CN108159829B - Aggregation device for coupling steam phase change and turbulent aggregation and application thereof - Google Patents
Aggregation device for coupling steam phase change and turbulent aggregation and application thereof Download PDFInfo
- Publication number
- CN108159829B CN108159829B CN201810212788.0A CN201810212788A CN108159829B CN 108159829 B CN108159829 B CN 108159829B CN 201810212788 A CN201810212788 A CN 201810212788A CN 108159829 B CN108159829 B CN 108159829B
- Authority
- CN
- China
- Prior art keywords
- vortex
- semi
- cuboid
- agglomeration
- flue gas
- 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
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D51/00—Auxiliary pretreatment of gases or vapours to be cleaned
- B01D51/02—Amassing the particles, e.g. by flocculation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/01—Pretreatment of the gases prior to electrostatic precipitation
Abstract
The utility model relates to a steam phase change and turbulence agglomeration coupled agglomeration device and application thereof, wherein the agglomeration device is in a cuboid shape as a whole, is in an axially symmetrical structure about the direction of incoming smoke, and is provided with a smoke inlet at the left end, connected with desulfurization equipment and a smoke outlet at the right end, and connected with a wet-type electric dust collector; a plurality of semi-elliptic cylindrical protrusions are symmetrically arranged on the upper side wall and the lower side wall of the cuboid along the central axis of the device, and two semi-elliptic cylindrical protrusions which are opposite up and down are in a group, and n groups are totally arranged, wherein n is more than or equal to 2; the lowest point of each semi-elliptic cylindrical bulge faces the inside of the device; a cuboid turbulent flow column is arranged between the first group of semi-elliptic cylindrical protrusions and the smoke inlet, the central line of the cuboid turbulent flow column coincides with the central axis of the device, the cuboid turbulent flow column is of a hollow cavity structure, and steam nozzles are arranged on the upper surface and the lower surface of the cuboid turbulent flow column. The device increases the particle size of superfine particles through the mode of coupling vapor phase transition and turbulent aggregation, and has simple structure.
Description
Technical Field
The utility model relates to the technical field of treatment of ultrafine particles in coal-fired flue gas, and in particular belongs to an agglomeration device with coupling of steam phase change and turbulent agglomeration and application thereof.
Background
PM2.5, also referred to as lung-afflictable particulate, refers to fine particulate having an aerodynamic equivalent diameter of less than or equal to 2.5 μm. PM2.5 not only causes haze weather, influences people's daily activities, has serious harm to human breathing, cardiovascular system etc. simultaneously. Coal-fired boilers are an important component in modern production and are also the main emission source of PM 2.5. At present, the electrostatic dust collector, the cloth bag dust collector and the like are mainly adopted to remove particles in the flue gas, the electrostatic dust collector and the cloth bag dust collector have better effect of removing particles with larger particle size in the flue gas, but the removal efficiency of ultrafine particles is lower due to high specific resistance and poor charge capacity. It is difficult to remove ultrafine particles by using a traditional dust removing method, so that a pretreatment device is required to be studied to agglomerate the ultrafine particles into particles with larger particle sizes, and further the removal efficiency of the ultrafine particles is improved. There are a variety of agglomeration modes at present, including acoustic agglomeration, magnetic agglomeration, electric agglomeration, chemical agglomeration, thermal agglomeration, turbulent agglomeration, vapor phase change agglomeration, and the like. The mode that adopts turbulent agglomeration and steam phase change agglomeration to combine together not only simple structure, convenient operation can effectual promotion fine particle's grow up moreover. After the ultra-fine particles are agglomerated in the pretreatment mode, the ultra-fine particles enter a traditional dust remover for removal, so that the dust removal efficiency is improved.
The utility model patent with application number 201621297870.0 provides a fine particulate matter conversion and collection unit and an agglomeration and collection device for sintering flue gas, which consists of a particulate agglomeration part and an elbow collection part, wherein the agglomeration part mainly adopts a chemical agglomeration and turbulent agglomeration method. The bent pipe trapping part mainly comprises a storage part, an air inlet bent pipe and an air outlet bent pipe. The agglomerated and grown particles will settle at the bend and be stored in the storage means. The utility model utilizes the agglomerating agent spray head to spray the agglomerating agent into the agglomerating device, and the agglomerating agent is influenced by a plurality of factors, such as the dosage of the agglomerating agent, the concentration of the agglomerating agent, the temperature and the surface activity, so that the actual operation is difficult, and meanwhile, other pollutants are generated by chemical agglomeration and are subjected to aftertreatment, so that the agglomeration mode of coupling the chemical agglomeration and the turbulent agglomeration is unfavorable for the actual operation.
Liu Hanxiao (Liu Hanxiao. Coal ultrafine particulate matter vortex coalescence numerical simulation [ D ]. North China electric university, 2012.) designs an agglomeration device, four triangular prisms are arranged near an inlet inside the agglomeration device to divide flow, then three rows of Z-shaped vortex sheets are arranged at the rear, each row of six vortex sheets are arranged, the angle of each Z-shaped vortex sheet is perpendicular to the direction of incoming smoke, and the defects are that: the distance between the vortex sheets is relatively short, so that the rear vortex sheet can influence the development of the front vortex, damage the formed vortex and further influence the agglomeration effect; in addition, the number of the vortex sheets is too large, so that the resistance is increased, the pressure drop is increased, and the normal operation of the equipment is not facilitated.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model aims to provide an agglomeration device for coupling steam phase change and turbulent agglomeration and application thereof. The device increases the particle size of superfine particles through the mode of steam phase transition and turbulent aggregation coupling, and simultaneously, because the turbulent elements are fewer in number, the device is simple in structure, and therefore the pressure drop is smaller. The flue gas passing through the pretreatment mode enters a wet electric dust collector to further remove particles, so that the removal efficiency of ultrafine particles is improved. The device for removing fine particles is simple and convenient to operate, and has turbulent agglomeration and vapor phase change agglomeration.
The utility model solves the technical problems by adopting the following solution: the agglomeration device is in a cuboid shape as a whole, is in an axially symmetrical structure about the direction of incoming smoke, is provided with a smoke inlet at the left end and is connected with desulfurization equipment, and is provided with a smoke outlet at the right end and is connected with a wet electric dust collector; the device is characterized in that a plurality of semi-elliptic cylindrical protrusions are symmetrically arranged on the upper side wall and the lower side wall of the cuboid along the central axis of the device, and two semi-elliptic cylindrical protrusions which are opposite up and down are in a group, n groups are shared, and n is more than or equal to 2; the lowest point of each semi-elliptic cylindrical bulge faces the inside of the device; a cuboid turbulent flow column is arranged between the first group of semi-elliptic cylindrical bulges and the flue gas inlet, the central line of the cuboid turbulent flow column coincides with the central axis of the device, the cuboid turbulent flow column is of a hollow cavity structure, steam nozzles are arranged on the upper surface and the lower surface of the cuboid turbulent flow column, interfaces for connecting high-pressure steam pipelines are arranged on the front side surface and the rear side surface of the cuboid turbulent flow column, and the interfaces of the high-pressure steam pipelines are connected with a steam sprayer; a C-shaped turbulence vortex sheet is arranged in the device between the first group of semi-elliptic cylindrical bulges and the second group of semi-elliptic cylindrical bulges, the C-shaped turbulence vortex sheet is positioned on the central axis of the device, two C-shaped turbulence vortex sheets are symmetrically arranged up and down by taking the central axis of the device as the axis after the second group of semi-elliptic cylindrical bulges, the C-shaped turbulence vortex sheet is arranged on the central axis of the device after the third group of semi-elliptic cylindrical bulges, and a plurality of C-shaped turbulence vortex sheets are arranged in a fork row mode; the opening direction of each C-shaped turbulence vortex sheet faces the flue gas outlet.
The application of the agglomeration device for coupling steam phase transition and turbulent agglomeration is that the device is used for removing ultrafine particles, and the specific removal process is as follows:
(1) The flue gas after desulfurization and denitrification enters the agglomeration device at a speed of 5m/s, and the dust-containing flue gas entering the agglomeration device can be diffused, wherein collision effect can be generated among particles;
(2) After the flue gas is diffused, the flue gas flows through a cuboid turbulent flow column with a steam spraying function, the cuboid turbulent flow column can generate a diversion effect on the flue gas, meanwhile, steam is sprayed into the agglomeration device, the spraying speed is increased when the content of particles is large, the flue gas speed is changed due to the two effects, a speed gradient is generated, two eddies with opposite directions are formed behind the cuboid turbulent flow column, particles with smaller diameters are collided with the eddies at the inner sides of the eddies, and then larger particles are grown;
(3) Then a vortex is formed behind the semi-elliptic cylindrical bulge through the semi-elliptic cylindrical bulge, the distance between the semi-elliptic cylindrical bulge and the cuboid vortex column enables steam to fully develop, the distance between the semi-elliptic cylindrical bulge and the C-shaped vortex sheet enables the vortex formed by the bulge not to be influenced by the vortex sheet and the C-shaped vortex sheet, and particles with smaller diameters collide with the vortex inside the vortex in a follow-up manner, so that larger particles grow;
(4) The flue gas speed after passing through the C-shaped vortex sheets arranged in a fork row is changed to form a larger speed gradient, and two vortices with opposite directions are formed behind the C-shaped vortex sheets; particles with smaller diameters collide with the vortex rotation inside the vortex, so that larger particles grow;
(5) The flue gas after being shunted by the cuboid vortex column and disturbed by the plurality of C-shaped vortex sheets flows out from the flue gas outlet and enters the wet electric dust collector, and the wet electric dust collector carries out further removal treatment on particles.
Compared with the prior art, the utility model has the beneficial effects that:
(1) The agglomeration device is provided with a cuboid turbulence element with a steam spraying function at a smoke inlet (the cuboid turbulence element can have the turbulence effect due to internal spraying, the method combines the two effects onto the same device), the cuboid turbulence element can generate a flow division phenomenon of parallel flow smoke, and simultaneously the steam phase change effect can rapidly occur, so that the periphery of the turbulence element has a larger speed gradient, two eddies with opposite directions are formed behind the turbulence element, small particles rotate along with the eddies at the inner sides of the eddies, so that mutual collision occurs, and finally particles with larger particle sizes are formed.
(2) According to the method and the agglomeration device for coupling steam phase change and turbulence agglomeration, the cuboid and the turbulence element with the steam spraying function are arranged in the particle agglomeration device, and the steam spraying direction is perpendicular to the incoming flow smoke direction, so that the contact opportunity of steam and superfine particles is properly increased, the damage of backward spraying to formed vortex is avoided, and the rapid agglomeration of the particles is promoted.
(3) The inner wall of the agglomeration device is provided with the semi-elliptic cylindrical bulge (the boundary line of the semi-elliptic bulge is smoother, and a flow dead zone is not easy to occur). When the incoming smoke passes through the semi-elliptical protrusions, a large velocity gradient is generated, and vortex is formed behind the protrusions. The structure can increase the fluid disturbance at the boundary, so that small particles rotate along with the vortex when flowing through the boundary, grow into particles with larger particle size, and enhance the agglomeration effect.
(4) The device is simple and is easy to process and popularize. The vortex element is provided with a cuboid vortex column with a steam spraying function and a C-shaped) vortex sheet, symmetrical oval protrusions are arranged on the inner wall of the aggregation device, flue gas is shunted by the cuboid vortex element and then enters the aggregation device channel with the novel vortex element, the combined arrangement mode of the vortex sheet has smaller pressure drop, and meanwhile, the speed gradient is increased, so that particles become particles with larger particle size.
(5) The water vapor phase change mainly acts on small particles, so that the first half part of the agglomeration device mainly uses the vapor phase change to agglomerate the particles, and the turbulence agglomeration is mainly adopted in the second half region of the agglomeration device because the vapor phase change occurs very quickly and the vapor phase change effect is not obvious after the particles in the second half region grow up, and the turbulence agglomeration aims at the particles with slightly larger particle size. The steam phase change and turbulence agglomeration coupling mode avoids inconvenience and pollution caused by chemical agglomeration. The dust-containing flue gas increases the collision probability of particles through the flow dividing and disturbance effects, enhances the agglomeration effect, can be connected with a wet electric dust remover for dust removal, and has long-term development prospect.
Drawings
FIG. 1 is a schematic diagram of a perspective structure of one embodiment of an agglomeration apparatus coupled with steam phase transition and turbulent agglomeration in accordance with the present utility model;
FIG. 2 is a graph of velocity vectors of fine particles in the agglomeration apparatus of example 1;
FIG. 3 is a graph showing particle size distribution of particles in flue gas before and after agglomeration by the agglomeration apparatus of example 1;
FIG. 4 is a schematic view of a rectangular spoiler;
in fig. 1: 1-a flue gas inlet; 2-semi-elliptical cylindrical protrusions; 3-a flue gas outlet; 4-cuboid turbulent flow column; 5-C-shaped turbulence vortex sheet; 41 and 42-high pressure steam lines, 43 and 44-steam vents.
Detailed Description
The following more detailed description of the embodiments of the utility model is merely exemplary and is not intended to limit the scope of the utility model, as claimed.
The utility model relates to a steam phase change and turbulence agglomeration coupled agglomeration device (see figure 1), which is generally rectangular and axially symmetrical in structure about the direction of incoming smoke, wherein the left end of the agglomeration device is a smoke inlet 1, connected with desulfurization equipment, and the right end of the agglomeration device is a smoke outlet 3, connected with a wet-type electric dust collector; a plurality of semi-elliptic cylindrical protrusions 2 are symmetrically arranged on the upper side wall and the lower side wall of the cuboid along the central axis of the device, and two semi-elliptic cylindrical protrusions which are opposite up and down are in a group, n groups are totally arranged, and n is more than or equal to 2; the lowest point of each semi-elliptic cylindrical bulge faces the inside of the device; a cuboid turbulent flow column 4 is arranged between the first group of semi-elliptic cylindrical bulges and the flue gas inlet 1, the central line of the cuboid turbulent flow column 4 coincides with the central axis of the device, the cuboid turbulent flow column is of a hollow cavity structure, steam nozzles are arranged on the upper surface and the lower surface of the cuboid turbulent flow column, namely 43 and 44 in fig. 4, interfaces for connecting a high-pressure steam pipeline, namely 41 and 42 in fig. 4, are arranged on the front side surface and the rear side surface of the cuboid turbulent flow column, and the interfaces of the high-pressure steam pipeline are connected with a steam sprayer; a C-shaped vortex sheet 5 is arranged in the device between the first group of semi-elliptic cylindrical bulges and the second group of semi-elliptic cylindrical bulges, the C-shaped vortex sheet 5 is positioned on the central axis of the device, two C-shaped vortex sheets are symmetrically arranged up and down by taking the central axis of the device as the axis after the second group of semi-elliptic cylindrical bulges, the C-shaped vortex sheet 5 is arranged on the central axis of the device after the third group of semi-elliptic cylindrical bulges, and the plurality of C-shaped vortex sheets 5 are arranged in a fork arrangement mode, so that the utilization rate of space is increased, the influence of the back vortex sheets on the vortex formation of the front vortex sheets is reduced, and the disturbance on fluid is enhanced; the opening direction of each C-shaped turbulence vortex sheet faces the flue gas outlet.
The device is further characterized in that the ratio of the distance between the cuboid turbulent flow column and the smoke inlet, the distance between the first C-shaped turbulent flow vortex sheet and the smoke inlet, the distance between the C-shaped turbulent flow vortex sheet positioned on the central axis of the device and two symmetrically arranged C-shaped turbulent flow vortex sheets, and the distance between two adjacent groups of bulges is 3:4:6:6, preparing a base material; the semi-major axis of the semi-elliptic cylindrical bulge is 1/5 of the width of the agglomeration device. Because the flow characteristics of flow field in this application, the distance between cuboid vortex post, novel vortex piece and the arch should rationally set up, both need get up space make full use of, need guarantee simultaneously that vortex and vortex do not influence each other. The short axis of the semi-elliptic cylindrical bulge coincides with the wall surface, and is connected with the wall surface in a welding mode.
The device of the utility model is further characterized in that n=2, the first set of semi-elliptical cylindrical projections and the second set of semi-elliptical cylindrical projections are located at 1/4 and 11/20 of the length of the whole agglomeration device, respectively.
In the utility model, the number of the convex groups n=2, in actual production, the content of fine particles is different due to different flue gas flow rates and loads, and when the content of fine particles in the flue gas is increased, the steam quantity and the number of the convex groups can be properly increased, so that the fine particles are mixed more fully in the vortex.
The height of the semi-elliptic cylindrical bulge refers to the long half-axial length of an ellipse.
The utility model also protects the application of the agglomeration device coupled with the steam phase change and the turbulent agglomeration, and the device is used for removing ultrafine particles, and the specific removal process is as follows:
(1) The flue gas after desulfurization and denitrification enters the agglomeration device at a speed of 5m/s, and the dust-containing flue gas entering the agglomeration device can be diffused, wherein collision effect can be generated among particles;
(2) After the flue gas is diffused, the flue gas flows through a cuboid turbulent flow column with a steam spraying function, the cuboid turbulent flow column can generate a diversion effect on the flue gas, steam is sprayed into the agglomeration device, the steam spraying speed can be correspondingly adjusted according to different flue gas contents, when the particle content is high, the spraying speed can be properly increased, the flue gas speed can be changed due to the two effects, a speed gradient is generated, two opposite-direction eddies are formed behind the cuboid turbulent flow column, particles with smaller diameters are collided along with the eddies at the inner sides of the eddies, and then larger particles are grown;
(3) Then a vortex is formed behind the semi-elliptic cylindrical bulge through the semi-elliptic cylindrical bulge, the distance between the semi-elliptic cylindrical bulge and the cuboid vortex column enables steam to fully develop, the distance between the semi-elliptic cylindrical bulge and the C-shaped vortex sheet enables the vortex formed by the bulge not to be influenced by the vortex sheet and the C-shaped vortex sheet, and particles with smaller diameters collide with the vortex inside the vortex in a follow-up manner, so that larger particles grow;
(4) The flue gas velocity after passing through the C-shaped vortex sheets arranged in a fork row is changed to form a larger velocity gradient, two vortices with opposite directions are formed behind the C-shaped vortex sheets, the distance of the C-shaped vortex sheets along the length direction of the device has a larger influence on particle agglomeration, and the development of front vortex is influenced by the rear vortex sheets due to the too small distance; particles with smaller diameters collide with the vortex rotation inside the vortex, so that larger particles grow;
(5) The flue gas after being shunted by the cuboid vortex column and disturbed by the plurality of C-shaped vortex sheets flows out from the flue gas outlet and enters the wet electric dust collector, and the wet electric dust collector carries out further removal treatment on particles.
The device has even particle diameter distribution in superfine particles, has more obvious particle removal effect when the particle diameters of the particles are below PM2.5, and the particles with the particle diameters below 0.3 μm are larger than the particles with the particle diameters of 1.5-2.5 μm after the fume is agglomerated by the agglomeration device. The application is mainly aimed at the removal of small particles with the particle size of inlet particles below 0.3 mu m, and the application has a post-treatment device, namely the wet electrostatic precipitator, has higher removal efficiency for particles with the particle size of about 2 mu m, and the flue gas after agglomeration enters the wet electrostatic precipitator to further and effectively remove the particles again.
According to the utility model, the vapor is combined with the growth of fine particles and the turbulence agglomeration to one device, the distance between two adjacent semi-elliptic cylindrical protrusions on the same side accounts for 3/10 of the total length of the agglomeration device, so that a complete vortex can be formed, the space utilization rate is increased, and the repeated simulation shows that when the height of the semi-elliptic cylindrical protrusions is 1/5 of the width of the agglomeration device, the combination of the first group of semi-elliptic cylindrical protrusions and the cuboid turbulent flow column and the combination of the second group of semi-elliptic cylindrical protrusions and the C-shaped turbulent flow vortex sheet are most beneficial to the agglomeration effect; the C-shaped vortex sheets are adopted and are distributed in a fork row mode, the distance between the first row of vortex sheets and the second row of vortex sheets is 3/10 of the length of the aggregation device, so that the space utilization rate is increased, and the damage of the rear device to the front vortex structure is reduced; the water vapor phase change mainly acts on small particles, so that the first half part of the agglomeration device mainly uses the vapor phase change to agglomerate the particles, and the turbulence agglomeration is mainly adopted in the second half part of the agglomeration device because the vapor phase change happens very fast and the vapor phase change effect is not obvious after the particles in the second half part grow up, so that the particles with slightly larger particle size are targeted.
Example 1
The agglomeration device of the embodiment is in a cuboid shape on the whole, but the boundary of the agglomeration device is provided with a semi-elliptic cylindrical bulge, and the whole is in an axially symmetrical structure relative to the direction of the incoming smoke. The left end of the agglomeration device is provided with a flue gas inlet 1 which is connected with desulfurization equipment, and the right end of the agglomeration device is provided with a flue gas outlet 3 which is connected with a wet-type electric dust collector. The inside cuboid vortex post 4 and C shape vortex piece 5 that have the steam injection function that include of reunion device, cuboid vortex post 4 central line that has the steam injection function is located the central line of reunion device, and cuboid vortex post is close to the flue gas entry position, and its top view is a rectangle, and the long limit is perpendicular with flue gas inflow direction, and first row C shape vortex piece 5 is located the 2/5 department of whole reunion device, and three C shape vortex piece altogether adopts the mode of fork row to arrange.
The length of the agglomeration device is 1000mm, the width is 400mm, and the height is 200mm.
The distance from the center of the rectangle to the smoke inlet is 150mm, the length of the rectangle is 80mm, and the width of the rectangle is 30mm.
The top view of the semi-elliptic cylindrical protrusions on the edge of the agglomeration device is semi-elliptic, the short axis of the semi-elliptic is coincident with the boundary of the agglomeration device, the long axis of the semi-elliptic is perpendicular to the boundary of the agglomeration device, the short half axis of the semi-elliptic is 20mm, the long half axis of the semi-elliptic is 80mm, the distance from the first group of semi-elliptic cylindrical protrusions to the smoke inlet is 250mm, the total two groups of protrusions are arranged, and the distance between the two groups of protrusions is 300mm.
FIG. 2 is a graph showing velocity vectors of fine particles in the agglomeration apparatus of this example, showing: flue gas after desulfurization and denitrification enters the agglomeration device at the speed of 5m/s, is fully mixed and diffused, flows through a cuboid turbulent flow column with a steam spraying function, can split the flue gas, simultaneously sprays steam into the agglomeration device, and rapidly generates steam phase change. Then the flue gas velocity after passing through the semi-elliptic cylindrical bulges and the C-shaped vortex sheets arranged in the fork rows changes to form a larger velocity gradient, two vortices with opposite directions are formed behind the C-shaped vortex sheets, and a relatively complete vortex is formed behind the semi-elliptic cylindrical bulges. The water vapor phase change mainly acts on small particles, so that the first half part of the agglomeration device mainly uses the vapor phase change to agglomerate the particles, and the turbulence agglomeration is mainly adopted in the second half region of the agglomeration device because the vapor phase change occurs very quickly and the vapor phase change effect is not obvious after the particles in the second half region grow up, and the turbulence agglomeration aims at the particles with slightly larger particle size. The flue gas after being subjected to cuboid vortex column flow distribution and C-shaped vortex sheet vortex flows out from an outlet of the agglomeration device, enters into a wet electric dust collector, and is subjected to further removal treatment by the wet electric dust collector.
FIG. 3 is a graph showing particle size distribution in flue gas before and after agglomeration by an agglomeration device, wherein the abscissa and ordinate represent particle size and particle number density percentage, respectively. Most of particle sizes at the inlet are lower than 0.3 mu m, the maximum value of particle size distribution is between 0.2 and 0.3 mu m, after agglomeration by the agglomeration device, the peak value of the particle size distribution diagram of the particles obviously moves in the direction of increasing the particle sizes, the particle size distribution diagram can be obtained by analyzing the particle size distribution diagram, and the flue gas has obvious growth effect of ultrafine particles by the agglomeration device.
In the utility model, terms such as up, down, left, right and the like are relative concepts. The direction of the flue gas inlet 1 is left, the direction of the flue gas outlet 3 is right, and the outer wall of the agglomeration device with the protrusions is up and down.
The utility model is applicable to the prior art where it is not described.
Claims (4)
1. The aggregation device is in a cuboid shape as a whole, is in an axially symmetrical structure about the direction of incoming smoke, is provided with a smoke inlet at the left end and is connected with desulfurization equipment, and is provided with a smoke outlet at the right end and is connected with a wet-type electric dust collector; the device is characterized in that a plurality of semi-elliptic cylindrical protrusions are symmetrically arranged on the upper side wall and the lower side wall of the cuboid along the central axis of the device, and two semi-elliptic cylindrical protrusions which are opposite up and down are in a group, n groups are shared, and n is more than or equal to 2; the lowest point of each semi-elliptic cylindrical bulge faces the inside of the device; a cuboid turbulent flow column is arranged between the first group of semi-elliptic cylindrical bulges and the flue gas inlet, the central line of the cuboid turbulent flow column coincides with the central axis of the device, the cuboid turbulent flow column is of a hollow cavity structure, steam nozzles are arranged on the upper surface and the lower surface of the cuboid turbulent flow column, interfaces for connecting high-pressure steam pipelines are arranged on the front side surface and the rear side surface of the cuboid turbulent flow column, and the interfaces of the high-pressure steam pipelines are connected with a steam sprayer; a C-shaped turbulence vortex sheet is arranged in the device between the first group of semi-elliptic cylindrical bulges and the second group of semi-elliptic cylindrical bulges, the C-shaped turbulence vortex sheet is positioned on the central axis of the device, two C-shaped turbulence vortex sheets are symmetrically arranged up and down by taking the central axis of the device as the axis after the second group of semi-elliptic cylindrical bulges, and the three C-shaped turbulence vortex sheets are arranged in a fork row mode; the opening direction of each C-shaped turbulence vortex sheet faces the flue gas outlet.
2. The condensing device of coupling vapor phase transition and turbulent flow condensing according to claim 1, wherein the ratio of the distance between the cuboid turbulent flow column and the flue gas inlet, the distance between the first C-shaped turbulent flow vortex sheet and the flue gas inlet, the distance between the C-shaped turbulent flow vortex sheet positioned on the central axis of the device and two symmetrically arranged C-shaped turbulent flow vortex sheets, and the distance between two adjacent semi-elliptic cylindrical protrusions is 3:4:6:6, preparing a base material; the semi-major axis of the semi-elliptic cylindrical bulge is 1/5 of the width of the agglomeration device.
3. The vapor phase transition and turbulent agglomeration coupled device of claim 1, wherein n = 2, the first set of semi-elliptical cylindrical protrusions and the second set of semi-elliptical cylindrical protrusions are located at 1/4 and 11/20 of the length of the entire agglomeration device, respectively.
4. Use of an agglomeration device coupled with steam phase transition and turbulent agglomeration according to claim 1 for removing ultra-fine particles, the specific removal process being:
(1) The flue gas after desulfurization and denitrification enters the agglomeration device at a speed of 5m/s, and the dust-containing flue gas entering the agglomeration device can be diffused, wherein collision effect can be generated among particles;
(2) After the flue gas is diffused, the flue gas flows through a cuboid turbulent flow column with a steam spraying function, the cuboid turbulent flow column can generate a diversion effect on the flue gas, meanwhile, steam is sprayed into the agglomeration device, the spraying speed is increased when the content of particles is large, the flue gas speed is changed due to the two effects, a speed gradient is generated, two eddies with opposite directions are formed behind the cuboid turbulent flow column, particles with smaller diameters are collided with the eddies at the inner sides of the eddies, and then larger particles are grown;
(3) Then a vortex is formed behind the semi-elliptic cylindrical bulge through the semi-elliptic cylindrical bulge, the distance between the semi-elliptic cylindrical bulge and the cuboid vortex column enables steam to fully develop, and the distance between the semi-elliptic cylindrical bulge and the C-shaped vortex sheet enables vortex formed by the semi-elliptic cylindrical bulge not to be influenced by the vortex sheet and the C-shaped vortex sheet, particles with smaller diameters collide with the vortex rotation at the inner side of the vortex, and further grow into larger particles;
(4) The flue gas speed after passing through the C-shaped vortex sheets arranged in a fork row is changed to form a larger speed gradient, and two vortices with opposite directions are formed behind the C-shaped vortex sheets; particles with smaller diameters collide with the vortex rotation inside the vortex, so that larger particles grow;
(5) The flue gas after being shunted by the cuboid vortex column and disturbed by the plurality of C-shaped vortex sheets flows out from the flue gas outlet and enters the wet electric dust collector, and the wet electric dust collector carries out further removal treatment on particles.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810212788.0A CN108159829B (en) | 2018-03-15 | 2018-03-15 | Aggregation device for coupling steam phase change and turbulent aggregation and application thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810212788.0A CN108159829B (en) | 2018-03-15 | 2018-03-15 | Aggregation device for coupling steam phase change and turbulent aggregation and application thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108159829A CN108159829A (en) | 2018-06-15 |
| CN108159829B true CN108159829B (en) | 2023-07-14 |
Family
ID=62512035
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810212788.0A Active CN108159829B (en) | 2018-03-15 | 2018-03-15 | Aggregation device for coupling steam phase change and turbulent aggregation and application thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108159829B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111773865B (en) * | 2020-07-09 | 2021-10-22 | 中国石油大学(华东) | Experimental device and method for efficiently removing PM2.5 fine particles in industrial boiler tail gas |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19532862A1 (en) * | 1995-09-06 | 1997-03-13 | Graf Epe Gmbh | Plant cleaning waste gases by solids contacting in recirculated fluidised bed |
| DE19717883A1 (en) * | 1997-03-22 | 1998-09-24 | Reiner Waese | Water flow-control assembly creates repeated change from turbulent to laminar flow |
| EP1795251A1 (en) * | 2005-12-12 | 2007-06-13 | United Technologies Corporation | Pulse detonation particulate agglomerator |
| CN104801420A (en) * | 2015-05-13 | 2015-07-29 | 东南大学 | Device and method for increasing grain size of PM2.5 (particulate matter2.5) through turbulent flow and chemical agglomeration coupling |
| CN105536423A (en) * | 2016-01-31 | 2016-05-04 | 河北工业大学 | Smoke gas PM2.5 (particulate matter 2.5) removing device and process of coal burning boiler |
| CN206587558U (en) * | 2017-03-18 | 2017-10-27 | 河北工业大学 | A kind of turbulent flow reunion room with recess channels |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2523886A1 (en) * | 2003-04-28 | 2004-11-11 | Rodney John Truce | Method and apparatus for mixing fluids for particle agglomeration |
| CN106512633B (en) * | 2016-12-19 | 2019-07-30 | 青岛大学 | Turbulent flow and chemical agglomeration couple fine grained agglomeration device |
| CN206613333U (en) * | 2017-04-10 | 2017-11-07 | 河北工业大学 | Tapering type reunion room with phase transformation side's chamber and turbulence columns |
-
2018
- 2018-03-15 CN CN201810212788.0A patent/CN108159829B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19532862A1 (en) * | 1995-09-06 | 1997-03-13 | Graf Epe Gmbh | Plant cleaning waste gases by solids contacting in recirculated fluidised bed |
| DE19717883A1 (en) * | 1997-03-22 | 1998-09-24 | Reiner Waese | Water flow-control assembly creates repeated change from turbulent to laminar flow |
| EP1795251A1 (en) * | 2005-12-12 | 2007-06-13 | United Technologies Corporation | Pulse detonation particulate agglomerator |
| CN104801420A (en) * | 2015-05-13 | 2015-07-29 | 东南大学 | Device and method for increasing grain size of PM2.5 (particulate matter2.5) through turbulent flow and chemical agglomeration coupling |
| CN105536423A (en) * | 2016-01-31 | 2016-05-04 | 河北工业大学 | Smoke gas PM2.5 (particulate matter 2.5) removing device and process of coal burning boiler |
| CN206587558U (en) * | 2017-03-18 | 2017-10-27 | 河北工业大学 | A kind of turbulent flow reunion room with recess channels |
Non-Patent Citations (3)
| Title |
|---|
| A new turbulent-burst-based model for particle resuspension from rough surfaces in turbulent flow;You,Siming;AEROSOL SCIENCE AND TECHNOLOGY;1031-1042 * |
| 平面湍流射流细颗粒物团聚的PBM-LES耦合模拟;李佳;热能动力工程;第32卷(第7期);64-72 * |
| 湍流聚并室内细颗粒物聚并的数值研究;张书斌;李佳;李阳;杨历;陈占秀;;河北工业大学学报(第06期);79-82 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108159829A (en) | 2018-06-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105597477B (en) | Remove the device and method of superfine particulate matter in fire coal boiler fume | |
| CN108159787B (en) | Device for strengthening collision aggregation and growth of fine particles in flue gas | |
| CN110496704B (en) | Bipolar atomizing is fine particles of electric agglomeration device in advance | |
| CN105854500B (en) | Turbulent flow reunion room and the method for application reunion room removing superfine particulate matter | |
| CN105749690A (en) | Device and method for promoting interaction of fine particles in smoke of coal-fired boiler | |
| CN203971653U (en) | A kind of gas-liquid reallocation and subparticle capturing device that is applicable to single tower double circulation desulphurization tower | |
| CN206391788U (en) | Fountain inertial dust separator | |
| CN104667677A (en) | Venturi washing and filtering device | |
| CN111558256A (en) | Superfine particle separation system under coupling mechanism | |
| CN110652807B (en) | Non-uniform film falling pipe, unit and device applied to falling film dust removal | |
| CN108159829B (en) | Aggregation device for coupling steam phase change and turbulent aggregation and application thereof | |
| CN101780361B (en) | Method and device for prompting aggregation of particles | |
| CN2393627Y (en) | Horizontal casing cyclone liquid remover | |
| CN104455897B (en) | Three-phase vortex street current sharing method and device | |
| CN112807925B (en) | Device for promoting particle agglomeration through multi-scale turbulence coupling | |
| CN206587558U (en) | A kind of turbulent flow reunion room with recess channels | |
| CN201316597Y (en) | Alveolate venturi smoke gas dust removal and desulphurization clearing device | |
| CN202237684U (en) | Novel streamline two-channel demister with barb | |
| CN205055823U (en) | Use and spout ammonia dust collector in advance in coal fired power plant flue gas | |
| CN208130753U (en) | The agglomeration device that steam phase transforming is coupled with turbulent flow reunion | |
| CN205598871U (en) | Fine particles interact's device in promotion coal fired boiler flue gas | |
| CN201906521U (en) | Flat-plate demisting device with pre-demister | |
| CN204637884U (en) | Electromechanical integration dedusting demister | |
| CN208260547U (en) | Power station SCR system ash hopper device based on high centrifugal force flue and brave tooth plate | |
| CN208003685U (en) | A kind of particle agglomeration room with tilting double entrances and turbulent element |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |