CN106693590A - Fine particle polymerizer and high-efficiency dedusting defogging integrated system - Google Patents

Abstract

The invention discloses a polymerizer for polymerization of fine particles; the polymerizer includes one or more cyclone devices, and each cyclone device comprises at least two rotational flow vanes; the rotational flow vanes are set to make a gas flow containing fine particles to form a rotary gas flow by the cyclone devices. The invention also provides a dedusting defogging integrated system comprising the polymerizer and an integrated dedusting defogging method. The high-efficiency dedusting defogging integrated system can effectively remove most of PM2.5 fine dust in the gas flow, and has quite high practical application value on governance of the fine particles in flue gas; moreover, the system is low device investment cost, low in energy consumption, and long-term running reliability, and can be used in the fields of flue gas purification of thermal power plants, steel plants, paper-making factories, glass factories, chemical plants and production workshops with particle emissions and the like.

Description

Fine particle polymerizer and high-effective dust-removing demisting integral system

Technical field

It is used for thermal power plant, steel plant, paper mill, glass the present invention relates to filed of flue gas purification, more particularly to one kind Fine particle polymerizer and dedusting demisting integral system in the exhaust treatment systems such as glass factory, chemical plant.

Background technology

To realize the ultra-clean discharge even near-zero release of coal-fired station, country proposes " 50355 " index, i.e., The soot emissions of coal-fired station are asked to be respectively smaller than 5mg/Nm³(reaching Gas Generator Set standard), sulfur dioxide SO₂ Discharge standard be less than 35mg/Nm³, nitrogen oxides NO_XConcentration is less than 50mg/Nm³。

To realize that dust concentration reaches ultra-clean discharge even near-zero release standard, because wet electrical dust precipitator investment is big, fortune The corrosion of new pollutant, positive plate is brought when row high energy consumption, bulky, auxiliary chemical consumption amount Datong District A series of problems, such as allow many thermal power plants to hang back.

But how to realize that non-wet electrical dust precipitator is issued to flue dust outlet drain less than 5mg/Nm³Standard is new skill Art problem.There is a little environmental improvement enterprise to propose " collaboration resolution " scheme at present, make using with high-effective dust-removing Wet desulfurization system (technology, the three-layer efficient demister such as subregion, setting pallet or rotation remittance coupling in single column, tower), While high-efficiency desulfurization is realized, the dust efficient removal of desulphurization system will be entered, realize the dedusting of desulphurization system >=70% Efficiency.

And state the main cause of wet desulfurization system high-effective dust-removing functional realiey：

(1) slurries particle diameter reduction by 30% is improved by the dust supplementary set ability of slurries using high performance nozzle.

(2) liquid film layer formed by technologies such as pallets, increases supplementary set ability of the liquid film to fine dust.

(3) absorption tower sets three-layer efficient demister, by absorption tower exiting flue gas concentration of liquid drops control in 20mg/Nm³ Hereinafter, the gypsum particle thing carrying amount of flue gas is greatly reduced.

Knowable to data above, when desulfurization Inlet dust is 20mg/Nm³When, even if desulphurization system realizes that >=70% goes Dirt rate, that is, the dust concentration for entering into high efficiency demister can still reach 6mg/Nm³, but high efficiency demister is only Have to slurry droplet and intercept removal effect well, even if reaching 20mg/Nm³Concentration of liquid drops, these residual solutions Drop contains gypsum and other solid and soluble-salt, is calculated according to minimum 7% solid concentration, and newly-increased dust content is 1.4mg/Nm³, therefore exit concentration will be controlled in 5mg/Nm³, it is necessary to it is required that high efficiency demister is to dust from 6mg/Nm³ Further it is removed to 3.6mg/Nm³Within, that is, requiring that high efficiency demister reaches more than 40% to dust dust removal rate, this is Do not meet completely it is actual, and remnants 6mg/Nm³Almost be smaller than 5 microns of fine solid particle, through research and Test result indicate that high efficiency demister (three-level roof demister) at most can be by dust from 6mg/Nm³It is reduced to 5.6mg/Nm³, dust removal has little effect！

In addition, co-publicated by Chemical Industry Press and Environmental Science and Engineering publishing centre in 2002《It is coal-fired The out of stock technology of flue gas desulfurization and case history》A kind of rotational flow plate defroster is taught in one book, it is made using eddy flow plate Air-flow is rotated, and rotation produces centrifugal force so as to be thrown toward to the drop being entrained in swirling eddy at a high speed in whirl cylinder On cylinder inner wall, so as to realize gas-liquid separation effect, the rotational flow plate defroster necessarily requires enough outer barrels highly, And its function is that be thrown on barrel droplet so as to realize gas-liquid separating function by the centrifugal force produced using spiral board.

Again, the application in number of patent application 201520058549.6 (a kind of high-effective dust-removing demisting integral system) One kind condensation wet film high-effective dust-removing demisting technology, in hollow corrugated plating Internal Cooling Passage medium, will be thin by condensing mode Micro mist dirt and drop are amplified, and separation is then removed to it by the superfinishing fine separator of downstream position.

The condensation wet film centrifugal dust-removing demisting technology belongs to huge technological innovation in smoke and dust treatment field, but to pole Its fine solid particle and drop, such as particle diameter are even less than 0.5 micron of dust and drop less than 1 micron, even if amplifying Still it is difficult to be removed by follow-up hyperfine separation afterwards and separates, therefore for further depth improves extremely fine solid particle and liquid The removal of drop, it is necessary to further improved the condensation wet film technology.

Therefore, solution is needed with following technical problem in the prior art：

1. flue dust exit concentration is administered using " collaboration resolution " and be less than 5mg/Nm³Unrealistic property, it is or more accurate Really saying that " collaboration resolution " does not have ensures that flue dust exit concentration is less than 5mg/Nm³Science certainty.

2. (such as dust inlet concentration is less than 10~15mg/Nm to some specific operation projects³), even if using collaboration Resolution is less than 5mg/Nm³Discharge standard, it is also difficult to judgement be actually improvement of which link to dust Key effect is played, to avoid giving smoke and dust treatment technology path one guide of mistake：As long as matching somebody with somebody import three-level Roof high efficiency demister is it is ensured that absorption tower outlet dust concentration is less than 5mg/Nm³。

3. " collaboration resolution " is used, once flue dust exit concentration is more than 5mg/Nm³, then cannot judge be actually Which sport technique segment does not reach the effect that collaboration is administered, therefore how diagnosis of also having no way of eliminates defect to system.

4., for further depth removes superfine dust and drop, technological improvement is carried out to condensation wet film technology.

5. rotational flow plate defroster gas-liquid separating function is removed, dust and polymerization of fluid drops function are switched to after carrying out particular design.

The content of the invention

In view of the drawbacks described above of prior art, the technical problems to be solved by the invention are to provide one kind and more effectively increase Big fine solid particle and/or drop so that dust and/or drop after increase can effectively be divided by follow-up superfinishing fine separator From polymerizer, and provide the high-effective dust-removing demisting integral system of a kind of dependable performance, clear function.

To achieve the above object, it is poly- the invention provides a kind of polymerizer for the fine particle that is polymerized, i.e. fine particle Clutch, the polymerizer can make fine solid particle and/or the fine droplet polymerization in flue gas grow up, and will specifically divide in advance Remaining fine droplet (0~20 micron of particle diameter) and fine solid particle (0~10 micron of particle diameter) after device removal is by touching The mode of hitting is polymerized.By a large number of experiments show that, by fine particle polymerizer of the invention, fine droplet and thin The total quantity of micro mist dirt can at least reduce 50%, and thus quantity is reduced causes particulate matter to increase.

Polymerizer for the fine particle that is polymerized of the invention includes one or more cyclones, and cyclone is included extremely Few two swirl vanes, shape when swirl vane is provided so that the air-flow comprising fine particle by the cyclone Into swirling eddy.

Further, when polymerizer includes multiple cyclones, the eddy flow leaf in the adjacent cyclone of any two The setting direction of piece is identical.

Further, cyclone also includes center column and outer barrel, and one end of swirl vane is fixed in center column, The other end is fixed in outer barrel.

Further, outer barrel has circular cross-section, and circular cross-section is vertical with the axis of outer barrel；Swirl vane is fixed in The height of the other end of outer barrel is highly essentially identical with outer barrel, or less than the height of outer barrel, and both differences in height No more than 1/3rd of the diameter of circular cross-section.

Further, outer barrel has equilateral polygon section, and equilateral polygon section is vertical with the axis of outer barrel；Eddy flow leaf The height that piece is fixed in the other end of outer barrel is highly essentially identical with outer barrel, or less than the height of outer barrel, and both Difference in height no more than equilateral polygon section most long-diagonal length 1/3rd.

Further, the axis of multiple cyclones is parallel to each other.

Further, multiple cyclones are located at two and are formed in V-shaped or lambdoid plane respectively, positioned at same The axis of the cyclone in plane is parallel to each other.

Further, the elevation angle of swirl vane, i.e. swirl vane pass through extension length direction with it is outer The angle α formed between the level cross-sectionn of cylinder, is 12.5~60 °, preferably 22~27 °.

Further, the quantity of swirl vane is 3~18.

Preferably, the quantity of swirl vane is 6~8.

Further, the specification of each cyclone is arranged to identical, to reduce the cost of investment of device.For not Same region can be using the cyclone of differentiation, to adapt to the gas flowfield of different zones, such as in cyclone Swirl vane quantity it is different, the diameter of outer barrel is different or height of cyclone is differed.Scientifically implement difference Changing polymerization of the arrangement to fine solid particle and fine droplet will produce more useful effect.

Further, in order to improve the service life and structural strength of cyclone, preferably by swirl vane, center Cylinder and outer barrel manufacture are integral, that is, be integrally formed.

Further, polymerizer also includes the fixture for installing cyclone, is provided with for installing on fixture The mounting hole of cyclone, multiple cyclones are arranged on fixture by mounting hole；It is additionally provided with fixture logical Stomata.Passage act as reducing the pressure loss of polymerizer, and avoids the polymerizer from producing hydrops pond, so as to maintain The polymerization of polymerizer.

Further, fixture is on the whole planar structure, and the multiple cyclones on fixture are in same In one plane, and the axis of multiple cyclones is parallel to each other.

Further, fixture includes two planes for forming herringbone or V-shaped, installs in the same plane The axis of cyclone is parallel to each other.

The operation principle of the above-mentioned polymerizer for the fine particle that is polymerized of the invention is as follows：

Cyclone in polymerizer can realize that dust is poly- with dust polymerization, drop and polymerization of fluid drops, dust and drop Close, bulky grain is polymerized with bulky grain, little particle is polymerized with little particle, bulky grain is polymerized with little particle, while hair The even repeatedly polymerization of raw once polymerization, after polymerization.

Swirl vane in cyclone promotes above-mentioned polymerization process in the presence of following three big effects：

First, big drop and (or) big dust pursue and attack droplet and (or) small dust chase effect cause drop and (or) dust grows up.The air-flow of a large amount of fine droplets and (or) fine solid particle is carried by after cyclone, Airflow direction changes, and produces swirling eddy.Because the swirl vane of adjacent two cyclone is clockwise Or counterclockwise, so the coupled zone that crosses of adjacent two cyclone produces gas flow counterflow effect, backwash effect hair It is raw, cause flue gas flow rate to decline, but due to drop, (density is 1000~1200Kg/m³) and (or) dust (heap Product density is about 1600~2200kg/m³) density be significantly larger than air-flow (density be 1.1-1.3Kg/m³) density, because There is Relative sliding, Er Qieyou under inertia force effect higher and with the air-flow for marching forward in this drop and (or) dust There is certain viscosity (under 1 atmospheric pressure, 50 DEG C of operating modes dynamic viscosity about 1.96 × 10 in air-flow^-5Pa.s) to hair The drop and (or) dust of raw Relative sliding produce viscous force (i.e. sticky internal friction, with dust and (or) drop Surface area it is proportional) prevent this Relative sliding, due to the ratio table of more small drop and (or) dust Area is big, thus the Relative sliding speed of larger drop and (or) larger dust be higher than smaller droplet and (or) compared with Small dust, therefore larger drop and (or) larger dust will pursue and attack more droplet and (or) smaller dust effect And very maximum probability will more droplet and (or) smaller dust capture so as to cause drop and (or) dust to be grown up.

Secondly, adjacent two cyclone crosses the fine solid particle that the backwash effect of coupling regime will result directly in flue gas stream And (or) the fine droplet and (or) fine solid particle in fine droplet and the air-flow that comes head-on directly in opposite directions collision so as to Realize that dust and (or) drop are grown up.Because the swirl vane of adjacent two cyclone is clockwise direction or inverse Clockwise, so the coupling regime that crosses of adjacent two cyclone produces gas flow counterflow effect, it is substantial amounts of in air-flow Fine solid particle and (or) fine droplet in fine solid particle and (or) fine droplet and the air-flow for coming head-on are touched Hit cause between dust and dust, occur once to be polymerized between dust and drop, between drop and drop, after polymerization Even repeatedly it is polymerized so as to form big dust and (or) big droplet particles.

Again, high velocity air causes the liquid film rested on swirl vane to be rolled phenomenon (calling carrying phenomenon in the following text) again Form newly-increased super large drop, super large droplet capture fine solid particle and (or) drop effect.The corrugated sheet of downstream position Droplet formation moisture film under separator or condensation wet film whizzer are separated can converge in cyclone under gravity Swirl vane on, a thin layer of liquid film can be formed on its surface, by the cyclone of particular design, flue gas stream When crossing the narrow and small runner constituted between adjacent two swirl vane, the carrying phenomenon of generation will form substantial amounts of super large drop, These newly-increased super large drops, will play more huge poly- in above two drop and (or) dust increase effect Cooperation is used.

Present invention also offers a kind of flue gas flow channel, including one or more levels it is above-mentioned any one be used to be polymerized fine particle Polymerizer, polymerizer is arranged on the section of the flue gas stream containing fine particle.

Further, the plane where polymerizer is substantially vertical with the direction of flue gas stream.

Further, it is 22.5~65 ° that the plane where polymerizer has angle β, angle β with the direction of flue gas stream.

Further, flue gas flow channel arranges that the plane where each area is interior correspondingly to be set using steel infrastructure partitions There is polymerizer.

Further, multiple cyclones of the polymerizer being arranged in each area respectively be located at two formed V-shaped or In lambdoid plane.

Further, a diameter of 1.5~30m of the flue gas flow channel.

Because the above-mentioned polymerizer for the fine particle that is polymerized that the present invention is provided mainly realizes that fine particulates are polymerized, In practical application, generally it is not suitable for being used separately as separator, therefore present invention also offers a kind of dedusting demisting one Body system, the system include one or more levels it is above-mentioned any one be used to be polymerized fine particle polymerizer, the polymerizer Upstream and/or downstream position be provided with curved channel formula separator, resolution element in curved channel formula separator is constituted The gas channel of multiple bending so that during the gas channel that air-flow bends by multiple, air-flow constantly changes flow direction, Drop in air-flow clashes into resolution element under the action of the centrifugal force, largely impinges upon the droplet formation moisture film of resolution element, Moisture film falls after rise under gravity.

Further, polymerizer is less than 1500mm with the distance of curved channel formula separator.

Preferably, polymerizer is less than 50mm with the distance of curved channel formula separator.

Further, the resolution element in curved channel formula separator is ripple board component, thus the curved channel formula point It is corrugated plate dst gas-liquid separator from device, corrugated plating that ripple board component includes multiple intervals, being evenly arranged is multiple Gas channel of the chevron-shaped into bending so that air-flow constantly changes flow direction；The distance between adjacent two corrugated plating It is 10~60mm；Corrugated plating is preferably sinusoidal corrugated sheet, and corrugated plating has the accessory structures such as hook and/or hole, Hook and hole are respectively provided with one or more；The thickness of corrugated plating is 1.0~3.5mm；Corrugated plating is solid or hollow structure.

Further, corrugated plating is hollow structure, and interior stream has cooling medium, and the temperature of cooling medium is less than air-flow Temperature, cooling medium is supplied by cooling medium supply system.Now the corrugated plate dst gas-liquid separator be specially condensation it is wet Film whizzer.

Further, the interior diameter of the outer barrel in cyclone preferably with adjacent two ripple in curved channel formula separator The distance of plate is identical, and the exit flow of cyclone is received by two corrugated plating completely.

Further, the resolution element in curved channel formula separator is 2~5 layers of interlaced tube bank, thus bending Flow channel type separator is tubular type gas-liquid separator, and each layer of tube bank includes multiple pipes being spaced, being evenly arranged, adjacent Pipe in two-layer tube bank is in interlaced arrangement, forms the airflow path of bending so that air-flow constantly changes flow direction；Place The center spacing of the pipe in same layer tube bank is 1.2~4 times of the caliber of this layer tube bank；The cross sectional form of pipe for it is circular, Water-drop-shaped or bullet-headed grade are adapted to aerodynamic section.

Present invention also offers another dedusting demisting integral system, including one or more levels it is above-mentioned any one be used for The polymerizer of polymerization fine particle, the upstream position of polymerizer is provided with one or more levels preseparator, and/or polymerizer Downstream position be provided with one or more levels fine separator and/or one or more levels superfinishing fine separator；

Fine separator has the drop separation performance higher than preseparator, and hyperfine separator has than fine separation Device drop separation performance higher.

Further, preseparator includes curved channel formula separator, or fine separator includes curved channel formula point From device.

Further, preseparator is tube designs preseparator, slab design preseparator, roof layouts pre-separation One or more combination in device, horizontal gas flow preseparator；Superfinishing fine separator is segmented for slab design superfinishing One or more combination in device, roof layouts superfinishing fine separator, horizontal gas flow superfinishing fine separator.

Further, one or more levels preseparator, one or more levels polymerizer and one or more levels fine separator And/or superfinishing fine separator is all arranged in smoke absorption tower, the flow direction of air-flow is vertical direction.

Further, one or more levels preseparator, one or more levels polymerizer and one or more levels fine separator And/or superfinishing fine separator is all arranged in absorption tower outlet horizontal flue, the flow direction of air-flow is horizontal direction.

Further, one or more levels preseparator, one or more levels polymerizer and one or more levels fine separator And/or the part in superfinishing fine separator is arranged in absorption tower, another part is arranged in absorption tower outlet horizontal flue Interior, on absorption tower, interior air-flow is in vertical direction, in absorption tower Horizontal Exit flue interior air-flow in horizontal direction.

Further, any one-level preseparator, any one-level polymerizer and the fine separator of any one-level and/or superfinishing Fine separator needs to be surveyed in each self-corresponding air flow inlet side and/or air stream outlet and is provided with all in accordance with actual operating mode Automatically and/or manually cleaning device, cleaning device includes pipeline and flooding nozzle.

Make the method for fine particle polymerization in flue gas present invention also offers a kind of, the method is flue gas is passed through whirlwind Device, so as to produce multiply direction of rotation identical swirling eddy, occurs between swirling eddy and adjacent swirling eddy Cross and liquidate.

Present invention also offers a kind of integration dust-removing defogging method, the method is flue gas is passed through cyclone, from And produce multiply direction of rotation identical swirling eddy, crossed between swirling eddy and adjacent swirling eddy with it is right Punching；Also make flue gas by being arranged on the curved channel formula separator of cyclone upstream and/downstream position, curved channel formula Resolution element in separator constitutes the gas channel of multiple bendings so that when air-flow passes through the gas channel of multiple bendings, Air-flow constantly changes flow direction, droplet in air-flow or carries the drop of solid particulate matter and clashes under the action of the centrifugal force Resolution element, and moisture film is formed, moisture film falls after rise under gravity.

Further, curved channel formula separator is arranged on the downstream position of cyclone so that moisture film is in Action of Gravity Field Under fall back on the swirl vane of cyclone.

Further, also make flue gas by be arranged on the upstream position of cyclone one or more levels preseparator and/ Or it is arranged on one or more levels superfinishing fine separator of the downstream position of cyclone.

In better embodiment of the invention, dedusting demisting integral system is arranged in the downstream position of smoke absorption tower, Air-flow sequentially passes through preseparator, fine particle polymerizer, condensation wet film centrifugation point in dedusting demisting integral system From device (or corrugated plate dst gas-liquid separator) and superfinishing fine separator etc., preseparator, fine particle polymerizer, Condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and superfinishing fine separator can all be arranged in cigarette Aspiration tower inner top position, it is also possible to be all arranged in smoke absorption tower outlet horizontal flue, it is also possible to a part It is arranged in an absorption tower inner top position part to be arranged in smoke absorption tower outlet horizontal flue, specific embodiment To be determined by the space at each project scene.

Preseparator, its major function is to remove the big drop that smoke absorption tower spraying layer is produced, for 18 microns of particle diameter Big drop above, its removal efficiency can reach 100%；For 5~18 microns of drop of particle diameter, with difference The separative efficiency of degree, drop is smaller, and separative efficiency is lower, and drop is bigger, and separative efficiency is higher；For particle diameter 5 Drop below micron, in theory without separating effect, the drop for only existing few quantity impinges upon quilt on resolution element Intercept removal.Typical coal fired power plant flue gas desulfurization absorption tower, former flue gas is by after 3-6 layers of spraying layer washing, there are about 10000mg/Nm³Drop possibly into preseparator, therefore be reduced to firstly the need of by substantial amounts of concentration of liquid drops ≤75mg/Nm³, even less than≤35mg/Nm³。

Preseparator is preferably by one-level pipe separator, the thick roof separator of one-level and the thin roof separator of one-level.

Pipe separator, preferably by 2~3 layers of pipe of interlaced arrangement as resolution element, between same layer pipe Preferably by 90~110mm, pipe diameter preferably selects D50~D90 to distance；Pipe in it is horizontally disposed ( Installed in absorption tower) or be arranged vertically (installed in absorption tower outlet horizontal flue)；

Thick roof separator, preferably by like sine bellows thin plate as resolution element, between adjacent two corrugated sheet Interval S preferably select 25~30mm, resolution element angle of inclination the angle of horizontal plane (resolution element with) is excellent Selection of land selects 25~37.5 °；Roof separator can with it is " V "-shaped arrangement or " people " font arrange, preferably From " people " font arrangement.

Thin roof demister, preferably by like sine bellows thin plate, used as resolution element, resolution element buckle is designed, Spacing states S preferably from 22.0~27.5mm between adjacent two corrugated sheet, and resolution element angle of inclination is preferably selected With 25~37.5 °；Thin roof separator can be arranged with " V "-shaped arrangement or " people " font.

As long as the concentration of liquid drops that the type selecting of preseparator meets preseparator rear is less than 75mg/Nm³, preferably examine Consider and be less than 35mg/Nm³, therefore the other prior arts of preseparator use, such as one-level pipe separator, The flat separator of one-level and the thin roof demister of one-level, it is also possible to only with one-level pipe separator and the thin roof of one-level Separator or the thick roof separator of one-level and the thin roof separator of one-level, pollutant emission of this set to neat stress Slightly influence.

Further, when fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) It is designed as when more than two-stage or two-stage, preseparator is preferably one-level pipe separator and one-level roof separator, The concentration of liquid drops at preseparator rear is less than 150mg/Nm³It is generally also feasible.

Condensation wet film whizzer, its major function is further depth micro- by what is crossed by fine particle aggregator aggregates Droplet and fine solid particle carry out two grades of increases again by condensing mode, simultaneously because how curved self structure form be Bellows-shaped, has remarkable drop separation performance concurrently.By two grades of increases of condensing mode, show through overtesting, in control During good suitable condensing water vapor amount of precipitation, the particle diameter of all fine droplets and fine solid particle can all be will be increased to 6 micro- Rice more than, the particle diameter of most drop more than 10 microns, even more than 13 microns, these increase after small liquid Drop and fine solid particle be sufficient so that itself as separator effect and follow-up superfinishing fine separator show it is very outstanding Separating property.

Condensation wet film whizzer, its resolution element is preferably hollow corrugated plating, and interior stream has cooling water, saturation When wet flue gas are by condensation wet film whizzer, flue-gas temperature declines and separates out substantial amounts of steam, and the steam of generation is certainly Dynamic remaining fine droplet and (or) the minute dusts found are adsorbed as the nuclei of condensation, fine droplet and (or) minute dusts Grown up after a large amount of steam, bigger centrifugal force will be subject under same gas flow velocity；What is more important irregular surface Dust become spheroid after adsorbing steam, dust and smoke contacts are converted into water droplet and smoke contacts so as to significantly The viscous force between dust and flue gas is reduced, therefore larger centrifugal force is formed so as to hit when being flowed in the runner of bending Hit on resolution element.And because hollow corrugation plate has cold-wall effect, can be formed in the outer surface of hollow corrugation plate One layer of uniform and stable moisture film, the drop and (or) dust for impinging upon hollow corrugation plate is buried in oblivion by moisture film moment so that Fine droplet and (or) minute dusts are captured and intercept and remove.

When soot emissions requirement can with it is lower slightly when (such as allow dust concentration be less than 10mg/Nm³), have to take the second best Selectable technical scheme is centrifuged instead of condensation wet film using traditional flat separator or roof type separator Separator, i.e. resolution element do not have hollow structure, and fine solid particle and (or) fine droplet are increased without condensation Function.

It should be strongly noted that result of the test shows, fine particle polymerizer and condensation wet film whizzer (or Corrugated plate dst gas-liquid separator) when being applied in combination, very pleasantly surprised polymerization effect and separating effect are made us into generation, its Performance after combination will be significantly larger than fine particle polymerizer and condensation wet film whizzer (or corrugated plate dst gas-liquid point From device) each single polymerization effect and separating effect sum.

Superfinishing fine separator, possesses unsurpassed separating property, after the design of corresponding operation optimization, its limit Size droplet diameter can as little as 12~13 microns, the separative efficiency to 10 microns of drops with more than 80%；To 8 microns Drop have more than 60% separative efficiency；There is more than 40% separative efficiency to 6 microns of drops.

Limit size droplet diameter refers to that the drop is separated 100% when the particle diameter of drop is up to or over the size Removal.Therefore limit size droplet diameter is the most important performance technologies index of separator.

Can contrast, existing thin roof separator, generally using sine bellows thin plate, the eddy flow of a two curved hooks Blade pitgh be 22~25mm, angle of inclination be 35~37.5 °, design void tower flue gas flow rate 3.85m/ spacing under, Limit size droplet diameter is about 18 microns.

Superfinishing fine separator, only as little as 12~13 microns of limit size droplet diameter, about the 1/3 of 18 micro droplets quality.

Superfinishing fine separator, preferably by three it is curved like sine bellows thin plate as resolution element, resolution element one hook of band With hole design, interval S preferably selects 22.0~33.0mm between adjacent two corrugated sheet, and angle of inclination is preferably From 30~37.5 °.

Superfinishing fine separator, preferably designs net area rate >=85%, in small absorption tower (such as less than 10m), if Meter net area rate is usually less than 80%.

High-effective dust-removing demisting integral system of the invention, air-flow sequentially pass through preseparator, fine particle polymerizer, After condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and superfinishing fine separator, droplet content will be small In 10.0mg/Nm³(use Mg²⁺Trace method) or less than 1.0mg/Nm³(using T ü V>15 microns of impingement method inspections Survey)；When using two-stage or multistage fine particle polymerizer, (or the corrugated plate dst gas-liquid separation of condensation wet film whizzer Device) design when, droplet content will be less than 5.0mg/Nm³(use Mg²⁺Trace method) or less than 0.5mg/Nm³(use TüV>15 microns of impingement method detections).Droplet separating effect is significantly larger than high efficiency demister (such as three-level roof demister) Showed except fog effect.

High-effective dust-removing demisting integral system of the invention, air-flow sequentially pass through preseparator, fine particle polymerizer, After condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and superfinishing fine separator, when absorption tower entrance Dust is less than 20mg/Nm³Under, it can be ensured that remaining dust concentration is less than 3.5mg/Nm in air-flow³；When desulfurization absorbs Tower Inlet dust is less than 30mg/Nm³Under, it can be ensured that remaining dust concentration is less than 5.0mg/Nm in air-flow³；When de- Sulphur absorption tower Inlet dust is less than 50mg/Nm³Under, it can be ensured that remaining dust concentration is less than 10.0 in air-flow mg/Nm³.According to two-stage or multistage fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas Liquid/gas separator), no matter entrance content how much, can realize less than 5.0mg/Nm³。

A kind of high-effective dust-removing demisting integral system of the invention, if the concentration of liquid drops in air-flow is not high in itself, can be with Cancel preprocessor, only with fine particle polymerizer, condensation wet film whizzer and superfinishing fine separator.

A kind of high-effective dust-removing demisting integral system of the invention, if the concentration of liquid drops in air-flow is not high in itself, outlet Dust concentration also require that it is not high, such as entrance dust concentration be 50mg/Nm³, exporting dust concentration allows to be less than 20mg/Nm³, preprocessor and superfinishing fine separator can be cancelled, only with fine particle polymerizer, condensation wet film from Centrifugal separator.

A kind of high-effective dust-removing demisting integral system of the invention, if using preprocessor or superfinishing fine separator or Person is using 1 grade or multistage fine particle polymerizer each depends on design parameter.After the design parameter for providing, profit Meet by doing design modification with computer Simulation calculation and with reference to scientific experiment, engineering practice.

A kind of high-effective dust-removing demisting integral system of the invention, due to not being water droplet in applied environment, but slurry drops, So for any one-level preseparator, fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas Liquid/gas separator) and superfinishing fine separator all in accordance with actual operating mode need and in its air flow inlet side and (or) air-flow Outlet side is provided with (or manual) cleaning device automatically, and cleaning device is made up of pipeline and flooding nozzle.

Compared with prior art, dedusting demisting integral system of the invention has the advantages that：

(1) high-effective dust-removing demisting integral system of the invention is both the liquid drop separator of brilliance and the dust separation of brilliance Device；

(2) such that the design of whole fume desulfurating absorption tower is more simplified, spraying layer, pallet, whirlwind coupling, FGD are general The facilities such as Lars are to absorb SO₂Function, and it is not additionally required consideration dust removal function；

(3) cost of investment of whole desulfurizer is reduced；

(4) operating cost of whole desulfurizer is reduced, meets national energy-saving emission reduction development strategy；

(5) by colliding polymerization and the dual increase effect of condensation adsorption, fine solid particle and fine droplet are more effectively amplified, Improve the overall efficiency of a whole set of dedusting demisting integral system；

(6) equipment is all using corrosion resistant nonmetallic materials, long service life；

(7) device regular maintenance cost is low, without often changing parts；

(8) equipment dependability is high, can longtime running more than 25000hr.

The technique effect of design of the invention, concrete structure and generation is described further below with reference to accompanying drawing, with It is fully understood from the purpose of the present invention, feature and effect.

Brief description of the drawings

Fig. 1 is the structure sectional view of the high-effective dust-removing demisting integral system of embodiments of the invention 1；

Fig. 2 is the A-A profiles of Fig. 1；

Fig. 3 is single cyclone graphics；

Fig. 4 is the top view of single cyclone；

Fig. 5 is fine particle polymerizer fundamental diagram；

Fig. 6 is the alternative plan structural representation of the high-effective dust-removing demisting integral system of the embodiment of the present invention 1；

Fig. 7 is the third program structural representation of the high-effective dust-removing demisting integral system of the embodiment of the present invention 1；

Fig. 8 is the fourth program structural representation of the high-effective dust-removing demisting integral system of the embodiment of the present invention 1；

Fig. 9 is the first scheme structural representation of the high-effective dust-removing demisting integral system of embodiments of the invention 2；

Figure 10 is the schematic diagram of typical tubular type preseparator 11；

Figure 11 is the structural representation of typical gable roof's formula separator；

Figure 12 is the hook-type corrugated plate dst structure of gas liquid separator schematic diagram of a hole one；

Figure 13 is the alternative plan structural representation of the high-effective dust-removing demisting integral system of embodiments of the invention 2；

Figure 14 is the third program structural representation of the high-effective dust-removing demisting integral system of embodiments of the invention 2.

Specific embodiment

Embodiment 1

As shown in Figure 1, the first scheme of the high-effective dust-removing demisting integral system of the present embodiment be dedusting demisting integrally Change system is arranged in absorption tower, and the system includes 30 liang of fine particle polymerizer 20 and condensation wet film whizzer Part, wherein fine particle polymerizer 20 and condensation wet film whizzer 30 are arranged in the cigarette containing fine particle On the section of gas air-flow.It is flat where plane and condensation wet film whizzer 30 where fine particle polymerizer 20 Face is substantially vertical with the direction of flue gas stream.

The fine particle polymerizer 20 and condensation wet film whizzer 30 are arranged in one layer of support beam.

Self-stripping system is provided with the top of the bottom of fine particle polymerizer 20 and condensation wet film whizzer 30.

The fine particle polymerizer 20 and condensation wet film whizzer 30 are close to (distance is less than 10mm) structure Into an entirety.

As shown in figs. 2 to 4, the fine particle polymerizer 20 of the present embodiment includes multiple cyclones 21, each whirlwind Device 21 includes center column 212, outer barrel 213 and s (s >=2) swirl vane 211, and swirl vane 211 can So that forming swirling eddy when the air-flow comprising fine particle is by cyclone 21.

Cyclone 21 is arranged to have 6 swirl vanes 211 in the present embodiment.Two cyclones of arbitrary neighborhood 21 swirl vane 211 is counterclockwise (vertical view).One end of multiple swirl vanes 211 is fixed in newel Body 212, the other end is fixed in outer barrel 213.The outer barrel 213 of the present embodiment have circular cross-section, the circular cross-section with it is outer The axis of cylinder 213 is vertical.Swirl vane 211 is fixed in the height of the other end of outer barrel 213 and the height of outer barrel 213 It is essentially identical, or less than the height of outer barrel 213, and both differences in height are cut no more than the above-mentioned circular of outer barrel 213 / 3rd of the diameter in face.

Outer barrel 213 can also have equilateral polygon section, and the regular polygon and outer barrel 213 in other embodiments Axis is vertical, now swirl vane 211 be fixed in the other end of outer barrel 213 height it is basic with the height of outer barrel 213 It is identical, or less than the height of outer barrel 213, and both differences in height are cut no more than the above-mentioned regular polygon of outer barrel 213 / 3rd of the most long-diagonal length in face.

In the present embodiment, in multiple cyclones 21 are generally aligned in the same plane, the axis of multiple cyclones 21 is mutually put down OK.In other embodiments, multiple cyclones 21 are located at two and are formed in V-shaped or lambdoid plane respectively, The axis of the cyclone 21 in being generally aligned in the same plane is parallel to each other.

The elevation angle of the swirl vane 211 of cyclone 21 is 12.5~60 °, and the present embodiment is preferably 22.5 °.

Cyclone 21 uses same size, and the interior diameter of outer barrel 213 is 32.5mm.

In the present embodiment, cyclone 21 is that swirl vane 211, center column 212 and outer barrel 213 are molded into one It is integrally formed.

The fine particle polymerizer 20 of the present embodiment also includes the fixture 22 for installing cyclone 21, fixture The mounting hole 221 for installing fixed cyclone 21 is provided with 22, multiple cyclones 21 pass through mounting hole 211 On fixture 22.Fixture 22 is additionally provided with passage 222, to reduce the pressure loss of polymerizer 20, And avoid polymerizer from producing the polymerization reduction of hydrops and the polymerizer 20 that causes.

Fig. 5 is the fundamental diagram of the fine particle polymerizer 20 of the present embodiment, by particular design (i.e. swirl vane 211 are designed to almost with the height of outer barrel 213) cyclone 21, it is possible to achieve dust and dust polymerization, Drop is polymerized with polymerization of fluid drops, bulky grain with polymerization of fluid drops, dust with bulky grain, little particle is polymerized with little particle, big Particle is polymerized with little particle, while there is the even repeatedly polymerization of once polymerization, after polymerization.

As shown in figure 5, the swirl vane 211 in cyclone 21 promotes above-mentioned polymerization process in the presence of following three big effects：

First, big drop and (or) big dust pursue and attack droplet and (or) small dust chase effect cause drop and (or) dust grows up.The air-flow of a large amount of fine droplets and (or) fine solid particle is carried by cyclone 21 Afterwards, airflow direction changes, and produces swirling eddy.Because the swirl vane 211 of adjacent two cyclone 21 is Direction clockwise or counter-clockwise, so the coupled zone that crosses of adjacent two cyclone 21 produces gas flow counterflow effect Should, backwash effect occurs, and causes flue gas flow rate to decline, but (density is 1000~1200Kg/m due to drop³) And (or) dust (bulk density is about 1600~2200kg/m³) density be significantly larger than air-flow (density be 1.1-1.3Kg/m³) density, therefore drop and (or) dust are under inertia force effect higher and with the gas for marching forward There is Relative sliding in stream, and because air-flow has certain viscosity (under 1 atmospheric pressure, 50 DEG C of operating modes dynamic viscosity About 1.96 × 10^-5Pa.s) drop and (or) dust that Relative sliding occurs are produced viscous force (i.e. sticky internal friction, Surface area with dust and (or) drop is proportional) this Relative sliding is prevented, due to more small drop And (or) the specific surface area of dust is big, so the Relative sliding speed of larger drop and (or) larger dust is higher than Smaller droplet and (or) smaller dust, thus larger drop and (or) larger dust will pursue and attack more droplet and (or) smaller dust effect and very maximum probability will more droplet and (or) smaller dust capture so as to cause drop and (or) Dust is grown up.

Secondly, adjacent two cyclone 21 crosses the trickle powder that the backwash effect of coupling regime will result directly in flue gas stream Fine droplet and (or) fine solid particle in dirt and (or) fine droplet and the air-flow that comes head-on directly collide in opposite directions from And realize dust and (or) drop and grow up.Due to the swirl vane of adjacent two cyclone 21 be clockwise or Person counterclockwise, so adjacent two cyclone 21 cross coupling regime produce gas flow counterflow effect, in air-flow Fine solid particle and (or) fine droplet in substantial amounts of fine solid particle and (or) fine droplet and the air-flow for coming head-on Collide cause between dust and dust, occur once to be polymerized between dust and drop, between drop and drop, two Secondary polymerization is even repeatedly polymerized so as to form big dust and (or) big droplet particles.

Again, high velocity air causes the liquid film rested on swirl vane to be rolled phenomenon (calling carrying phenomenon in the following text) again Form newly-increased super large drop, super large droplet capture fine solid particle and (or) drop effect.The condensation wet film of downstream position Droplet formation moisture film under the separation of whizzer 30 can converge in the swirl vane 211 of cyclone under gravity On, a thin layer of liquid film can be formed on its surface, by after cyclone 21, flue gas flows through adjacent two swirl vane During the narrow and small runner constituted between 211, the carrying phenomenon of generation will form substantial amounts of super large drop, and these are newly-increased to surpass Big drop, more huge polymerization will be played in above two drop and (or) dust increase effect.

Using three curved ripple hollow sheetings 31, interior stream has recirculated cooling water to the resolution element of condensation wet film whizzer 30 32.Adjacent two ripples hollow sheeting interval S is 32.5mm.

The air-flow of drop and dust is carry by after the above-mentioned high-effective dust-removing demisting integral system of the present embodiment, air-flow Remaining droplet content will be less than 40mg/Nm³；When high-effective dust-removing demisting integral system Inlet dust concentration is less than 50mg/Nm³When, outlet dust concentration will be less than 20mg/Nm³, i.e., efficiency of dust collection is more than 60%.

As shown in fig. 6, the selectable alternative plan of the present embodiment is to use with reality condensation wet film whizzer 30 The corrugated plating of the heart replaces for the corrugated plate dst gas-liquid separator 302 of resolution element, i.e. high-effective dust-removing demisting integral system Including fine particle polymerizer 20 and the two parts of corrugated plate dst gas-liquid separator 302, and with the perpendicular arrangement of air-flow.Ripple The resolution element of card formula gas-liquid separator 302 can for two it is curved like sine wave curve without hook-type, as shown in Figure 1 three Curved ripple hollow sheeting 31；Or two is curved like sine wave curve band hook-type, the resolution element 132 of buckle as shown in Figure 10； Three it is curved like sine wave curve without hook-type, three it is curved like sine wave curve band hook-type, with one or more holes and (or) hook Shape etc..

As shown in fig. 7, in the selectable third program of the present embodiment, high-effective dust-removing demisting integral system includes bag Fine particle polymerizer 20 and (or the corrugated plate dst gas-liquid separator) two parts of condensation wet film whizzer 30 are included, In this programme, by fine particle polymerizer 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) Using being in tilted layout, i.e., the β that had angle with cigarette airflow direction structure (β is more than 0 °), wherein fine particle polymerizer 20 The plane at place is 22.5~65 ° with the angle β that the direction of flue gas stream is constituted, and its Main Function is to improve separator Effective area and improve developing result.

As shown in figure 8, in the selectable fourth program of the present embodiment, high-effective dust-removing demisting integral system includes thin Microparticle polymerizer 20 and (or the corrugated plate dst gas-liquid separator) two parts of condensation wet film whizzer 30, and will Fine particle polymerizer 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) using herringbone or V-shaped arranges that its Main Function is to improve the effective area of separator and improve developing result.For opium air-flow Road (such as a diameter of 1.5~3m), flue gas flow channel is arranged using steel infrastructure partitions, in the plane where each area Fine particle polymerizer 20 is correspondingly provided with, the multiple of the fine particle polymerizer 20 being provided with each area Cyclone 21 is located in two planes for forming herringbone or V-shaped respectively.

Embodiment 2

As shown in figure 9, the dedusting demisting integral system of the present embodiment includes one-level preprocessor 10, fine particle gathers Clutch 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) and superfinishing fine separator 40, And all in absorption tower.

Boiler exit gas after electric cleaner dust concentration with≤20mg/Nm³Into desulfuration absorbing tower 60.On absorption tower 3~6 layers of spraying layer 70 and possible 1~2 layer of pallet or FGD pulas this 80, flue gas process support are provided with 60 Disk or FGD pulas this 80 and spraying layer 70 after sequentially pass through preprocessor 10, fine particle polymerizer 20, condensation Wet film whizzer 30 and superfinishing fine separator 40.Arrow in Fig. 9 indicates the flow direction of flue gas.

The preseparator 10 includes the thick roof separator 12 of one-level pipe separator 11, one-level and the thin roof of one-level point From device 13.

Tubular demister 11 is horizontally disposed in absorption tower, including the pipe 111 that two rows or three rows are staggeredly arranged, As shown in Figure 10, wherein often row's pipe 111 is in horizontality, pipe 111 is free to rotate.In same row Adjacent pipe 111 between center spacing be 90~120mm, the caliber of pipe 111 is63mm.Pipe 111 Two ends have pipe stopper 112, and are cased with end plate 113, and multiple central dividing plates 114 are cased with pipe 111.Multiple circle Pipe 111 is fitted together by central dividing plate 114 and end plate 113.The flue gas for carrying a large amount of drops is separated by tubular type After device 11,85~90% drop of volume ratio is removed by pipe separator 11, and flue gas is obtained effectively Rectification.

Figure 11 shows thick roof separator 12 and thin roof separator 13, and both differences are different resolution element, The left mould block of thick roof separator and the resolution element 121 of right mould block not buckle, the left mould block of thin roof separator and the right side The buckle of module resolution element 131.Specifically, thick roof type demister and thin roof demister include first wave respectively The ripple board component 131 of card component 121 and second, the first corrugated plating component 121 and the second ripple board component 131 are equal It is made up of multi-disc corrugated sheet, there is the distance between half-sine wave shape, adjacent corrugated plate to be for the section of corrugated plating 20.0~40mm.Hook portion 132 is provided with corrugated plating in second ripple board component 131, the opening of the hook portion 132 The flow direction of direction and flue gas is conversely, the hook portion 132 is located at the crest of half-sine wave shape or at trough.First The combination of 121 and second ripple board component of ripple board component 131 forms " people " font arrangement, and the thickness of corrugated plating is preferred It is 2.0~3.5mm.After flue gas is through meticulous roof type demister 13, small drop, liquid are only remained in neat stress Drop concentration can be with≤35mg/Nm³。

The fine particle polymerizer 20 and condensation wet film whizzer 30 of this high-effective dust-removing demisting integral system are with real The first scheme for applying example one is identical.

Superfinishing fine separator 40 is made up of multi-disc corrugated plating 41, as shown in figure 12, the section of corrugated plating be including at least One sine wave shape of wavelength；Hole 411 is provided with the crest of sine wave shape, in the trough of sine wave shape Place is provided with hook portion 412；Or hole 411 is provided with the trough of sine wave shape, at the crest of sine wave shape It is provided with hook portion 412.Wherein, the opening direction of hook portion 412 and the flow direction of flue gas are opposite.Adjacent corrugated plate it Between distance be preferably 20.0~38mm.Distance between corrugated plating is designed as in flue gas flow rate region high preferably It is small, the distance between corrugated plating is designed as greatly in flue gas flow rate low region.Corrugated plating spacing can also be using fixation Spacing.The inclined arrangement of corrugated plating, specially arranges, the angle of inclination (ripple of corrugated plating in herringbone or V-shaped The angle of plate and horizontal plane) 28~39.0 ° are preferably, the thickness of corrugated plating is preferably 2.0~3.5mm.Flue gas passes through After hyperfine demister, the drop 100% in neat stress for particle diameter more than 13 microns is removed separation；To particle diameter 10 microns of drop has more than 80% separative efficiency；The separation that 8 microns of drop of particle diameter has more than 60% is imitated Rate；There is more than 40% separative efficiency to 6 microns of drop of particle diameter.

In the present embodiment, pipe separator 11 and thick roof type separator 12 are arranged on lower layer support beam；Thin roof Formula separator 13 is arranged in the support beam of intermediate layer；Fine particle polymerizer 20, the and of condensation wet film whizzer 30 Roof type superfinishing fine separator 40 is arranged in the support beam of upper strata.

For the high-effective dust-removing demisting integral system for avoiding the present embodiment is blocked, six layers of rinse-system 50 are provided with, the One layer of rinse-system 51 is used for rinsing the upstream side of the downstream of pipe separator 11 and thick roof separator 12, the second layer Rinse-system 52 is used for rushing the downstream of thick roof separator 11, and third layer rinse-system 53 is used for thin thick roof and separates The upstream side of device 13, the 4th layer of rinse-system 54 is used for rinsing fine particle polymerizer 20, and takes into account the thin thick room of flushing The downstream of separator 13 is pushed up, layer 5 rinse-system 55 is used for rinsing the upstream side of superfinishing fine separator 40, and takes into account The downstream of thin condensation wet film whizzer 30 is rinsed, layer 6 rinse-system 56 is used for rinsing superfinishing fine separator 40 downstreams.First rinses 51~56 to layer 5 uses self-stripping system, layer 6 rinse-system 56 to use hand Dynamic rinse-system, it would however also be possible to employ self-stripping system.

Using the present embodiment high-effective dust-removing demisting integral system, as entrance dust concentration≤20mg/Nm³When, can make Obtain the smoke content≤3.5mg/Nm in flue gas³；When desulfuration absorbing tower Inlet dust is less than 30mg/Nm³Under, it can be ensured that Remaining dust concentration is less than 5.0mg/Nm in air-flow³；When desulfuration absorbing tower Inlet dust is less than 50mg/Nm³Under, Can ensure that the dust concentration of remnants in air-flow is less than 10.0mg/Nm³；Droplet content will be less than 10.0mg/Nm³(use Mg²⁺Trace method) or less than 1.0mg/Nm³(using T ü V>15 microns of impingement method detections).

Limited by the space of live absorption tower 60, can be by the superfinishing of the high-effective dust-removing demisting integral system in Fig. 9 Fine separator 40 is arranged in horizontal flue 601 (as shown in figure 13).Flue gas by one-level preseparator (including pipe Formula preseparator 11, thick roof separator 12, thin roof separator 13), fine particle polymerizer 20, condensation wet film Whizzer 30 (or corrugated plate dst gas-liquid separator) and hyperfine horizontal gas flow separator 40；Preseparator and thin Microparticle polymerizer 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) are arranged in absorption tower； Hyperfine horizontal gas flow separator 40 is arranged in absorption tower outlet horizontal flue.

For special item, the installing space of separator is not provided with absorption tower 60, the present embodiment can efficiently be removed Dirt demisting integral system is arranged in the outlet horizontal flue 601 on absorption tower 60.Wherein flue gas is by one-level pre-separation Device (including tubular type preseparator 11, horizontal gas flow coarse separator 12, horizontal gas flow thickness separator 13), trickle Grain polymerizer 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) and hyperfine horizontal gas flow point From device 40.(as shown in figure 14).

No matter hyperfine horizontal gas flow separator 40 or whole high-effective dust-removing demisting integral system are disposed in out In mouth horizontal flue, in hyperfine horizontal gas flow separator 40 or the upstream of whole high-effective dust-removing demisting integral system The flue shell body of position can not take Insulation to be used to reduce the overall cost of desulphurization system, while condensed water can To capture sub-fraction fine solid particle and mist droplet, these condensed waters can be installed in hyperfine in horizontal flue Horizontal gas flow separator 40 or whole high-effective dust-removing demisting integral system intercept removal, therefore improve remove on the contrary Dirt and except fog effect.

Preferred embodiment of the invention described in detail above.It should be appreciated that one of ordinary skill in the art without Need creative work just can make many modifications and variations with design of the invention.Therefore, it is all in the art Technical staff under this invention's idea on the basis of existing technology can by logical analysis, reasoning, or a limited experiment With the technical scheme for obtaining, all should be in the protection domain being defined in the patent claims.

Claims (37)

1. a kind of polymerizer for the fine particle that is polymerized, it is characterised in that the polymerizer includes one or more rotations Wind apparatus, the cyclone includes at least two swirl vanes, and the swirl vane is provided so that comprising trickle Swirling eddy is formed when the air-flow of particle is by the cyclone.

2. as claimed in claim 1 for the polymerizer of the fine particle that is polymerized, it is characterised in that when the polymerizer During including multiple cyclones, the setting side of the swirl vane in the adjacent cyclone of any two To identical.

3. as claimed in claim 1 for the polymerizer of the fine particle that is polymerized, it is characterised in that the cyclone Also include center column and outer barrel, one end of the swirl vane is fixed in the center column, and the other end is fixed in institute State outer barrel.

4. as claimed in claim 3 for the polymerizer of the fine particle that is polymerized, it is characterised in that the outer barrel has Circular cross-section, the circular cross-section is vertical with the axis of the outer barrel.

5. as claimed in claim 4 for the polymerizer of the fine particle that is polymerized, it is characterised in that the swirl vane The height for being fixed in the other end of the outer barrel is highly essentially identical with the outer barrel, or less than the outer barrel Height, and both difference in height no more than the circular cross-section diameter 1/3rd.

6. as claimed in claim 3 for the polymerizer of the fine particle that is polymerized, it is characterised in that the outer barrel has Equilateral polygon section, the equilateral polygon section is vertical with the axis of the outer barrel.

7. as claimed in claim 6 for the polymerizer of the fine particle that is polymerized, it is characterised in that the swirl vane The height for being fixed in the other end of the outer barrel is highly essentially identical with the outer barrel, or less than the outer barrel Height, and both difference in height no more than the equilateral polygon section most long-diagonal length 1/3rd.

8. as claimed in claim 1 for the polymerizer of the fine particle that is polymerized, it is characterised in that the multiple whirlwind The axis of device is parallel to each other.

9. as claimed in claim 1 for the polymerizer of the fine particle that is polymerized, it is characterised in that the multiple whirlwind Device is located at two and is formed in V-shaped or lambdoid plane respectively, is generally aligned in the same plane the axis of interior cyclone It is parallel to each other.

10. as claimed in claim 3 for the polymerizer of the fine particle that is polymerized, it is characterised in that the eddy flow leaf The elevation angle of piece is 12.5~60 °.

11. polymerizers for the fine particle that is polymerized as claimed in claim 3, it is characterised in that the eddy flow leaf The quantity of piece is 3~18.

12. polymerizers for the fine particle that is polymerized as claimed in claim 11, it is characterised in that the eddy flow leaf The quantity of piece is 6~8.

13. polymerizers for the fine particle that is polymerized as claimed in claim 1, it is characterised in that the polymerizer Also include the fixture for installing the cyclone, be provided with the fixture for installing the cyclone Mounting hole, the multiple cyclone by the mounting hole be arranged on the fixture on；On the fixture also It is provided with passage.

14. polymerizers for the fine particle that is polymerized as claimed in claim 13, it is characterised in that the fixture It is on the whole planar structure, the multiple cyclone on the fixture is in same plane, and institute The axis for stating multiple cyclones is parallel to each other.

15. polymerizers for the fine particle that is polymerized as claimed in claim 13, it is characterised in that the fixture Including two planes for forming herringbone or V-shaped, the axis for installing cyclone in the same plane is parallel to each other.

16. a kind of flue gas flow channels, it is characterised in that including one or more levels such as any one institute in claim 1~15 The polymerizer for the fine particle that is polymerized stated, the polymerizer is arranged in the disconnected of the flue gas stream containing fine particle On face.

17. flue gas flow channels as claimed in claim 16, it is characterised in that plane where the polymerizer with it is described The direction of flue gas stream is substantially vertical.

18. flue gas flow channels as claimed in claim 16, it is characterised in that plane where the polymerizer with it is described It is 22.5~65 ° that the direction of flue gas stream has angle β, the angle β.

19. flue gas flow channels as claimed in claim 16, it is characterised in that the flue gas flow channel uses steel foundation structure Subregion arrangement, is correspondingly provided with the polymerizer in the plane where each area.

20. flue gas flow channels as claimed in claim 19, it is characterised in that be arranged on the polymerizer in each area The multiple cyclone be located at two respectively and formed in V-shaped or lambdoid plane.

21. a kind of dedusting demisting integral systems, it is characterised in that including one or more levels such as claim 1~15 The polymerizer for the fine particle that is polymerized described in middle any one, the upstream of the polymerizer and/or downstream position are set There is curved channel formula separator, the resolution element in the curved channel formula separator constitutes the gas channel of multiple bendings.

22. dedusting demisting integral systems as claimed in claim 21, it is characterised in that the polymerizer with it is described The distance of curved channel formula separator is less than 1500mm.

23. dedusting demisting integral systems as claimed in claim 22, it is characterised in that the polymerizer with it is described The distance of curved channel formula separator is less than 50mm.

24. dedusting demisting integral systems as claimed in claim 21, it is characterised in that the curved channel formula point Resolution element in device is ripple board component, ripple that the ripple board component includes multiple intervals, being evenly arranged Plate, gas channel of multiple chevron-shapeds into bending；The distance between corrugated plating described in adjacent two is 10~60mm； The corrugated plating is sinusoidal corrugated plating, and the corrugated plating has hook and/or hole, and the hook and the hole are respectively provided with One or more；The thickness of the corrugated plating is 1.0~3.5mm.

25. dedusting demisting integral systems as claimed in claim 24, it is characterised in that the corrugated plating is hollow Structure, interior stream has a cooling medium, the temperature of the temperature less than the air-flow of the cooling medium, the cooling medium by Cooling medium supply system is supplied.

26. dedusting demisting integral systems as claimed in claim 21, it is characterised in that the curved channel formula point Resolution element in device is 2~5 layers of interlaced tube bank, and each layer tube bank includes multiple intervals, uniform The pipe of arrangement, the pipe in tube bank described in adjacent two layers is in interlaced arrangement, forms the airflow path of bending；In same layer The center spacing of the pipe in the tube bank is 1.2~4 times of the caliber of this layer tube bank；The cross sectional form of the pipe for it is circular, Water-drop-shaped is bullet-headed.

A kind of 27. dedusting demisting integral systems, including one or more levels is as described in any one in claim 1~15 The polymerizer for the fine particle that is polymerized, the upstream position of the polymerizer is provided with one or more levels preseparator, And/or the downstream position of the polymerizer is provided with one or more levels fine separator and/or the subdivision of one or more levels superfinishing From device；

The fine separator has the drop separation performance higher than the preseparator, the hyperfine separator There is the drop separation performance higher than the fine separator.

28. dedusting demisting integral systems as claimed in claim 27, it is characterised in that the preseparator includes Curved channel formula separator, or the fine separator includes curved channel formula separator.

29. dedusting demisting integral systems as claimed in claim 27, it is characterised in that the preseparator is pipe In formula design preseparator, slab design preseparator, roof layouts preseparator, horizontal gas flow preseparator one Plant or various combinations；The superfinishing fine separator is slab design superfinishing fine separator, the subdivision of roof layouts superfinishing One or more combination in device, horizontal gas flow superfinishing fine separator.

30. dedusting demisting integral systems as claimed in claim 27, it is characterised in that one or more levels is described pre- Separator, one or more levels described polymerizer and one or more levels described fine separator and/or the hyperfine separation Device is all arranged in smoke absorption tower, and the flow direction of air-flow is vertical direction.

31. dedusting demisting integral systems as claimed in claim 27, it is characterised in that one or more levels is described pre- Separator, one or more levels described polymerizer and one or more levels described fine separator and/or the hyperfine separation Device is all arranged in absorption tower outlet horizontal flue, and the flow direction of air-flow is horizontal direction.

32. dedusting demisting integral systems as claimed in claim 27, it is characterised in that one or more levels is described pre- Separator, one or more levels described polymerizer and one or more levels described fine separator and/or the hyperfine separation A part in device is arranged in absorption tower, and another part is arranged in absorption tower outlet horizontal flue, in absorption tower Air-flow is in vertical direction, in absorption tower Horizontal Exit flue interior air-flow in horizontal direction.

33. dedusting demisting integral systems as claimed in claim 27, it is characterised in that divide in advance described in any one-level From fine separator described in device, polymerizer described in any one-level and any one-level and/or the superfinishing fine separator all in accordance with Actual operating mode needs are provided with automatically and/or manually clear in each self-corresponding air flow inlet side and/or air stream outlet survey Cleaning device, the cleaning device includes pipeline and flooding nozzle.

A kind of 34. methods for making fine particle polymerization in flue gas, it is characterised in that make the flue gas by cyclone, So as to produce multiply direction of rotation identical swirling eddy, handed between the swirling eddy and adjacent swirling eddy Converge and liquidate.

35. a kind of integration dust-removing defogging methods, it is characterised in that make flue gas by cyclone, so as to produce many Stock direction of rotation identical swirling eddy, crosses and liquidates between the swirling eddy and adjacent swirling eddy； Also make flue gas by being arranged on the curved channel formula separator of the cyclone upstream and/downstream position, the bending stream Resolution element in road formula separator constitutes the gas channels of multiple bendings so that air-flow by the multiple bending gas During circulation road, air-flow constantly changes flow direction, droplet in air-flow or carries the drop of solid particulate matter in centrifugal force Effect is lower to clash into the resolution element, and forms moisture film, and the moisture film falls after rise under gravity.

36. integration dust-removing defogging methods as claimed in claim 35, it is characterised in that the curved channel formula point The downstream position of the cyclone is arranged on from device so that the moisture film falls back to the bookbinding method under gravity On the swirl vane put.

37. integration dust-removing defogging methods as claimed in claim 35, it is characterised in that also make flue gas pass through to set The upstream position of the cyclone one or more levels preseparator and/or be arranged on the downstream of the cyclone One or more levels superfinishing fine separator of position.