CN112275079A - SO in flue gas after wet desulphurization3Device of high-efficient desorption - Google Patents
SO in flue gas after wet desulphurization3Device of high-efficient desorption Download PDFInfo
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- CN112275079A CN112275079A CN202011309383.2A CN202011309383A CN112275079A CN 112275079 A CN112275079 A CN 112275079A CN 202011309383 A CN202011309383 A CN 202011309383A CN 112275079 A CN112275079 A CN 112275079A
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- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
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- B03C1/30—Combinations with other devices, not otherwise provided for
Abstract
The invention discloses SO in flue gas after wet desulphurization3The device of high-efficient desorption, including the cylindric tower body, set up the flue gas import on the bottom of cylindric tower body or the lateral wall that the cylindric tower body is close to the bottom, set up the exhanst gas outlet at the top of cylindric tower body, supreme inertia defroster, agglomeration agent sprayer, the filler defroster, whirl electrostatic apparatus, the flusher of setting gradually are down followed to supreme in the inner chamber of cylindric tower body, and the inertia defroster is located the top of exhanst gas inlet, and the flusher is located the below of exhanst. The device realizes the ordered optimized combination of different sizes of SO through the inertia collision, the particle agglomeration, the filler absorption and filtration, the centrifugal force demisting and the electrostatic demisting3Particulate, different phase SO3The fine and effective removal is realized.
Description
Technical Field
The invention relates to the field of flue gas treatment, in particular to SO (sulfur dioxide) after wet desulphurization3The purification apparatus of (1).
Background
SO in combustion process3Mainly comprises the following parts: during high temperature combustion in a boiler, the sulfur content of the coal is oxidized, with a small portion (about 0.5% to 1.5%) being oxidized to SO3(ii) a SCR denitration reactor universally installed at tail of coal-fired boiler for reducing NOxDischarging V in catalyst installed in SCR denitration reactor2O5The component can catalyze SO in the flue gas2And partially oxidized to SO3. For coal-fired units not equipped with a denitration unit, SO3The yield of (a) accounts for 1% of the total sulfur content; for units equipped with SCR denitration apparatus, SO3The formation of (B) is higher, and usually 1.5-2% of the total sulfur content can be achieved. SO (SO)3The high concentration can cause the increase of the generation concentration of ammonium bisulfate, easily cause the blockage of the air preheater, the reduction of the availability ratio of the denitration device, the increase of the running resistance and the service life of the air preheater, the corrosion of a flue and the like.
At present, the electrostatic precipitator and the wet desulphurization tower are used for SO3The removal of (a) is incomplete. SO in flue gas3H formed by reaction with water vapour2SO4Fog drops are discharged into the atmosphere from a chimney, the opacity of the smoke is increased, a blue plume phenomenon appears, and H of a submicron level2SO4Acid mist discharged into the atmosphere can cause disastrous weather such as haze, acid rain and the like, and cause serious harm to human health. Thus realizing SO3The deep removal of the catalyst is significant to the safe and economic operation of a power plant and the improvement of the atmospheric environment.
SO in the present coal-fired flue gas3The removing method mainly comprises the following steps: (1) alkaline absorbent is sprayed in the flue behind the furnace, SO that SO in the flue gas can be effectively reduced3The content of (a). The sorbent injection location is primarily between the economizer and the SCR or between the SCR and the air preheater. The absorbent is sprayed after the economizer and before the SCR denitration system, SO that SO generated in the furnace can be avoided3And the catalyst enters an SCR reactor, so that the adverse effects of the generation of ammonium bisulfate on the catalyst and the denitration efficiency are reduced. The absorbent is sprayed into the flue between the SCR and the air preheater to remove SO3The problem of blockage of the air preheater caused by adhesion of ammonium bisulfate and ash in the air preheater can be effectively relieved. Spraying of absorbentThe position can also be between the air preheater and the electric dust remover and after the electric dust removal, and the SO removal can also be realized3Reduction of SO3Effect of total amount of emissions. However, the conveying of the powdery alkaline substance in the spraying process can not realize continuous and smooth feeding at present, the phenomena of hardening, discontinuous conveying and uneven spraying are easy to occur, and the absorbent can not be mixed with SO in the flue gas3The absorbent is excessively consumed and the removal efficiency is low due to full mixing and reaction, and the flue resistance is increased and the energy consumption is improved due to the fact that the spraying device occupies a large space; (2) and the tail part of the air preheater is subjected to removal by means of wet desulphurization. Conventional wet desulfurization of SO2Has high removal efficiency on SO3The removal efficiency is influenced by various factors such as unit installed capacity, load, coal quality, type of a desulfurizing tower and the like, and research results are not consistent. Generally, the flue gas is rapidly cooled in a wet absorption tower, and a large amount of SO3Submicron sulfuric acid mist aerosol particles which are difficult to be trapped are quickly generated without being absorbed, the dust concentration in the flue gas is low and is not enough to adsorb the sulfuric acid mist, SO the desulfurizing tower is used for SO3The removal efficiency is low. Research data based on actual measurement shows that WFGD system is to SO3The removal efficiency is lower than 35%.
At present, SO in flue gas after wet desulphurization in China3The content of (A) is 20-100 mg/m3There is still a small gap from the corresponding emission standards. For example, there are 22 states in the United states to coal burning power plants SO3Emission limit requirements are set forth, with 14 states having emission limits below 6mg/m3Florida is the most stringent, emission limit of 0.6mg/m3. Singapore regulated fixed source SO3The emission standard is 10mg/m3. In 2015, Shanghai City issued local Standard "air pollution Integrated emission Standard" (DB 31/933-2015), and regulated sulfuric acid mist emission limit to 5mg/m3. In recent years, part of local governments continuously release control requirements of colored smoke plume of coal-fired power plants, such as release of technical requirements (trial) for testing gypsum rain and colored smoke plume of coal-fired power plants in Shanghai city in 2017, release of emission standards of atmospheric pollutants of coal-fired power plants in Zhejiang province in 2018 (DB33/2147 and 2018), and the like. To this end, SO3Control is provided withWaiting for transformation and lifting.
In summary, various SOs are currently available3Both control and removal techniques have their applicability and limitations. At present, SO is realized by generally adopting a combined mode for flue gas3The removal, such as low-low temperature dust removal, wet desulphurization, wet static electricity and other overall process flue gas cooperative control technologies, but the technical system is more complex, the investment and operation costs are higher, and the SO3The removal efficiency is unstable and fluctuates between 60 and 90 percent. As the national emission requirements for coal-fired power plants become stricter, SO3Adverse effects of generation and emission are urgently needed to be solved and research and develop low-cost, efficient and stable SO3The control device is at hand.
Disclosure of Invention
The invention aims to solve the technical problem of providing SO obtained after wet desulphurization3High-efficient desorption device.
In order to solve the problem, the invention provides a method for removing SO in flue gas after wet desulphurization3The device of high-efficient desorption:
the device comprises a cylindrical tower body, wherein a flue gas inlet is formed in the bottom of the cylindrical tower body or the side wall of the cylindrical tower body close to the bottom, a flue gas outlet is formed in the top of the cylindrical tower body, and the flue gas inlet and the flue gas outlet are communicated with an inner cavity of the cylindrical tower body;
set gradually inertia defroster, aggregating agent sprayer, filler defroster, whirl electrostatic apparatus, flusher from supreme down in the inner chamber of cylindric tower body, the inertia defroster is located the top of flue gas inlet, and the flusher is located the below of exhanst gas outlet.
SO in flue gas after wet desulphurization3Improvement of the device for high-efficiency removal:
when the device is used as a matched device directly arranged at the top end of a conventional wet desulphurization tower:
the bottom surface of the cylindrical tower body is provided with a through hole, so that a flue gas inlet is formed, and the flue gas inlet is communicated with the top of the conventional wet desulphurization tower.
SO in flue gas after wet desulphurization3Improvement of the device for high-efficiency removal:
when acting as a stand-alone reactor:
because the cylindrical tower body is provided with the bottom surface, the inner cavity at the bottom of the cylindrical tower body is used as a liquid collecting pool, and a liquid outlet is arranged on the side wall of the cylindrical tower body corresponding to the liquid collecting pool; a flue gas inlet is arranged on the side wall of the cylindrical tower body close to the bottom, and the flue gas inlet is positioned above the liquid collecting tank; the flue gas inlet inclines downwards 5-10 degrees.
When in actual use, the solution in the liquid collecting tank can be pumped into the desulfurizing tower slurry tank through the liquid outlet by using the slurry pump.
SO in flue gas after wet desulphurization3Further improvement of the device for efficient removal:
the inertia demister consists of at least one layer (one group) of corrugated plate demisters; the empty tower flow velocity of the cylindrical tower body is 2.5-3.5 m/s.
When the wave-shaped plate demister is more than or equal to 2 layers (2 groups), the wave-shaped plate demister is overlapped up and down.
SO in flue gas after wet desulphurization3Further improvement of the device for efficient removal:
in each layer of corrugated plate demister, the height of the blades is 200-300 mm, the distance is 20-40 mm, and the thickness is 3-4 mm.
Therefore, when the inertia demister consists of 5 groups of single-stage corrugated plate demisters which are stacked up and down, the total height of the inertia demister is generally 1-1.5 m, and the residence time is about 0.4-0.6 s calculated by the empty tower flow velocity of 2.5 m/s.
The inertia demister can realize primary demisting and remove SO3Large droplets of (a).
SO in flue gas after wet desulphurization3Further improvement of the device for efficient removal:
an agglomeration agent ejector is arranged 20-50 mm above the inertia demister; the agglomeration agent ejector sprays agglomeration agent solution to the flue gas passing through the inertia demister; the mass concentration of the agglomeration agent in the agglomeration agent solution is 0.05-0.1 g/L (conventional high-molecular solvent is adopted, so that the agglomeration agent can be dissolved);
the agglomerating agent is any one of the following:
a mixture of the agglomeration agent KC and the agglomeration agent LBG with the same mass,
or a mixture of the agglomeration agent KC and the agglomeration agent KGM in equal mass;
the agglomeration agent sprayer adopts a two-fluid atomizing nozzle, the atomizing particle size of the two-fluid atomizing nozzle is less than or equal to 10um, and the spraying angle (spraying included angle) is 80-100 degrees; the spraying coverage rate is more than or equal to 150 percent.
The two-fluid atomizing nozzles may be designed to be evenly arranged within the cross-section of the cylindrical tower along the dendritic structure (i.e., the ends of the branches are provided as nozzles).
The number of nozzles is calculated according to the coverage rate and the spray angle, and then the nozzles are uniformly arranged, which is a conventional technology.
SO in flue gas after wet desulphurization3Further improvement of the device for efficient removal:
the packing demister consists of a grid plate bracket and a packing layer;
a grid plate bracket is arranged above the agglomerating agent injector, and the distance between the grid plate bracket and the agglomerating agent injector is 200 +/-50 mm;
a packing layer with the height of 300 +/-50 mm is paved on the upper surface of the grid plate bracket; the packing in the packing layer is pall ring or step ring packing.
SO in flue gas after wet desulphurization3Further improvement of the device for efficient removal:
a rotational flow static device is arranged above the packing demister;
the rotational flow electrostatic device consists of a plurality of discharge tubes which are parallel to each other and have a line tube type structure; each discharge tube is used as a discharge unit of the rotational flow electrostatic device, and the central axis of each discharge tube is parallel to the central axis of the cylindrical tower body.
SO in flue gas after wet desulphurization3Further improvement of the device for efficient removal:
the discharge tube comprises a circular tube-shaped (no top surface and no bottom surface) electrode cylinder, the diameter of the electrode cylinder is 150-250 mm, the material of the electrode cylinder is stainless steel, and the electrode cylinder is grounded;
arranging a discharge electrode at the axial lead of the electrode cylinder, namely, the discharge electrode is coincided with the axial lead of the electrode cylinder; the discharge electrode adopts a bur type structure and is connected with negative high voltage;
the bottom, the middle and the upper part of the electrode barrel are respectively sleeved with a rotational flow plate, and the axial lead of the rotational flow plate is superposed with the discharge electrode; the inclination angle of the blades of the rotational flow plate and the horizontal plane is 30-45 degrees, and the included angle of the blades of the rotational flow plate and the axial lead is 45-60 degrees; the top of the electrode cylinder is provided with an air outlet; the flue gas enters the electrode cylinder from the inlet of the cyclone plate at the bottom of the electrode cylinder, and forms spirally rising air flow under the action of the cyclone plate, and the centrifugal force generated by the air flow can make part of SO in the flue gas3The particles migrate to the electrode cylinder; simultaneously the discharge electrode starts corona discharge to make SO3The particles are charged with electrons, thus electrostatic adsorption is generated and the particles migrate to the electrode cylinder to be trapped, pass through the cyclone plate and the discharge electrode, and SO in the flue gas3The particles are removed efficiently; the treated flue gas is discharged from an outlet of the cyclone plate positioned at the upper part of the electrode cylinder;
the average flow velocity of the flue gas in the electrode cylinder is controlled to be 0.8-1 m/s, and the retention time is 2-3 s.
The discharge tube with the cyclone structure can not only realize the centrifugal removal of larger particles, but also remove fine particles through wet electrostatic dust removal; the influence of the size structure of the cyclone plate on the rotational speed is better, and the larger the rotational speed is, the better the particle removal effect is.
The device realizes the ordered optimized combination of different sizes of SO through the inertia collision, the particle agglomeration, the filler absorption and filtration, the centrifugal force demisting and the electrostatic demisting3Particulate, different phase SO3Refining of (1) removing SO efficiently3The removal efficiency reaches more than 95 percent, and is improved for improving SO in the flue gas after wet desulphurization3Provide new approaches and methods. The invention firstly adopts an inertia demister to remove large liquid drops, then agglomerant solution liquid drops and aerosol SO3Greatly enhances the contact probability of the sulfur and promotes SO3And (3) agglomeration. The filling layer can not only strengthen the gaseous SO3And for agglomerated liquid SO3The particles having a filtering action, SO3The removal effect is further enhanced. The rotational flow electrostatic apparatus is adopted, SO that large agglomerated particles can be removed through centrifugal force, and SO can be efficiently removed through electrostatic force3The aerosol small particles achieve the effect of fine demisting and can remove low-concentration SO3The removal effect of (2) is remarkably enhanced.
The invention has the following technical advantages:
1. the invention combines inertia collision, particle agglomeration, filler absorption and filtration, centrifugal force demisting and electrostatic demisting in a tower in order, can be used for the reconstruction of the original desulfurizing tower and can also be directly used for SO after the desulfurizing tower3Is removed separately.
2. The processes of inertial collision, particle agglomeration, filler absorption and filtration, centrifugal force demisting, electrostatic demisting and the like can be reasonably configured and combined according to the emission concentration and the standard of the actual engineering SO3, and the investment cost and the operation cost are reduced on the basis of stably reaching the standard.
3. The rotational flow electrostatic tube adopts a rotational flow plate and corona discharge synergistic mode, and can realize SO under the simultaneous action of centrifugal force and electrostatic force3The efficient removal of the organic-inorganic composite material is realized, namely, the organic combination of centrifugal SO3 removal and electrostatic SO3 removal is realized.
4. The reasonably prepared agglomerant can promote SO3Agglomeration of the aerosol to form particles of larger particle size to improve SO of the subsequent filler filter layer and cyclone electrostatic tube3And (4) removing effect.
5. The filler filter layer can not only promote SO3And can promote SO3The aerosol is filtered by collision, the device is simple, and SO is effectively reduced3The concentration of (c).
Drawings
The following describes embodiments of the present invention in further detail with reference to the accompanying drawings.
FIG. 1 shows SO in flue gas after wet desulfurization3The structure schematic diagram of the device for high-efficiency removal;
fig. 2 is an enlarged schematic structural view of one discharge unit of the swirling electrostatic device 4 of fig. 1.
Detailed Description
The invention will be further described with reference to specific examples, but the scope of the invention is not limited thereto:
example 1 SO in flue gas after Wet desulfurization3The device of high-efficient desorption, as independent reactor:
the tower comprises a cylindrical tower body 100, wherein the cylindrical tower body 100 is provided with a bottom surface, so that an inner cavity at the bottom of the cylindrical tower body 100 is used as a liquid collecting pool 103, and a liquid outlet 104 is arranged on the side wall of the cylindrical tower body 100 corresponding to the liquid collecting pool 103; a flue gas inlet 101 is arranged on the side wall of the cylindrical tower body 100 close to the bottom, and the flue gas inlet 101 is positioned above the liquid collecting tank 103 (i.e. above the liquid outlet 104); the flue gas inlet 101 inclines downwards 5-10 degrees.
The top of the cylindrical tower body 100 is provided with a flue gas outlet 102, and therefore, the flue gas inlet 101 and the flue gas outlet 102 are both communicated with the inner cavity of the cylindrical tower body 100.
After wet desulfurization, the flue gas enters the cylindrical tower body 100 from the flue gas outlet 102.
The inner cavity of the cylindrical tower body 100 is internally provided with an inertia demister 1, an agglomeration agent sprayer 2, a filler demister 3, a cyclone electrostatic apparatus 4 and a flusher 5 from bottom to top in sequence, the inertia demister 1 is positioned above the flue gas inlet 101, and the flusher 5 is positioned below the flue gas outlet 102.
The inertia demister 1 consists of at least 2 layers (2 groups) of corrugated plate demisters which are stacked up and down; the empty tower flow velocity of the cylindrical tower body 100 is 2.5-3.5 m/s.
In each layer of corrugated plate demister, the height of the blades is 200-300 mm, the distance is 20-40 mm, and the thickness is 3-4 mm. Therefore, when the inertia demister 1 is composed of 5 groups of single-stage corrugated plate demisters stacked up and down, the total height of the inertia demister 1 is generally 1-1.5 m, and the residence time is about 0.4-0.6 s calculated by the empty tower flow rate of 2.5 m/s.
The inertia demister 1 can realize primary demisting and remove SO through collision of particles and corrugated plates3Large droplets, concentration of droplets after inertial demisting<100mg/Nm3。
An agglomeration agent ejector 2 is arranged 20-50 mm above the inertia demister 1; the agglomeration agent ejector 2 ejects an agglomeration agent solution to the flue gas passing through the inertia demister 1; the mass concentration of the agglomeration agent in the agglomeration agent solution is 0.05-0.1 g/L;
the agglomerating agent is any one of the following:
a mixture of the agglomeration agent KC and the agglomeration agent LBG with the same mass,
or a mixture of the agglomeration agent KC and the agglomeration agent KGM in equal mass;
the agglomeration agent sprayer 2 adopts a two-fluid atomizing nozzle, the atomizing particle size of the two-fluid atomizing nozzle is less than or equal to 10um, and the spraying angle (spraying included angle) is 80-100 degrees; the nozzles are uniformly arranged in the section of the cylinder along the dendritic structure, so that the spraying coverage rate reaches 150% or more. That is, the two-fluid atomizing nozzle may be designed to be evenly arranged within the cross-section of the cylindrical tower along the dendritic structure, i.e., the end of the tree branch is provided as a nozzle. The number of nozzles is calculated according to the coverage rate and the spray angle, and then the nozzles are uniformly arranged, which is a conventional technology.
The agglomeration agent used in the invention can generate synergistic effect; KC enlarges the particle size, LBG and KGM not only enlarge the particle size of the particles, but also change the particle size distribution to be normal; the chemical agglomeration technology is to utilize long polymer chain with polar group to neutralize and adsorb PM2.5 or SO in bridging mode3Connection promotes PM2.5 and SO3And (4) agglomeration and growth. That is, the agglomerating agent can promote the agglomeration of the nano-sized particles into micron-sized particles, and meanwhile, the particle size distribution of the particles tends to be normal distribution, so that the particles are easier to remove.
The agglomerant solution eventually falls into the liquid collection sump 103.
The packing demister 3 consists of a grid plate bracket 31 and a packing layer 32; a grid tray 31 is arranged above the agglomerating agent injector 2, and the distance between the grid tray and the agglomerating agent injector 2 is 200 +/-50 mm; a filler layer 32 with the height of 30 +/-500 mm is paved on the upper surface of the grid plate bracket 31; the packing in the packing layer 32 is pall ring or step ring packing. The flue gas treated by the agglomerating agent ejector 2 continuously passes through the filler layer 32; the filler layer 32 enhances gas-liquid mass transfer and enhances absorption of gaseous SO3(ii) a At the same time, the particles collide with the filler to remove SO3Liquid droplets of。
A rotational flow electrostatic layer 4 is arranged above the filler demister 3; the discharge unit of the rotational flow electrostatic layer 4 is of a wire tube structure, and the bottom of the discharge tube is sleeved with a rotational flow plate. The method comprises the following specific steps:
the rotational flow electrostatic layer 4 is composed of a plurality of discharge tubes 40 with mutually parallel tubular structures; each discharge tube 40 serves as a discharge unit of the swirling electrostatic layer 4, and the central axis of the discharge tube 40 is parallel to the central axis of the cylindrical tower body 100.
The discharge tube 40 comprises a circular tube-shaped electrode cylinder 41 without a top surface and a bottom surface, the electrode cylinder 41 is a circular tube with the diameter of 150-250 mm and made of stainless steel, and the electrode cylinder 41 is grounded;
a discharge electrode 42 is arranged at the axial lead of the electrode cylinder 41 and is a wire electrode, and the discharge electrode 42 is coincided with the axial lead of the electrode cylinder 41; the discharge electrode 42 adopts a bur type structure, and the discharge electrode 42 is connected with negative high voltage;
the bottom, the middle part and the upper part of the electrode cylinder 41 are respectively sleeved with a cyclone plate 43 (for the sake of clarity of the drawing, in fig. 2, only the cyclone plate 43 at the bottom of the electrode cylinder 41 is shown) which is a planar cyclone plate, and the axial lead of the cyclone plate 43 is coincident with the discharge electrode 42; the swirl plate 43 takes the discharge electrode 42 as a rotating shaft, and the rotating shaft is welded and fixed with the center of the swirl plate 43; the inclination angle of the blades of the rotational flow plate 43 and the horizontal plane is 30-45 degrees, and the included angle of the blades and the rotating shaft is 45-60 degrees; the top of the electrode cylinder 41 is an air outlet. The working process is as follows: the flue gas treated by the filler layer 32 enters the electrode cylinder 41 from the inlet of the cyclone plate 43 at the bottom of the electrode cylinder 41, and forms a spirally rising air flow under the action of the cyclone plate 43, and the centrifugal force generated by the air flow can make part of SO in the flue gas3The particles migrate to the electrode cylinder 41; while the discharge electrode 42 starts corona discharge to make SO3The particles are charged with electrons, thus electrostatic adsorption is generated and the particles migrate to the electrode cylinder 41 to be trapped, and SO in the flue gas is generated through the cooperation of the cyclone plate 43 and the discharge electrode 423The particles are removed efficiently; the treated flue gas is discharged from the outlet of the cyclone plate 43 located at the upper part of the electrode barrel 41. The average flow velocity of the flue gas in the electrode cylinder 41 is controlled to be 0.8-1 m/s, and the retention time is 2-3 s.
Between the outer surfaces of adjacent discharge tubes 40 is a baffle structure so that the flue gas must pass through the discharge tubes 40.
A flusher 5 is arranged above the rotational flow static device 4, the arrangement of the flusher 5 belongs to the conventional technology, and a large amount of flushing water is regularly sprayed; the resulting rinse liquid falls into the liquid collection tank 103. The solution (the solution of the agglomerating agent and the low concentration H) in the liquid collection tank 103 can be collected by a slurry pump2SO4) is pumped into a slurry pool of the desulfurizing tower.
The flue gas treated by the device of the invention is finally discharged from the flue gas outlet 102.
The specific parameters are as follows:
the inertia defroster 1 adopts single-stage corrugated plate defroster, comprises 5 groups of single-stage corrugated plate defroster, and the overall height is about 1m, and the empty tower velocity of flow is 2.5m/s, and dwell time is 0.4 s.
The agglomerating agent is KC: LBG is 1:1 mass ratio, and the total mass concentration is controlled to be 0.1 g/L; the agglomeration agent is sprayed by a two-fluid atomizing nozzle, the atomizing particle size is 10 mu m, the spraying angle is 90 degrees, and the spraying coverage rate reaches 150 percent. Arranging a grating plate bracket 31 200mm above the spraying layer, and paving a filler layer 32 with the height of 300mm on the upper surface of the grating plate bracket 31; the filler adopts pall ring filler. A rotational flow static device 4 is arranged above the packing layer 32, the discharge tube is a stainless steel round tube with the diameter of 200mm, and the discharge tube is grounded. The line electrode adopts a bur type structure and is connected with negative high voltage. The average flow velocity of the flue gas in the electrode cylinder is controlled to be 1m/s, and the retention time is 2 s. The inclination angle of the blades of the rotational flow plate and the horizontal plane is 45 degrees, and the included angle of the blades of the rotational flow plate and the rotating shaft is 45 degrees.
The original flue gas after wet desulphurization is as follows: fog drop content 152mg/Nm3，SO3Concentration 48mg/Nm3；
The treated flue gas discharged from the flue gas outlet 102 has various performance indexes as follows: the content of fogdrops is 25mg/Nm3，SO3Concentration 4mg/Nm3；
Comparative example 1-1, the use of the entire agglomeration agent injector 2 was eliminated, and the remainder was identical to experiment 1.
From flue gasTreated flue gas exiting port 102: fog drop content of 79mg/Nm3，SO3Concentration 23mg/Nm3。
Comparative examples 1-2, the entire packing mist eliminator 3 was removed, and the remainder was identical to experiment 1.
Treated flue gas exiting the flue gas outlet 102: fog drop content of 72mg/Nm3，SO3Concentration 16mg/Nm3。
Comparative examples 1 to 3, only one swirl plate 43 was provided at the bottom of the electrode cylinder 41, i.e., the swirl plates 43 located at the middle and upper portions of the electrode cylinder 41 were removed, and the rest was identical to experiment 1.
Treated flue gas exiting the flue gas outlet 102: fog drop content 52mg/Nm3，SO3Concentration 18mg/Nm3。
Comparative example 2-1, the agglomeration agent KC in experiment 1: the LBG mass ratio was changed to 1:2, and the rest was identical to experiment 1. Treated flue gas exiting the flue gas outlet 102: the content of fogdrops is 30mg/Nm3，SO3Concentration 13mg/Nm3。
Comparative example 2-2, the concentration of the agglomerating agent in experiment 1 was changed to 0.03g/L, and the remainder was identical to experiment 1.
Treated flue gas exiting the flue gas outlet 102: the content of fogdrops is 31mg/Nm3，SO3Concentration 12mg/Nm3。
Comparative examples 2 to 3, the atomized particle size of the agglomerating agent in experiment 1 was changed to 15um, and the remainder was the same as experiment 1.
Treated flue gas exiting the flue gas outlet 102: the content of fogdrops is 28mg/Nm3，SO3Concentration 10mg/Nm3。
Description of the drawings: when the device is arranged at the top end of the conventional wet desulphurization tower for matched use (the device is arranged at the top of the conventional wet desulphurization tower after the liquid collection pool is removed), the obtained effect is basically equal to that when the device is used as an independent reactor.
Finally, it is also noted that the above-mentioned lists merely illustrate a few specific embodiments of the invention. It is obvious that the invention is not limited to the above embodiments, but that many variations are possible. All modifications which can be derived or suggested by a person skilled in the art from the disclosure of the present invention are to be considered within the scope of the invention.
Claims (9)
1. SO in flue gas after wet desulphurization3The device of high-efficient desorption, its characterized in that:
the device comprises a cylindrical tower body (100), wherein a flue gas inlet (101) is formed in the bottom of the cylindrical tower body (100) or the side wall of the cylindrical tower body (100) close to the bottom, a flue gas outlet (102) is formed in the top of the cylindrical tower body (100), and the flue gas inlet (101) and the flue gas outlet (102) are communicated with an inner cavity of the cylindrical tower body (100);
the device is characterized in that an inertia demister (1), an agglomeration agent sprayer (2), a filler demister (3), a cyclone electrostatic device (4) and a flusher (5) are sequentially arranged in an inner cavity of a cylindrical tower body (100) from bottom to top, the inertia demister (1) is located above a flue gas inlet (101), and the flusher (5) is located below a flue gas outlet (102).
2. SO in flue gas after wet desulphurization according to claim 13The device of high-efficient desorption, its characterized in that:
as a device which is directly arranged at the top end of a conventional wet desulphurization tower and is used together with the wet desulphurization tower:
and a through hole is formed in the bottom surface of the cylindrical tower body (100) so as to form a flue gas inlet (101), and the flue gas inlet (101) is communicated with the top of the conventional wet desulphurization tower.
3. SO in flue gas after wet desulphurization according to claim 13The device of high-efficient desorption, its characterized in that:
as independent reactors:
because the cylindrical tower body (100) is provided with the bottom surface, the inner cavity at the bottom of the cylindrical tower body (100) is used as a liquid collecting pool (103), and a liquid outlet (104) is arranged on the side wall of the cylindrical tower body (100) corresponding to the liquid collecting pool (103); a flue gas inlet (101) is arranged on the side wall of the cylindrical tower body (100) close to the bottom, and the flue gas inlet (101) is positioned above the liquid collecting tank (103); the flue gas inlet (101) inclines downwards by 5-10 degrees.
4. The method for removing SO in flue gas after wet desulphurization according to any one of claims 1 to 33The device of high-efficient desorption, its characterized in that:
the inertia demister (1) consists of at least one layer of corrugated plate demister; the empty tower flow velocity of the cylindrical tower body (100) is 2.5-3.5 m/s.
5. SO in flue gas after wet desulphurization according to claim 43The device of high-efficient desorption, its characterized in that: in each layer of corrugated plate demister, the height of the blades is 200-300 mm, the distance is 20-40 mm, and the thickness is 3-4 mm.
6. SO in flue gas after wet desulphurization according to claim 43The device of high-efficient desorption, its characterized in that:
an agglomeration agent ejector (2) is arranged 20-50 mm above the inertia demister (1); the agglomeration agent ejector (2) ejects an agglomeration agent solution to the flue gas passing through the inertia demister (1); the mass concentration of the agglomeration agent in the agglomeration agent solution is 0.05-0.1 g/L
The agglomerating agent is any one of the following:
a mixture of the agglomeration agent KC and the agglomeration agent LBG with the same mass,
or a mixture of the agglomeration agent KC and the agglomeration agent KGM in equal mass;
the agglomeration agent sprayer (2) adopts a two-fluid atomizing nozzle, the atomizing particle size of the two-fluid atomizing nozzle is less than or equal to 10um, and the spraying angle is 80-100 degrees; the spraying coverage rate is more than or equal to 150 percent.
7. SO in flue gas after wet desulphurization according to claim 43The device of high-efficient desorption, its characterized in that:
the packing demister (3) consists of a grid plate bracket (31) and a packing layer (32);
a grid plate bracket (31) is arranged above the agglomerating agent injector (2), and the distance between the grid plate bracket and the agglomerating agent injector (2) is 200 +/-50 mm;
a filler layer (32) with the height of 300 +/-50 mm is paved on the upper surface of the grid plate bracket (31); the packing in the packing layer (32) is pall ring or step ring packing.
8. SO in flue gas after wet desulphurization according to claim 43The device of high-efficient desorption, its characterized in that:
a rotational flow static device (4) is arranged above the filler demister (3);
the rotational flow electrostatic device (4) is composed of a plurality of discharge tubes (40) which are parallel to each other and have a linear tube structure; each discharge tube (40) is used as a discharge unit of the cyclone electrostatic device (4), and the central axis of each discharge tube (40) is parallel to the central axis of the cylindrical tower body (100).
9. SO in flue gas after wet desulphurization according to claim 83The device of high-efficient desorption, its characterized in that:
the discharge tube (40) comprises a tubular electrode cylinder (41), the diameter of the electrode cylinder (41) is 150-250 mm, the electrode cylinder is made of stainless steel, and the electrode cylinder (41) is grounded;
a discharge electrode (42) is arranged at the axial lead of the electrode cylinder (41), the discharge electrode (42) adopts a bur type structure, and the discharge electrode (42) is connected with negative high voltage;
the bottom, the middle part and the upper part of the electrode barrel (41) are respectively sleeved with a rotational flow plate (43), and the axial lead of the rotational flow plate (43) is superposed with the discharge electrode (42); the inclination angle of the blades of the rotational flow plate (43) and the horizontal plane is 30-45 degrees, and the included angle of the blades and the axial lead is 45-60 degrees; the top of the electrode cylinder (41) is an air outlet; the flue gas enters the electrode cylinder (41) from the inlet of the cyclone plate (43) positioned at the bottom of the electrode cylinder (41), and forms spirally rising airflow under the action of the cyclone plate (43), and the centrifugal force generated by the airflow can enable part of SO in the flue gas3The particles migrate to the electrode cylinder (41); simultaneously the discharge electrode (42) starts corona discharge to make SO3The particles are charged with electrons, thus electrostatic adsorption is generated, the particles migrate to the electrode cylinder (41) to be trapped, SO in the flue gas passes through the cyclone plate (43) and the discharge electrode (42)3The particles are removed efficiently; the treated flue gas is discharged from an outlet of a cyclone plate (43) positioned at the upper part of the electrode cylinder (41);
the average flow velocity of the flue gas in the electrode cylinder (41) is controlled to be 0.8-1 m/s, and the retention time is 2-3 s.
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