CN110124427A - The capturing device and method of fine particle in a kind of wet flue gas - Google Patents
The capturing device and method of fine particle in a kind of wet flue gas Download PDFInfo
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- CN110124427A CN110124427A CN201910409028.3A CN201910409028A CN110124427A CN 110124427 A CN110124427 A CN 110124427A CN 201910409028 A CN201910409028 A CN 201910409028A CN 110124427 A CN110124427 A CN 110124427A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- 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
Abstract
The invention discloses the capturing device and method of fine particle in a kind of wet flue gas, device includes scrubbing tower, Sprayer Circulation pump, air cooling tower and condensate circulation pump；Wash spray layer, cyclone cylinder deduster layer, indirect condensing layer, level-one demisting layer, hydrops layer, packing layer, condensation spraying layer and second level demisting layer are set gradually by smoke inlet to exhanst gas outlet in scrubbing tower；Condensate liquid storage pool, condensate liquid cooling packing layer and condensate liquid cooling spraying layer are set gradually in air cooling tower tower body from the bottom to top；The leakage fluid dram for being equipped with below level-one demisting layer and being connected to outside scrubbing tower；Hydrops layer, indirect condensing layer the liquid inlet of condensate liquid cooling spraying layer of leakage fluid dram and air cooling tower be connected to；Indirect condensing layer, the liquid inlet for condensing spraying layer are pumped by condensate circulation to be connected to air-cooled tower bottom condensate liquid storage pool.The present invention is by carrying out multiple demisting, heat exchange, condensation, final low energy consumption high-efficiency coalescence, increase and the trapping for realizing superfine particulate matter in wet flue gas to wet flue gas.
Description
Technical field
The present invention relates to resource and environment protection field more particularly to a kind of wet flue gas in fine particle capturing device and
Method.
Background technique
In recent years, Environmental Inputs dynamics is constantly reinforced with country, China's air environmental pollution object total emission volumn obtains
Effectively control, from the point of view of classification of pollutant, the four class major pollutants such as sulfur dioxide, nitrogen oxides, particulate matter, VOCs are average annual
Downward trend year by year is presented in concentration substantially, and city ratio up to standard increases.But the total emission volumn of atmosphere pollution is still all the year round
Occupy high, atmosphere quality improves slowly, the current atmospheric pollution level in China still have with ideal air environment it is larger away from
From especially the particle concentrations such as PM2.5, PM10 are exceeded serious.It wherein pollutes and stands in the breach caused by fire coal, to PM in air
2.5 pollution contribution amounts are most.The major pollutants generated when coal burning include sulfur dioxide, nitrogen oxides, particulate matter, an oxygen
Change carbon etc., is largely difficult to the ultra-fine grain removed wherein having in the flue dust discharged, is the main source of PM 2.5；On the other hand,
The sulfur dioxide and nitrogen oxides of coal burning discharge, in winter in low temperature and high relative humidity surrounding air, with the mist being suspended in the air
Drop is carrier, carries out complicated Atmospheric Chemistry with other pollutants in air and reacts, forms secondary thin of sulfate, nitrate etc.
Grain object, these are converted into solid contaminant by gaseous pollutant, are further exacerbated by the formation of haze weather.
Currently, China's coal unit is more than 90% using wet scrubbing flue gas desulfurization technique.The row of wet desulphurization tail gas
Smoke temperature degree, for supersaturated wet flue gas, discharges containing water vapor, condensing water droplet, slurries droplet, CO in flue gas at 50 DEG C~60 DEG C2, not
The SO of removingx、NOx, dissolubility salt, gel dust, the multiple pollutants such as micronic dust etc. (for the main component of haze).In order to slow down
Environmental pollution caused by industrial coal, China was in promulgation new edition " fossil-fuel power plant atmospheric pollutant emission standard " in 2011
(GB13223-2011), it is come into effect on January 1st, 2012, discharge of the new standard to sulfur dioxide, nitrogen oxides and flue dust
Concentration requires to be improved largely, and some projects have been strict in EU criteria, further promotes thermal power plant to carry out energy-saving and emission-reduction and changes
It makes, reduces discharge amount, increases exhaust-gas treatment disposal facility to improve handling rate.
The industrial coal smoke pollution discharge standard for increasingly becoming tight only proposes strictly the Absolute emissions concentration of pollutant
It is required that the harm of discharge flue gas environmental pollution can be effectively relieved by reduction concentration of emission for gaseous pollutant；But
For fine particle, the particulate matters removal technology such as existing dry electric precipitation, wet-esp, eddy flow centrifuge separation can only
The particulate matter of greater particle size is removed, but lower to the removal efficiency of the superfine particulate matters such as PM2.5, PM1.0, PM0.5, and existing skill
It is mainly the superfine particulate matter for being less than PM2.5 or PM1.0 that art, which not can be removed and be discharged into the particulate matter in atmosphere, and these are ultra-fine
Harm caused by particulate matter enters in ambient air is the master of haze much larger than the large-size particles object that the prior art can remove
Want component part.
Therefore, the efficient removal for how realizing superfine particulate matter in industrial coal flue gas is the required face of current smoke pollution
Pair problem.
Summary of the invention
The present invention provides the capturing devices and method of fine particle in a kind of wet flue gas, carry out to the flue gas after demisting cold
It is solidifying, the superfine particulate matter for being difficult to trap will be remained in the flue gas after demisting as the crystallization of vapor condensation liquefaction process in flue gas
Core is realized that the coalescence of superfine particulate matter increases, and is trapped using high-efficiency demisting apparatus；By repeatedly being removed to wet flue gas
Mist, condensation, trapping, final efficient coalescence, increase and the trapping for realizing superfine particulate matter in wet flue gas, greatly improve in wet flue gas
The removal efficiency of superfine particulate matter.
Specific technical solution is as follows:
The capturing device of fine particle in a kind of wet flue gas, including scrubbing tower, Sprayer Circulation pump, air cooling tower and condensate liquid follow
Ring pump；
The washing tower side wall is equipped with smoke inlet, top is equipped with exhanst gas outlet, is partially tower reactor below smoke inlet；
In the scrubbing tower by smoke inlet to exhanst gas outlet set gradually wash spray layer, cyclone cylinder deduster layer, indirect condensing layer,
Level-one demisting layer, hydrops layer, packing layer, condensation spraying layer and second level demisting layer；
The air cooling tower includes tower body, and tower body bottom is equipped with air intake, and top is equipped with air outlet slit；In tower body by down toward
On set gradually condensate liquid storage pool, condensate liquid cooling packing layer and condensate liquid cooling spraying layer；
The liquid inlet of the wash spray layer be connected to by pipeline with Sprayer Circulation pump discharge, the tower reactor pass through pipeline and
Sprayer Circulation pump inlet connection；
The leakage fluid dram for being equipped with below the level-one demisting layer and being connected to outside scrubbing tower；
It is equipped with leakage fluid dram below the hydrops layer, is connected by the liquid inlet of the condensate liquid of pipeline and air cooling tower cooling spraying layer
It is logical；
The indirect condensing layer, the liquid inlet for condensing spraying layer pump liquid outlet with condensate circulation by pipeline and are connected to,
It connects condensate layer liquid outlet and is connected to by pipeline with the liquid inlet of the condensate liquid of air cooling tower cooling spraying layer, air-cooled tower bottom condensate liquid
Storage pool pumps liquid inlet with condensate circulation by pipeline and is connected to.
The cyclone cylinder deduster layer is made of several cyclone cylinder dedusters up and down and fixed bottom plate, the fixation
Bottom plate outer and washing inner wall of tower are tightly connected, and the cyclone cylinder deduster, which runs through, to be fixed on fixed bottom plate；Each cyclone cylinder
Deduster is made of the swirl vane that cylinder and several layers are installed on inner barrel.
Preferably, the spacing of the cyclone cylinder deduster layer and wash spray layer is 0.5m-2m, and cyclone cylinder deduster is high
0.5m-2m, cyclone cylinder overcurrent gas velocity are 5m/s-10m/s.
On the one hand cyclone cylinder deduster can remove the coarseparticulate in flue gas, on the other hand can increase flue gas eddy flow,
Reinforce the heat transfer effect of flue gas and top indirect condensing layer.
Several condensing heat-exchange modules are equipped in the indirect condensing layer, each condensing heat-exchange module is by several equidistant vertical
The metal blade and several layers equidistantly distributed of arrangement and the condensate liquid circulation duct composition for passing perpendicularly through metal blade；
Metal blade is 0.3m- with a thickness of 0.5mm-3mm, blade pitgh 20mm-80mm, indirect condensing layer height
0.6m, the flue-gas temperature range of decrease is 0.5 DEG C -5 DEG C after heat exchange.
The level-one demisting layer is made of demister modules, supporting beam, intake chute, and several demister modules inclinations are symmetrically put
It is placed in supporting beam, two adjacent demister modules form V-shaped；
Intake chute is fixed in supporting beam, and opening is located at below two adjacent demister modules bottom joining places；
The opening of the intake chute has draining plate；One end of intake chute is equipped with the leakage fluid dram being connected to outside with scrubbing tower.
Preferably, the demister modules are made of folded sheet or corrugated sheet, folded sheet or waveform plate spacing are 5mm-
The slanted angle degree of 20mm, demister modules and horizontal plane is 30 ° -60 °；The level-one demisting layer height is 0.5m-1.5m.
Level-one demisting layer captures the droplet containing particle dust, collects through intake chute and is discharged outside scrubbing tower in time, keeps away
Exempting to fall into scrubbing tower tower reactor causes dust in washing tower reactor accumulation.
The hydrops layer is made of several hydrops slots being equidistantly evenly arranged and deflector, and deflector is obliquely installed and bottom
End is located in hydrops slot, and the gap section between two neighboring hydrops slot is airflow channel.Preferably, airflow channel and hydrops
The ratio of slot groove width is 0.5-1:1, and the tilt angle of deflector and horizontal plane is 40 ° -70 °, and hydrops layer height is 0.3m-
0.8m。
Preferably, the deflector top abuts packing layer；Bed stuffing height is 0.5m-2m.
Groove body collects the high temperature condensate liquid for completing condensing heat-exchange, and deflector plays the drop taken off under flue gas and packing layer and leads
To effect, hydrops slot leakage is avoided.
Preferably, described filler layer is tilted is provided with several honeycomb channels, and packing layer bottom abuts the deflector
Upper end；
Preferably, honeycomb hole wall thickness is 0.2mm-0.5mm, honeycomb hole section is regular hexagon or circle, section
Hole area is 15cm2-50cm2；Bed stuffing height is 20cm-50cm, and honeycomb axially bored line angle with horizontal plane is 40 ° -80 °.
The honeycomb hole wall thickness refers to the packing layer wall thickness between two adjacent honeycomb holes.
Preferably, the spacing of the condensation spraying layer and packing layer is 0.5m-1.5m；Condense the spray liquid-gas ratio of spraying layer
For 0.5L/Nm3-3.0L/Nm3, nozzle atomization pressure is 0.10MPa-0.30MPa, and flue gas cool-down amplitude is 5 DEG C -20 after heat exchange
℃。
Preferably, the second level demisting layer height is 0.2m-0.5m；Baffle plate demister, folding are set in second level demisting layer
For flowing plate with a thickness of 0.2mm-2.0mm, adjacent baffle spacing is 3mm-10mm.
It is further preferred that the baffle plate is sheet metal.
Preferably, the tower body of the air cooling tower is hyperbola tower body.
Preferably, the indirect condensing layer is higher than condensate liquid cooling spraying layer 10m-30m.The high temperature for completing heat exchange is cold
Lime set is sent through pipeline to condensate liquid cooling spraying layer liquid inlet, in the work of height pressure difference by indirect condensing layer and hydrops layer leakage fluid dram
It under, is sprayed by nozzle atomization, forms fine drop in air cooling tower, fine drop and cold air heat exchange cool down, air themperature
It increases, it is poor that air from top to bottom forms certain Graded Density in air cooling tower, is produced from pull out force and forms heat transfer free convection.
Preferably, cooling extent of the condensate liquid in air cooling tower is 5 DEG C -20 DEG C.
Condensate liquid after cooling is delivered to condensation spraying layer by condensate circulation pump, realizes condensate liquid low energy consumption circulation benefit
With with flue gas cool-down.
The present invention also provides a kind of capture methods of fine particle in wet flue gas, it is preferred to use thin in the wet flue gas
The capturing device of particulate matter is implemented, comprising the following steps:
(1) flue gas enters scrubbing tower by smoke inlet, and tower reactor slurries are after Sprayer Circulation is pumped to the atomization of wash spray layer
Flue gas is washed, gaseous pollutant and large dust particle are removed, flue gas and cleaning solution heat exchange are condensed to saturation state；Saturation
Flue gas enters cyclone cylinder deduster layer, goes down in eddy flow centrifugal action except the slurries droplet and large dust particle in flue gas, completes
The level-one trapping of fine particle in flue gas (the wet flue gas processing for containing only particulate matter can not set wash spray layer)；
(2) flue gas for completing the trapping of particulate matter level-one enters the condensation of indirect condensing layer and is cooled to supersaturation, and vapor is with residual
The fine particle stayed is condensation karyogenesis liquid mist drop, and flue gas carries liquid droplet and enters level-one demisting layer, and liquid droplet is by one
The trapping of grade demisting layer is simultaneously discharged outside scrubbing tower by intake chute, completes B-grade condensation, the coalescence, trapping of fine particle in flue gas；
(3) wet flue gas for completing second level trapping carries a small amount of residual fine particles object and passes through hydrops layer, packing layer, condensation spray
Layer and second level demisting layer, with condensation spray liquid by indirect condensing in packing layer, vapor continuation is to remain fine particle
Nuclei of crystallization condensation；Flue gas contacts with low temperature spray liquid continuation deep condensation in condensation spraying layer, and traps fine particle and cold
Lime set drop；The flue gas for carrying residual droplet is discharged after second level demister layer demisting by exhanst gas outlet, completes the three of fine particle
Grade deep condensation, coalescence, trapping.
Compared with prior art, the invention has the benefit that
(1) the present invention provides a kind of solution for realizing that fine particle low energy consumption traps in wet flue gas, machine is first passed through
Tool demister pattern removes slurries droplet, condensing droplet and the larger particles in flue gas, and it is solidifying then to carry out chilling to saturated flue gas
Realize that the increase of particulate matter is gone forward side by side to supersaturation using the superfine particulate matter for being difficult to remove as the liquefied nuclei of condensation of vapor
Row trapping；By multistage demisting, condensation, coalescence and trapping, realize that the low energy consumption of superfine particulate matter is removed in depth；
(2) the present invention provides the solution party that fine particle capturing device in a kind of wet flue gas realizes continuous and steady operation
Case efficiently traps the condensation drop after completing condensation, coalescence using the ridge type demister of baffle plate composition, and
It realizes that demister cleans using the liquid film of droplet formation, effectively prevents demister blocking, scale formation, greatly improve thin
The stability of particlate trap system continuous operation；
(3) the present invention provides a kind of solutions for realizing that fine particle efficiently traps in wet flue gas, using cyclone cylinder
The guide functions of dust-extraction unit and indirect condensing blading improve the uniformity in flue gas flow field in scrubbing tower, and it is cold to improve flue gas
Solidifying efficiency；By carrying out first demisting and then the again control mode of indirect condensing to flue gas, the droplet in flue gas is removed, wet cigarette is strengthened
Gas is to the coalescence efficiency of fine particle, by multistage demisting, condensation, coalescence and trapping, it can be achieved that fine particle is arranged in wet flue gas
Concentration is put less than 0.1mg/Nm3。
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the capturing device of fine particle in wet flue gas；
Fig. 2 is the structural schematic diagram of condensing heat-exchange module；
Fig. 3 is the structural schematic diagram of level-one demister；
Fig. 4 is the structural schematic diagram of collecting tank and deflector；
Wherein, the appended drawing reference in figure is as follows:
1, scrubbing tower；2, Sprayer Circulation pumps；3, condensate circulation pumps；4, air cooling tower；1-1, gas inlet；1-2, washing spray
Drenching layer；1-3, cyclone cylinder deduster layer；1-4, indirect condensing layer；1-4-1, metal blade；1-4-2, condensate liquid circulation duct；
1-5, level-one demisting layer；1-5-1, demister modules；1-5-2, intake chute；1-5-3, draining plate；1-6, hydrops layer；1-6-1, it leads
Flowing plate； 1-6-2；Hydrops slot；1-7, packing layer；1-8, condensation spraying layer；1-9, second level demisting layer.
Specific embodiment
Present invention is further described in detail with reference to the accompanying drawings and examples, it should be pointed out that reality as described below
It applies example to be intended to convenient for the understanding of the present invention, and does not play any restriction effect to it.
As shown in Figure 1, in a kind of wet flue gas the capturing device of fine particle include scrubbing tower 1, Sprayer Circulation pump 2, it is air-cooled
Tower 4 and condensate circulation pump 3.
There is gas inlet 1-1, top has exhanst gas outlet, and tower bottom is tower reactor in the bottom sidewall of scrubbing tower 1.Scrubbing tower
1 inside and be located at gas inlet 1-1 above set gradually from the bottom to top wash spray layer 1-2, cyclone cylinder deduster layer 1-3,
Meet condensate layer 1-4, level-one demisting layer 1-5, hydrops layer 1-6, packing layer 1-7, condensation spraying layer 1-8 and second level demisting layer 1-9.
The inlet of wash spray layer 1-2 is connected to by Sprayer Circulation pump 2 with tower reactor, and Sprayer Circulation pump 2 is used for tower reactor
Interior cleaning solution is delivered to wash spray layer 1-2.
Cyclone cylinder deduster layer 1-3 is located above wash spray layer 1-2, apart from wash spray layer 1-2 0.5m-2m, whirlwind
The cylinder high 0.5m-2m of deduster, cyclone cylinder overcurrent gas velocity are 5m/s-10m/s.
Cyclone cylinder deduster layer is made of several cyclone cylinder dedusters up and down and fixed bottom plate, the fixed bottom plate
Outer and washing inner wall of tower are tightly connected, and the cyclone cylinder deduster, which runs through, to be fixed on fixed bottom plate；Each cyclone cylinder dedusting
Device is made of the swirl vane that cylinder and several layers are installed on inner barrel.
Risen to by wash spray layer 1-2 in the wet flue gas of cyclone cylinder deduster layer 1-3, the biggish particulate matter of partial size from
It is thrown toward cyclone wall under mental power function, is trapped by the liquid film on cyclone wall, while the vortex gas-flow of cyclone cylinder outlet
Reinforce the heat transfer effect of top indirect condensing layer 1-4 and flue gas, improves flue gas cool-down amplitude.
Indirect condensing layer 1-4 is located above cyclone cylinder deduster, apart from cyclone cylinder deduster 0.5m-1m.As shown in Fig. 2,
It is provided with several condensing heat-exchange modules in indirect condensing layer 1-4, each condensing heat-exchange module is equidistantly arranged vertically by several
Metal blade 1-4-1 and several layers equidistantly distributed and the condensate liquid circulation duct 1-4-2 composition for passing perpendicularly through metal blade；Gold
Belong to blade 1-4-1 with a thickness of 0.5-3mm, blade pitgh 20-80mm, indirect condensing layer height is 0.3m-0.6m, cigarette after heat exchange
Gas temperature drop is 0.5 DEG C -5 DEG C.
It is level-one demisting layer 1-5 above indirect condensing layer 1-4, level-one demister is set in level-one demisting layer 1-5, is highly
0.5m-1.5m。
As shown in figure 3, level-one demister height is 0.5m-1.5m, by demister modules 1-5-1, supporting beam, intake chute 1-
5-2 composition, demister modules 1-5-1 is placed in supporting beam and two adjacent demister modules form V-shaped；Intake chute 1-5-2
It is fixed in supporting beam, opening is located at the lower section of V-shaped bottom end；The opening of intake chute 1-5-2 has draining plate 1-5-3；
One end of intake chute 1-5-2 is equipped with the leakage fluid dram being connected to outside with tower.Demister modules 1-5-1 is made of folded sheet or corrugated sheet,
Folded sheet or waveform plate spacing are 5-20mm, and the slanted angle degree of demister modules and horizontal plane is 30-60 °.
Level-one demister captures the droplet containing particle dust, collects outside discharge scrubbing tower in time through intake chute 1-5-2,
Avoiding falling into scrubbing tower tower reactor causes dust in washing tower reactor accumulation.
As shown in figure 4, hydrops layer 1-6 is by several hydrops slot 1-6-2 being equidistantly evenly arranged and deflector 1-6-1 group
At deflector 1-6-1 is obliquely installed and bottom end is located in hydrops slot 1-6-2, the space part between two neighboring hydrops slot 1-6-2
It is divided into airflow channel.The ratio of airflow channel and hydrops slot 1-6-2 groove width is 0.5-1:1, deflector 1-6-1 and horizontal plane
Tilt angle is 40-70 °, and hydrops layer 1-6 height is 0.3-0.8m.
Packing layer 1-7 is erected at the top deflector 1-6-1, bed stuffing height 20-50cm, and filler material is metal material
Or nonmetallic materials, bed stuffing height 0.5m-2m.Packing layer 1-7 is tilted to be provided with honeycomb channels, honeycomb axially bored line with
Horizontal plane angle is 40-80 °.Honeycomb hole section is regular hexagon or circle, and section hole area is 15-50cm2.Two adjacent cells
Packing layer wall thickness between hole is 0.2-0.5mm.
Hydrops slot 1-6-2 collects condensate liquid, and deflector 1-6-1 plays guiding to flue gas and packing layer the 1-7 drop to fall
Effect, avoids hydrops slot 1-6-2 leakage.
Condensation spraying layer 1-8 is located at 0.5m-1.5m above packing layer, and condensation spraying layer 1-8 spray liquid-gas ratio is 0.5L/
Nm3-3.0L/Nm3, nozzle atomization pressure is 0.10MPa-0.30MPa, and flue gas cool-down amplitude is 5 DEG C -20 DEG C.
Second level demisting layer 1-9 is located above condensation spraying layer 1-8, is highly 0.2m-0.5m.Second level demisting layer 1-9 is used
Baffle plate demister, baffle plate are made of sheet metal, sheet metal thickness 0.2mm-2.0mm, between adjacent metal thin plate
Away from for 3mm-10mm.
The tower body of air cooling tower 4 is hyperbola tower body, be disposed in tower body from the bottom to top condensate liquid cooling packing layer and
Condensate liquid cooling spraying layer.The liquid inlet of condensate liquid cooling spraying layer and the liquid outlet of indirect condensing layer 1-4 and hydrops layer 1-6
Connection, indirect condensing layer 1-4 are higher than condensate liquid cooling spraying layer 10m-30m.The bottom of air cooling tower 4 passes through condensate circulation pump 3
With in scrubbing tower 1 indirect condensing layer 1-4 and condensation spraying layer 1-8 liquid inlet be connected to, by condensate circulation pump 3 to indirect cold
Solidifying layer 1-4 and condensation spraying layer 1-8 transporting low temperature condensate liquid.
Indirect condensing layer 1-4 and hydrops layer 1-6 collects the high temperature condensate liquid of discharge in scrubbing tower 1, in indirect condensing layer 1-
4, it under the action of the height pressure difference in hydrops layer 1-6 and air cooling tower 4 between condensate liquid cooling spraying layer, is sprayed by nozzle atomization,
Form fine drop in air cooling tower 4, fine drop and cold empty heat exchange cool down, and air themperature increases, air in air cooling tower 4 by
It is poor up to the lower certain Graded Density of formation, it is produced from pull out force and forms heat transfer free convection.The cooling extent of condensate liquid is 5 DEG C -20
℃.Condensate liquid after cooling is delivered to indirect condensing layer 1-4 and condensation spraying layer 1-8 by condensate circulation pump 3, realizes cold
Lime set low energy consumption recycles and flue gas cool-down.
The process flow for carrying out fine particle trapping in wet flue gas using above-mentioned apparatus is as follows:
Flue gas containing particulate matter and gaseous pollutants is entered scrubbing tower by the gas inlet 1-1 of scrubbing tower 1 and is flowed up,
Washing slurries in tower reactor are sent to wash spray layer 1-2 by Sprayer Circulation pump 2 and are atomized into drop falls downward, are carried out with flue gas
Reverse contact washing, removes the part large dust particle and gaseous pollutant in flue gas, and flue gas and the heat exchange of wash spray liquid are evaporated
Extremely close to saturation state (wet flue gas for containing only particulate matter can not set wash spray layer).The flue gas for completing wash spray enters whirlwind
Cylinder deduster layer 1-3, under the guide functions of cyclone cylinder swirl vane, flue gas carry a large amount of tiny sprayed slurry drops and
Grain object is thrown toward cylinder inboard wall under the action of the centrifugal force and is captured.The flue gas for completing cyclonic separation carries the fine grained for being difficult to remove
Object enters indirect condensing layer 1-4, carries out heat exchange drop with the internal cryogenic condensation heat exchange module equipped with condensate liquid circulation duct 1-4-2
Temperature, flue gas condensing to hypersaturated state, since slurry droplets a large amount of in flue gas have been removed, vapor condensation liquefaction process can only
It is condensed using the fine particle in flue gas as the nuclei of condensation, partial particulate object realizes volume and quality in Water vapor condensation process
Increased dramatically, and risen with condensing drops with air-flow, while under the guide functions of condensing heat-exchange module, flue gas stream
The equidistant vertically-mounted blade rectification in module that is condensed is uniform.The flue gas carrying for completing indirect condensing and rectification is a large amount of indirect
The condensation drop that condensation is formed enters level-one demisting layer 1-5, under the inertia and demister baffling guide functions of condensation drop, coagulates
Knot drop collides and is captured with demister blade, and forms liquid film in demister blade surface, finally in gravity
It is discharged outside scrubbing tower 1 into intake chute 1-5-2 by intake chute 1-5-2, the demister modules 1-5-1 for tilting installation is further increased
Flue gas circulation area improves demisting time and demisting efficiency.The flue gas for completing level-one demisting carries remaining thin not eliminated
Grain object passes through hydrops layer 1-6 and enters packing layer 1-7, and low temperature cold lime set is after condensation spraying layer 1-8 atomization along packing layer 1-7
Inclination honeycomb channel lower end flow downward, flue gas along inclination honeycomb channel upper end flow up, water temperature difference of being bullied influence, wet cigarette
Vapor in gas is further condensed by nuclei of condensation fast cooling of residual dust particulate matter, and the fine particle in flue gas is realized deep
Coalescence is spent to increase.The flue gas for completing depth coalescence carries condensation drop and sprays through the spray region condensation spraying layer 1-8 and low-temperature atomizing
Leaching drop further cools down, coalescence, after collision, the volume and quality for condensing drop further increase.Complete atomizing spray cooling
Flue gas afterwards carries condensation drop and enters second level demisting layer 1-9, under the inertia and demister baffling guide functions of condensation drop,
Condensation drop collides and is captured with demister blade, and forms liquid film in demister blade surface, finally makees in gravity
With hydrops layer 1-6 is entered, sent by pipeline to condensate liquid cooling spraying layer with condensation cycle liquid by hydrops layer 1-6 leakage fluid dram.It is complete
It is discharged at multistage demisting, condensation, coalescence and the clean flue gas of trapping by 1 exhanst gas outlet of scrubbing tower.
Low-temperature circulating condensate liquid, which is sent by condensate circulation pump 3 to indirect condensing layer 1-4 and condensation spraying layer 1-8, enters liquid
Mouthful, for reducing the temperature of indirect condensing layer 1-4, packing layer 1-7 and condensation spraying layer 1-8, the high temperature condensation for completing heat exchange is followed
Ring liquid send the cooling spraying layer of the condensate liquid into air cooling tower 4 by pipeline, and high temperature circulation condensate liquid is through condensate liquid cooling spraying layer mist
Enter condensate liquid cooling packing layer after change, cools down with the Cryogenic air heat exchange entered by 4 air inlet of air cooling tower, complete heat exchange and cool down
Low-temperature circulating condensate liquid fall under gravity into the condensate liquid storage pool of air-cooled tower bottom, by condensate circulation pump 3 send to
Indirect condensing layer 1-4 and condensation spraying layer 1-8 are recycled.
Technical solution of the present invention and beneficial effect is described in detail in embodiment described above, it should be understood that
Above is only a specific embodiment of the present invention, it is not intended to restrict the invention, it is all to be done in spirit of the invention
Any modification, supplementary, and equivalent replacement etc., should all be included in the protection scope of the present invention.
Claims (10)
1. the capturing device of fine particle in a kind of wet flue gas, which is characterized in that including scrubbing tower, Sprayer Circulation pump, air cooling tower
It is pumped with condensate circulation；
The washing tower side wall is equipped with smoke inlet, top is equipped with exhanst gas outlet, is partially tower reactor below smoke inlet；It is described
Wash spray layer, cyclone cylinder deduster layer, indirect condensing layer, level-one are set gradually by smoke inlet to exhanst gas outlet in scrubbing tower
Demisting layer, hydrops layer, packing layer, condensation spraying layer and second level demisting layer；
The air cooling tower includes tower body, and tower body bottom is equipped with air intake, and top is equipped with air outlet slit；In tower body from the bottom to top according to
Secondary setting condensate liquid storage pool, condensate liquid cooling packing layer and condensate liquid cooling spraying layer；
The liquid inlet of the wash spray layer is connected to by pipeline with Sprayer Circulation pump discharge, and the tower reactor passes through pipeline and spray
Pump inlet connection；
The leakage fluid dram for being equipped with below the level-one demisting layer and being connected to outside scrubbing tower；
It is equipped with leakage fluid dram below the hydrops layer, is connected to by pipeline with the liquid inlet of the condensate liquid of air cooling tower cooling spraying layer；
The indirect condensing layer, the liquid inlet for condensing spraying layer pump liquid outlet with condensate circulation by pipeline and are connected to, indirectly cold
Solidifying layer liquid outlet is connected to by pipeline with the liquid inlet of the condensate liquid of air cooling tower cooling spraying layer, air-cooled tower bottom condensate liquid storage
Pond pumps liquid inlet with condensate circulation by pipeline and is connected to.
2. the capturing device of fine particle in wet flue gas according to claim 1, which is characterized in that the cyclone cylinder dedusting
Device layer is made of several cyclone cylinder dedusters up and down and fixed bottom plate, and the fixed bottom plate outer and washing inner wall of tower are close
Envelope connection, the cyclone cylinder deduster, which runs through, to be fixed on fixed bottom plate；Each cyclone cylinder deduster is pacified by cylinder and several layers
Swirl vane composition loaded on inner barrel；
The spacing of the cyclone cylinder deduster layer and wash spray layer is 0.5m-2m, the high 0.5m-2m of cyclone cylinder deduster, whirlwind
Cylinder overcurrent gas velocity is 5m/s-10m/s.
3. the capturing device of fine particle in wet flue gas according to claim 1, which is characterized in that
Several condensing heat-exchange modules are equipped in the indirect condensing layer, each condensing heat-exchange module is by several equidistant vertical arrangements
Metal blade and several layers equidistantly distributed and pass perpendicularly through metal blade condensate liquid circulation duct composition；
Metal blade is 0.3m-0.6m with a thickness of 0.5mm-3mm, blade pitgh 20mm-80mm, indirect condensing layer height, is changed
The flue-gas temperature range of decrease is 0.5 DEG C -5 DEG C after heat.
4. the capturing device of fine particle in wet flue gas according to claim 1, which is characterized in that the level-one demisting layer
It is made of demister modules, supporting beam, intake chute, the inclination of several demister modules is symmetrically placed in supporting beam, and two adjacent remove
Day with fog module forms V-shaped；
Intake chute is fixed in supporting beam, and opening is located at below two adjacent demister modules bottom joining places；
The opening of the intake chute has draining plate；One end of intake chute is equipped with the leakage fluid dram being connected to outside with tower.
5. the capturing device of fine particle in wet flue gas according to claim 4, which is characterized in that the demister modules
It is made of folded sheet or corrugated sheet, folded sheet or waveform plate spacing are 5mm-20mm, and the inclination of demister modules and horizontal plane is pressed from both sides
Angle is 30 ° -60 °；The level-one demisting layer height is 0.5m-1.5m.
6. the capturing device of fine particle in wet flue gas according to claim 1, which is characterized in that if the hydrops layer by
The dry hydrops slot being equidistantly evenly arranged and deflector composition, deflector is obliquely installed and bottom end is located in hydrops slot, and adjacent two
Gap section between a hydrops slot is airflow channel；
The ratio of airflow channel and hydrops slot groove width is 0.5-1: 1, and the tilt angle of deflector and horizontal plane is 40 ° -70 °, product
Height of liquid layer is 0.3m-0.8m.
7. the capturing device of fine particle in wet flue gas according to claim 1, which is characterized in that described filler layer introversion
Tiltedly it is provided with several honeycomb channels；Honeycomb hole wall thickness is 0.2mm-0.5mm, and honeycomb hole section is regular hexagon or circle
Shape, section hole area are 15cm2-50cm2；Bed stuffing height is 20cm-50cm, honeycomb axially bored line angle with horizontal plane is 40 °-
80°。
8. the capturing device of fine particle in wet flue gas according to claim 1, which is characterized in that the condensation spraying layer
Spacing with packing layer is 0.5m-1.5m；The spray liquid-gas ratio for condensing spraying layer is 0.5L/Nm3-3.0L/Nm3, nozzle atomization pressure
Power is 0.10MPa-0.30MPa.
9. the capturing device of fine particle in wet flue gas according to claim 1, which is characterized in that the second level demisting layer
Height is 0.2m-0.5m；Baffle plate demister is set in second level demisting layer, and baffle plate is with a thickness of 0.2mm-2.0mm, adjacent baffling
Plate spacing is 3mm-10mm.
10. the capture method of fine particle in a kind of wet flue gas, which comprises the following steps:
(1) flue gas enters scrubbing tower by smoke inlet, and tower reactor slurries are after Sprayer Circulation is pumped to the atomization of wash spray layer to cigarette
Gas is washed, and gaseous pollutant and large dust particle are removed, and flue gas and cleaning solution heat exchange are condensed to saturation state；Saturated flue gas
Into cyclone cylinder deduster layer, goes down in eddy flow centrifugal action except the slurries droplet and large dust particle in flue gas, complete flue gas
The level-one trapping of middle fine particle (the wet flue gas processing for containing only particulate matter can not set wash spray layer)；
(2) flue gas for completing the trapping of particulate matter level-one enters the condensation of indirect condensing layer and is cooled to supersaturation, and vapor is with remaining
Fine particle is condensation karyogenesis liquid mist drop, and flue gas carries liquid droplet and enters level-one demisting layer, and liquid droplet is removed by level-one
The trapping of mist layer is simultaneously discharged outside scrubbing tower by intake chute, completes B-grade condensation, the coalescence, trapping of fine particle in flue gas；
(3) complete second level trapping wet flue gas carry a small amount of residual fine particles object pass through hydrops layer, packing layer, condensation spraying layer and
Second level demisting layer, with condensation spray liquid by indirect condensing in packing layer, vapor continues to remain fine particle as crystallization
Core condensation；Flue gas is contacted with low temperature spray liquid in condensation spraying layer continues deep condensation, and traps fine particle and condensate liquid
Drop；The flue gas for carrying residual droplet is discharged after second level demister layer demisting by exhanst gas outlet, and the three-level for completing fine particle is deep
Spend condensation, coalescence, trapping.
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| CN110772938A (en) * | 2019-11-01 | 2020-02-11 | 中冶东方工程技术有限公司 | Intensive smoke plume treatment and purification system and method |
| CN110882608A (en) * | 2019-11-27 | 2020-03-17 | 攀枝花市蓝鼎环保科技有限公司 | Flue gas desulfurization dust removal defogging coupled system |
| CN111773860A (en) * | 2020-06-05 | 2020-10-16 | 新兴河北工程技术有限公司 | Steel slag hot-braising and dedusting process and device |
| CN112275079A (en) * | 2020-11-20 | 2021-01-29 | 浙江富春江环保热电股份有限公司 | SO in flue gas after wet desulphurization3Device of high-efficient desorption |
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| CN111773860A (en) * | 2020-06-05 | 2020-10-16 | 新兴河北工程技术有限公司 | Steel slag hot-braising and dedusting process and device |
| CN112275079A (en) * | 2020-11-20 | 2021-01-29 | 浙江富春江环保热电股份有限公司 | SO in flue gas after wet desulphurization3Device of high-efficient desorption |
| CN112807913A (en) * | 2020-12-26 | 2021-05-18 | 界首市成铭塑业有限公司 | Visual plastics granulation flue gas intelligent processing device based on thing networking |
| CN112843964A (en) * | 2021-01-06 | 2021-05-28 | 东南大学 | Gravity flow type air dust removal device and method based on water vapor phase change |
| CN113101779A (en) * | 2021-04-14 | 2021-07-13 | 浙江理工大学 | System and method for purifying industrial flue gas containing sulfur and dust |
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| CN114838974A (en) * | 2022-03-10 | 2022-08-02 | 浙江大学 | Deep sea horizontal turbid flow particle collection device and collection method thereof |
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