cavity (13) coincides with the central axis of the second conical cavity (14), the height of the first conical cavity (13) is larger than that of the second conical cavity (14), the central angle of the first conical cavity (13) is smaller than that of the second conical cavity (14), the expansion section of the first conical cavity (13) is communicated with the pressure pump (11), the contraction section of the second conical cavity (14) is communicated with the contraction section of the first conical cavity (13), the expansion section of the second conical cavity (14) is communicated with the end face of the nozzle (12) away from the pressure pump (11), when the deacidification agent flows through the contraction section of the first conical cavity (13), the pressure of the liquid is increased, and spray is formed in the reaction tower (2) at the expansion section of the second conical cavity (14).
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CN204768033U (en) * | 2015-07-30 | 2015-11-18 | 中电投远达环保工程有限公司 | Dust removal defogging device |
CN208824231U (en) * | 2018-09-28 | 2019-05-07 | 航天凯天环保科技股份有限公司 | A kind of low-temperature denitration reaction tower and odor at low temperature denitrification apparatus |
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CN204768033U (en) * | 2015-07-30 | 2015-11-18 | 中电投远达环保工程有限公司 | Dust removal defogging device |
CN208824231U (en) * | 2018-09-28 | 2019-05-07 | 航天凯天环保科技股份有限公司 | A kind of low-temperature denitration reaction tower and odor at low temperature denitrification apparatus |
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