CN205095604U - Fine particle polymerizer, flue gas runner and high -efficient dust removal defogging integration system - Google Patents
Fine particle polymerizer, flue gas runner and high -efficient dust removal defogging integration system Download PDFInfo
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- CN205095604U CN205095604U CN201520618652.1U CN201520618652U CN205095604U CN 205095604 U CN205095604 U CN 205095604U CN 201520618652 U CN201520618652 U CN 201520618652U CN 205095604 U CN205095604 U CN 205095604U
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Abstract
The utility model discloses a polymerization fine particle's polymerizer, this polymerizer include one or more cyclone, and cyclone includes two at least whirl blades, and the whirl blade is set up as that the feasible air current that contains fine particle forms rotatory air current when passing through cyclone. The utility model also discloses a dust removal defogging integration system that flue gas runner and one kind that contains above -mentioned polymerizer is including above -mentioned polymerizer. The utility model discloses a most slight dust of PM2.5 in the air current can effectively be got rid of by high -efficient dust removal defogging integration system, has very high practical application to worth to the improvement of fine particle thing in the flue gas, and installs that investment cost is low, operating power consumption hangs down, has long -term operational reliability, can be used to thermal power factory, steel plant, paper mill, glass factory, chemical plant and has the gas cleaning fields such as workshop that the particulate matter discharged.
Description
Technical field
The utility model relates to filed of flue gas purification, particularly relates to a kind of for fine particle polymerizer, flue gas flow channel and the dedusting demist integral system in the exhaust treatment systems such as thermal power plant, steel plant, paper mill, glass factory, chemical plant.
Background technology
For realizing the ultra-clean discharge even near-zero release of coal-fired station, country proposes " 50355 " index, namely requires that the soot emissions of coal-fired station are less than 5mg/Nm respectively
3(reaching Gas Generator Set standard), sulfur dioxide SO
2discharge standard be less than 35mg/Nm
3, nitrogen oxide NO
xconcentration is less than 50mg/Nm
3.
Reach ultra-clean discharge even near-zero release standard for realizing dust concentration, because wet electrical dust precipitator investment is large, operation energy consumption is high, bulky, auxiliary chemical consumption amount Datong District time bring the series of problems such as the corrosion of new pollutant, positive plate to allow many thermal power plants hang back.
But how to realize non-wet electrical dust precipitator and be issued to flue dust outlet drain and be less than 5mg/Nm
3standard is new technical barrier.A little environmental improvement enterprise is had to propose " govern coordinately scheme " scheme at present, adopt the wet desulfurization system (subregion in Dan Ta, tower, pallet is set or revolves and converge technology, the three-layer efficient demisters such as coupling) with high-effective dust-removing effect, while realizing high-efficiency desulfurization, to the dust efficient removal of desulphurization system be entered, realize the efficiency of dust collection of desulphurization system >=70%.
And state the main cause of wet desulfurization system high-effective dust-removing functional realiey:
(1) adopt high performance nozzle that slurries particle diameter is reduced by 30%, improve the dust supplementary set ability of slurries.
(2) by the liquid film layer that the technology such as pallet are formed, liquid film is increased to the supplementary set ability of fine dust.
(3) absorption tower arranges three-layer efficient demister, controls absorption tower exiting flue gas concentration of liquid drops at 20mg/Nm
3below, the gypsum particle thing carrying amount of flue gas is greatly reduced.
From above data, when desulfurization Inlet dust is 20mg/Nm
3time, even if desulphurization system realizes the dust removal rate of>=70%, the dust concentration namely entering into high efficiency demister still can reach 6mg/Nm
3, but high efficiency demister only has slurry droplet and well tackles removal effect, even if reach 20mg/Nm
3concentration of liquid drops, these residual droplets contain gypsum and other solid and soluble-salt, according to minimum 7% solid concentration calculate, newly-increased dust content is 1.4mg/Nm
3, therefore exit concentration will control at 5mg/Nm
3, necessarily require high efficiency demister to dust from 6mg/Nm
3be removed to 3.6mg/Nm further
3within, namely require that high efficiency demister reaches more than 40% to dust dust removal rate, this does not meet reality completely, and the 6mg/Nm of remnants
3be nearly all be less than the fine solid particle of 5 microns, show that high efficiency demister (three grades of roof demisters) at most can by dust from 6mg/Nm after deliberation with experimental result
3be reduced to 5.6mg/Nm
3, dust removal has little effect!
In addition, a kind of rotational flow plate defroster is taught in " the out of stock technology of coal-fired flue gas desulfurization and the case history " book to be co-publicated by Chemical Industry Press and Environmental Science and Engineering publishing centre for 2002, it utilizes eddy flow plate that air-flow is rotated, the drop High Rotation Speed in whirl cylinder be entrained in swirling eddy produces centrifugal force thus is thrown toward on cylinder inner wall, thus realize gas-liquid separation effect, described rotational flow plate defroster necessarily requires enough urceolus height, and its function is the centrifugal force utilizing spiral board to produce to be thrown to by droplet on barrel thus to realize gas-liquid separating function.
Again, a kind of condensation wet film high-effective dust-removing demist technology has been applied in number of patent application 201520058549.6 (a kind of high-effective dust-removing demist integral system), at the corrugated plating Internal Cooling Passage medium of hollow, by condensing mode, fine solid particle and drop are amplified, then by the hyperfine separator of downstream position, removal is carried out to it and be separated.
Described condensation wet film centrifugal dust-removing demist technology belongs to huge technological innovation in smoke and dust treatment field, but to extremely fine solid particle and drop, such as particle diameter is less than dust and the drop that 1 micron is even less than 0.5 micron, even if being still difficult to after amplifying be removed by follow-up hyperfine separation is separated, therefore for the further degree of depth improves the removal of extremely fine solid particle and drop, be necessary to do described condensation wet film technology further to improve.
Therefore, there is in prior art following technical problem need to solve:
1. adopt " govern coordinately scheme " to administer flue dust exit concentration and be less than 5mg/Nm
3unrealistic property, or " govern coordinately scheme " does not have and guarantees that flue dust exit concentration is less than 5mg/Nm more precisely
3science certainty.
2. (such as dust inlet concentration is less than 10 ~ 15mg/Nm to some specific operation project
3), even if adopt govern coordinately scheme to be less than 5mg/Nm
3discharge standard, also be difficult to judge to be that key effect is played in the improvement of which link to dust, for avoiding to the wrong guide of smoke and dust treatment technology path one: as long as namely join import three grades of roof high efficiency demister just can ensure that absorption tower outlet dust concentration is less than 5mg/Nm actually
3.
3. adopt " govern coordinately scheme ", once flue dust exit concentration is greater than 5mg/Nm
3, then cannot judge it is the effect which sport technique segment does not reach govern coordinately, how diagnosis of therefore also having no way of eliminates defect to system actually.
4. remove superfine dust and drop for the further degree of depth, technological improvement is carried out to condensation wet film technology.
5. remove rotational flow plate defroster gas-liquid separating function, after carrying out particular design, transfer dust and polymerization of fluid drops function to.
Utility model content
Because the above-mentioned defect of prior art, technical problem to be solved in the utility model is to provide one and more effectively increases fine solid particle and/or drop, make the polymerizer that the dust after increasing and/or drop effectively can be separated by follow-up hyperfine separator, and the high-effective dust-removing demist integral system of a kind of dependable performance, clear function is provided.
For achieving the above object, the utility model provides a kind of polymerizer for being polymerized fine particle, i.e. fine particle polymerizer, this polymerizer can make the fine solid particle in flue gas and/or fine droplet polymerization grow up, and the remaining fine droplet (particle diameter 0 ~ 20 micron) after being removed by preseparator specifically and fine solid particle (particle diameter 0 ~ 10 micron) are polymerized by collision mode.Through a large number of experiments show that, by fine particle polymerizer of the present utility model, the total quantity of fine droplet and fine solid particle at least can reduce 50%, and quantity minimizing causes particle to increase thus.
Polymerizer for being polymerized fine particle of the present utility model comprises one or more cyclone, and cyclone comprises at least two swirl vanes, and swirl vane is provided so that the air-flow comprising fine particle is by forming swirling eddy during described cyclone.
Further, when polymerizer comprises multiple cyclone, the setting direction of the swirl vane in any two adjacent cyclones is identical.
Further, cyclone also comprises center column and urceolus, and one end of swirl vane is fixed in center column, and the other end is fixed in urceolus.
Further, urceolus has circular cross-section, the axes normal of circular cross-section and urceolus; The height that swirl vane is fixed in the other end of urceolus is substantially identical with the height of urceolus, or is less than the height of urceolus, and both differences in height are no more than 1/3rd of the diameter of circular cross-section.
Further, urceolus has equilateral polygon section, the axes normal of equilateral polygon section and urceolus; The height that swirl vane is fixed in the other end of urceolus is substantially identical with the height of urceolus, or is less than the height of urceolus, and both differences in height are no more than 1/3rd of the most long-diagonal length of equilateral polygon section.
Further, the axis of multiple cyclone is parallel to each other.
Further, multiple cyclone lays respectively at two and is formed in V-shaped or lambdoid plane, and the axis being positioned at the cyclone of same plane is parallel to each other.
Further, the elevation angle of swirl vane, namely swirl vane passes through the angle α that formed between length direction and the level cross-sectionn of urceolus extended, and is 12.5 ~ 60 °, is 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 set to identical, to reduce the cost of investment of device.Can adopt the cyclone of differentiation for different regions, to adapt to the gas flowfield of zones of different, the swirl vane quantity in such as cyclone is different, and the diameter of urceolus height that is different or cyclone is not identical.Scientifically implement differentiation layout and will produce more useful effect to the polymerization of fine solid particle and fine droplet.
Further, in order to improve service life and the structural strength of cyclone, preferably swirl vane, center column and urceolus are manufactured in aggregates, namely one-body molded.
Further, polymerizer also comprises the fixture for installing cyclone, and fixture is provided with the installing hole for installing cyclone, multiple cyclone is arranged on fixture by installing hole; Fixture is also provided with passage.The pressure loss acting as reduction polymerizer of passage, and avoid polymerizer to produce hydrops pond, thus maintain the polymerization of polymerizer.
Further, fixture is planar structure on the whole, and the multiple cyclones be arranged on fixture are in same plane, and the axis of multiple cyclone is parallel to each other.
Further, fixture comprises the plane that two form herringbone or V-shaped, and the axis being arranged on the cyclone in same plane is parallel to each other.
The operation principle of the above-mentioned polymerizer for being polymerized fine particle of the present utility model is as follows:
Cyclone in polymerizer can realize dust with dust polymerization, drop is polymerized with bulky grain with polymerization of fluid drops, bulky grain with polymerization of fluid drops, dust, granule is polymerized with granule, bulky grain is polymerized with granule, and occur once to be polymerized simultaneously, after polymerization is even repeatedly polymerized.
There are following three large effects and impel above-mentioned polymerization process in the swirl vane in cyclone:
First, the effect of chasing that large drop and (or) large dust pursue and attack droplet and (or) little dust causes drop and (or) dust to be grown up.Carry the air-flow of a large amount of fine droplet and (or) fine solid particle after cyclone, airflow direction changes, and produces swirling eddy.Swirl vane due to adjacent two cyclones is clockwise or counter clockwise direction, so the coupled zone that crosses of adjacent two cyclones produces gas flow counterflow effect, backwash effect occurs, and cause flue gas flow rate to decline, but (density is 1000 ~ 1200Kg/m due to drop
3) and (or) dust (bulk density is approximately 1600 ~ 2200kg/m
3) density higher than air-flow, (density is 1.1-1.3Kg/m far away
3) density, therefore drop and (or) dust are under higher inertia force effect and with progressive air-flow generation Relative sliding, and there is certain viscosity (under 1 atmospheric pressure, 50 DEG C of operating modes dynamic viscosity about 1.96 × 10 due to air-flow
-5pa.s) viscous force (i.e. viscosity internal friction is produced to drop and (or) dust that Relative sliding occurs, proportional with the surface area of dust and (or) drop) stop this Relative sliding, because the specific area of more small drop and (or) dust is large, so the Relative sliding speed of larger drop and (or) larger dust is higher than compared with droplet and (or) less dust, therefore also very large probability will more droplet and (or) less dust be caught thus are caused drop and (or) dust to be grown up by pursuing and attacking more droplet and (or) less dust effect for larger drop and (or) larger dust.
Secondly, the fine solid particle directly caused in flue gas stream and (or) fine droplet and the fine droplet come head-on in air-flow and (or) fine solid particle directly collide thus realize dust and (or) drop is grown up by adjacent two cyclones the cross backwash effect of coupling regime in opposite directions.Swirl vane due to adjacent two cyclones is clockwise or counter clockwise direction, so the coupling regime that crosses of adjacent two cyclones produces gas flow counterflow effect, a large amount of fine solid particle in air-flow and (or) fine droplet and the fine solid particle in oncoming air-flow and (or) fine droplet collide cause occurring between dust and dust, between dust and drop, between drop and drop being once polymerized, after polymerization even repeatedly be polymerized thus forms large dust and (or) droplet particles greatly.
Again, high velocity air causes the liquid film rested on swirl vane again to be rolled phenomenon (call in the following text and carry phenomenon) and forms newly-increased super large drop, super large droplet capture fine solid particle and (or) drop effect.Drop under the corrugated sheet separator of downstream position or condensation wet film whizzer are separated forms moisture film and can converge under gravity on the swirl vane of cyclone, it can form the liquid film of thin layer on the surface, through the cyclone of particular design, when flue gas flows through the narrow and small runner formed between adjacent two swirl vanes, the phenomenon of carrying occurred will form a large amount of super large drops, these newly-increased super large drops, increase in effect will play more huge polymerization at above-mentioned two kinds of drops and (or) dust.
The utility model additionally provides a kind of flue gas flow channel, comprise one or more levels above-mentioned any one for being polymerized the polymerizer of fine particle, polymerizer is arranged on the section of the flue gas stream containing fine particle.
Further, the plane at polymerizer place and the direction of flue gas stream substantially vertical.
Further, the plane at polymerizer place and the direction of flue gas stream have angle β, and angle β is 22.5 ~ 65 °.
Further, flue gas flow channel adopts steel infrastructure partitions to arrange, is correspondingly provided with polymerizer in the plane at place, each district.
Further, the multiple cyclones being arranged on the polymerizer in each district lay respectively at two and are formed in V-shaped or lambdoid plane.
Further, the diameter of described flue gas flow channel is 1.5 ~ 30m.
The above-mentioned polymerizer for being polymerized fine particle provided due to the utility model mainly realizes fine particulates polymerization, in actual applications, usually be not suitable for using as separator separately, therefore the utility model additionally provides a kind of dedusting demist integral system, this system comprise one or more levels above-mentioned any one for being polymerized fine particle polymerizer, the upstream of this polymerizer and/or downstream position are provided with curved channel formula separator, resolution element in curved channel formula separator forms multiple bending gas channel, make air-flow through multiple bending gas channel, air-flow constantly changes flow direction, drop in air-flow clashes into resolution element under centrifugal action, the drop impinging upon resolution element in a large number forms moisture film, moisture film falls after rise under gravity.
Further, the distance of polymerizer and curved channel formula separator is less than 1500mm.
Preferably, the distance of polymerizer and curved channel formula separator is less than 50mm.
Further, resolution element in curved channel formula separator is corrugated plating assembly, thus this curved channel formula separator is corrugated plate dst gas-liquid separator, corrugated plating that corrugated plating assembly comprises multiple interval, that be evenly arranged, multiple chevron-shaped becomes bending gas channel, makes air-flow constantly change flow direction; Distance between adjacent two corrugated platings is 10 ~ 60mm; Corrugated plating is preferably sinusoidal corrugated sheet, and corrugated plating has the accessory structure such as hook and/or hole, and hook and Kong Jun have 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 the temperature of air-flow, and cooling medium is supplied by cooling medium supply system.Now this corrugated plate dst gas-liquid separator is specially condensation wet film whizzer.
Further, the interior diameter of the urceolus in cyclone is preferably identical with the distance of adjacent two corrugated platings in curved channel formula separator, and the exit flow of cyclone completely receive by this two corrugated plating.
Further, resolution element in curved channel formula separator is 2 ~ 5 layers of interlaced tube bank, thus curved channel formula separator is tubular type gas-liquid separator, pipe that every one deck tube bank comprises multiple interval, that be evenly arranged, pipe in adjacent two layers tube bank is interlaced arrangement, form bending airflow path, make air-flow constantly change flow direction; The center distance being in the pipe in same layer tube bank is 1.2 ~ 4 times of the caliber of this layer of tube bank; The cross sectional form of pipe is circular, water-drop-shaped or bullet-headed etc. is applicable to aerodynamic cross section.
The utility model additionally provides another kind of dedusting demist integral system, comprise one or more levels above-mentioned any one for being polymerized the polymerizer of fine particle, the upstream position of polymerizer is provided with one or more levels preseparator, and/or the downstream position of polymerizer is provided with one or more levels meticulous separator and/or one or more levels hyperfine separator;
Meticulous separator has the drop separation performance higher than preseparator, and hyperfine separator has the drop separation performance higher than meticulous separator.
Further, preseparator comprises curved channel formula separator, or meticulous separator comprises curved channel formula separator.
Further, preseparator is one or more the combination in tube designs preseparator, slab design preseparator, roof layouts preseparator, horizontal gas flow preseparator; Hyperfine separator is one or more the combination in the hyperfine separator of slab design, the hyperfine separator of roof layouts, the hyperfine separator of horizontal gas flow.
Further, one or more levels preseparator, one or more levels polymerizer and one or more levels meticulous separator and/or hyperfine separator are all arranged in smoke absorption tower, and 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 meticulous separator and/or hyperfine separator are all arranged in absorption tower outlet horizontal flue, and the flow direction of air-flow is horizontal direction.
Further, a part in one or more levels preseparator, one or more levels polymerizer and one or more levels meticulous separator and/or hyperfine separator is arranged in absorption tower, another part is arranged in absorption tower outlet horizontal flue, in absorption tower, air-flow is vertical direction, and in the Horizontal Exit flue of absorption tower, air-flow in horizontal direction.
Further, any one-level preseparator, any one-level polymerizer and the meticulous separator of any one-level and/or hyperfine separator all need to survey in each self-corresponding air flow inlet side and/or air stream outlet to be provided with automatically and/or manual cleaning device according to actual operating mode, and cleaning device comprises pipeline and flooding nozzle.
In better embodiment of the present utility model, dedusting demist integral system is arranged in the downstream position of smoke absorption tower, the preseparator of air-flow successively in dedusting demist integral system, fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and hyperfine separator etc., preseparator, fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and hyperfine separator all can be arranged in smoke absorption tower inner top position, also can all be arranged in smoke absorption tower outlet horizontal flue, also can a part be arranged in inner top position, an absorption tower part be arranged in smoke absorption tower outlet horizontal flue in, space by each project scene determined by specific embodiment.
Preseparator, its major function removes the large drop of smoke absorption tower spraying layer generation, and for the large drop of particle diameter more than 18 microns, its removal efficiency can reach 100%; For the drop of particle diameter 5 ~ 18 microns, have separative efficiency in various degree, drop is less, and separative efficiency is lower, and drop is larger, and separative efficiency is higher; For the drop of particle diameter less than 5 microns, do not have separating effect in theory, the drop that only there is few quantity impinges upon on resolution element and is blocked removal.Typical coal fired power plant flue gas desulfurization absorption tower, former flue gas, after the washing of 3-6 layer spraying layer, about has 10000mg/Nm
3drop may enter preseparator, therefore first need a large amount of concentration of liquid drops to be reduced to≤75mg/Nm
3, be even less than≤35mg/Nm
3.
Preseparator preferably adopts one-level pipe separator, one-level thick roof separator and one-level thin roof separator.
Pipe separator, preferably adopt the pipe of 2 ~ 3 layers of interlaced arrangement as resolution element, the spacing of same layer pipe preferably adopts 90 ~ 110mm, and pipe diameter preferably selects D50 ~ D90; Pipe be horizontally disposed (installing in absorption tower) or be arranged vertically (absorption tower outlet horizontal flue in install);
Thick roof separator, preferably adopt like sine bellows thin plate as resolution element, interval S between adjacent two corrugated sheets preferably selects 25 ~ 30mm, and resolution element angle of inclination (angle of resolution element and horizontal plane) preferably selects 25 ~ 37.5 °; Roof separator can arrange in " V " font or " people " font is arranged, preferably selects " people " font to arrange.
Thin roof demister, preferably adopt like sine bellows thin plate as resolution element, resolution element buckle designs, and between adjacent two corrugated sheets, spacing is stated S and preferably selected 22.0 ~ 27.5mm, and resolution element angle of inclination preferably selects 25 ~ 37.5 °; Thin roof separator can arrange in " V " font or " people " font is arranged.
As long as the concentration of liquid drops that the type selecting of preseparator meets preseparator rear is less than 75mg/Nm
3, preferably consider to be less than 35mg/Nm
3therefore preseparator adopts other prior art, such as one-level pipe separator, the flat separator of one-level and one-level thin roof demister, also only can adopt one-level pipe separator and one-level thin roof separator or one-level thick roof separator and one-level thin roof separator, the pollutant emission of this set on neat stress slightly affects.
Further, when fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) are designed to more than two-stage or two-stage time, preseparator is preferably one-level pipe separator and one-level roof separator, and the concentration of liquid drops at preseparator rear is less than 150mg/Nm
3usually be also feasible.
Condensation wet film whizzer, its major function is that the fine droplet crossed by fine particle aggregator aggregates and fine solid particle are carried out secondary increase by condensing mode by the further degree of depth again, simultaneously because self structure form is how curved bellows-shaped, have remarkable drop separation performance concurrently.Increased by condensing mode secondary, show through test, when controlling suitable condensing water vapor amount of precipitation well, the particle diameter of all fine droplets and fine solid particle all will can be increased to more than 6 microns, the particle diameter of most drop is more than 10 microns, even more than 13 microns, the fine droplet after these increases and fine solid particle are enough to make self to show very outstanding separating property as separator effect and follow-up hyperfine separator.
Condensation wet film whizzer, its resolution element is preferably the corrugated plating of hollow, interior stream has cooling water, saturated wet flue gas is through condensation wet film whizzer, flue-gas temperature declines and separates out a large amount of steam, the remaining fine droplet of the steam Automatic-searching produced and (or) minute dusts are as the nuclei of condensation, and fine droplet and (or) minute dusts are grown up after adsorbing a large amount of steam, will be subject to larger centrifugal force under same gas flow velocity; The dust of what is more important irregular surface is by becoming spheroid after absorption steam, dust and smoke contacts be converted into water droplet and smoke contacts thus significantly reduce the viscous force between dust and flue gas, form larger centrifugal force thus impinge upon on resolution element when therefore flowing in bending runner.And there is cold-wall effect due to hollow corrugation plate, the uniform and stable moisture film of one deck can be formed at the outer surface of hollow corrugation plate, the drop and (or) the dust that impinge upon hollow corrugation plate are buried in oblivion instantaneously by moisture film, fine droplet and (or) minute dusts are captured and tackle and remove.
When soot emissions require can lower slightly time (such as allow dust concentration be less than 10mg/Nm
3), the selectable technical scheme of having to take the second best adopts traditional flat separator or roof type separator to replace condensation wet film whizzer, namely resolution element does not have hollow structure, does not have condensation and increases function to fine solid particle and (or) fine droplet.
It should be noted that, result of the test shows, when fine particle polymerizer and condensation wet film whizzer (or corrugated plate dst gas-liquid separator) combinationally use, generation is made us very pleasantly surprised polymerization effect and separating effect, the performance after its combination will far away higher than fine particle polymerizer and condensation wet film whizzer (or corrugated plate dst gas-liquid separator) respective single polymerization effect and separating effect sum.
Hyperfine separator, has unsurpassed separating property, and after corresponding operation optimization design, its limit size droplet diameter can be low to moderate 12 ~ 13 microns, the drops of 10 microns is had to the separative efficiency of more than 80%; The drops of 8 microns are had to the separative efficiency of more than 60%; The drops of 6 microns are had to the separative efficiency of more than 40%.
Limit size droplet diameter refers to that this drop is by 100% separated removal when the particle diameter of drop reaches or exceedes this size.Therefore limit size droplet diameter is the most important performance technologies index of separator.
What can contrast is, existing thin roof separator, sine bellows thin plate, the swirl vane spacing of the curved hook of usual employing two are 22 ~ 25mm, angle of inclination is 35 ~ 37.5 °, under design void tower flue gas flow rate 3.85m/ spacing, limit size droplet diameter is about 18 microns.
Hyperfine separator, limit size droplet diameter is low to moderate 12 ~ 13 microns, is only about 1/3 of 18 micro droplets quality.
Hyperfine separator, preferably adopt three curved seemingly sine bellows thin plates as resolution element, resolution element band one hook and hole design, between adjacent two corrugated sheets, interval S preferably selects 22.0 ~ 33.0mm, and angle of inclination preferably selects 30 ~ 37.5 °.
Hyperfine separator, preferably designs net area rate >=85%, in little absorption tower, (is such as less than 10m), and design net area rate is not less than 80% usually.
High-effective dust-removing demist integral system of the present utility model, air-flow is successively after preseparator, fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and hyperfine separator, and droplet content will be less than 10.0mg/Nm
3(adopt Mg
2+trace method) or be less than 1.0mg/Nm
3(adopting T ü V>15 micron impingement method to detect); When adopting two-stage or multistage fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) is when designing, and droplet content will be less than 5.0mg/Nm
3(adopt Mg
2+trace method) or be less than 0.5mg/Nm
3(adopting T ü V>15 micron impingement method to detect).What droplet separating effect showed higher than high efficiency demister (such as three grades of roof demisters) far away removes fog effect.
High-effective dust-removing demist integral system of the present utility model, air-flow is successively after preseparator, fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and hyperfine separator, and when absorption tower, Inlet dust is less than 20mg/Nm
3under, can guarantee that dust concentration remaining in air-flow is less than 3.5mg/Nm
3; When desulfuration absorbing tower Inlet dust is less than 30mg/Nm
3under, can guarantee that dust concentration remaining in air-flow is less than 5.0mg/Nm
3; When desulfuration absorbing tower Inlet dust is less than 50mg/Nm
3under, can guarantee that dust concentration remaining in air-flow is less than 10.0mg/Nm
3.According to two-stage or multistage fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator), no matter entrance content is how many, can realize being less than 5.0mg/Nm
3.
A kind of high-effective dust-removing demist integral system of the present utility model, if the concentration of liquid drops in air-flow itself is not high, can cancel preprocessor, only adopts fine particle polymerizer, condensation wet film whizzer and hyperfine separator.
A kind of high-effective dust-removing demist integral system of the present utility model, if the concentration of liquid drops in air-flow itself is not high, outlet dust concentration is also less demanding, and such as entrance dust concentration is 50mg/Nm
3, outlet dust concentration allows to be less than 20mg/Nm
3, preprocessor and hyperfine separator can be cancelled, only adopt fine particle polymerizer, condensation wet film whizzer.
Whether a kind of high-effective dust-removing demist integral system of the present utility model, adopt preprocessor or hyperfine separator or adopt 1 grade or multistage fine particle polymerizer all to depend on design parameter.After the design parameter provided, utilize computer Simulation calculation and do design modification can meet in conjunction with scientific experiment, engineering practice.
A kind of high-effective dust-removing demist integral system of the present utility model, owing to not being water droplet in applied environment, but slurry drops, so all need according to actual operating mode for any one-level preseparator, fine particle polymerizer, condensation wet film whizzer (or corrugated plate dst gas-liquid separator) and hyperfine separator and be provided with automatically (or manual) cleaning device in its air flow inlet side and (or) air stream outlet side, cleaning device is made up of pipeline and flooding nozzle.
Compared with prior art, dedusting demist integral system of the present utility model has following beneficial effect:
(1) high-effective dust-removing demist integral system of the present utility model is remarkable liquid drop separator is also remarkable dust separator;
(2) design of whole fume desulfurating absorption tower is more simplified, spraying layer, pallet, whirlwind coupling, FGD pula this etc. facility just absorb SO
2function, and additionally do not need to consider dust removal function;
(3) cost of investment of whole desulfurizer is reduced;
(4) reduce the operating cost of whole desulfurizer, meet national energy-saving and reduce discharging development strategy;
(5) by collision polymerization and the dual increase effect of condensation adsorption, fine solid particle and fine droplet are more effectively amplified, improves the overall efficiency of a whole set of dedusting demist integral system;
(6) equipment all adopts corrosion resistant nonmetallic materials, long service life;
(7) device regular maintenance cost is low, without the need to often changing parts;
(8) equipment dependability is high, can longtime running more than 25000hr.
Be described further below with reference to the technique effect of accompanying drawing to design of the present utility model, concrete structure and generation, to understand the purpose of this utility model, characteristic sum effect fully.
Accompanying drawing explanation
Fig. 1 is the structure sectional view of the high-effective dust-removing demist integral system of embodiment 1 of the present utility model;
Fig. 2 is the A-A profile 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 demist integral system of the utility model embodiment 1;
Fig. 7 is the third program structural representation of the high-effective dust-removing demist integral system of the utility model embodiment 1;
Fig. 8 is the fourth program structural representation of the high-effective dust-removing demist integral system of the utility model embodiment 1;
Fig. 9 is the first scheme structural representation of the high-effective dust-removing demist integral system of embodiment 2 of the present utility model;
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 a hole one hook-type corrugated plate dst structure of gas liquid separator schematic diagram;
Figure 13 is the alternative plan structural representation of the high-effective dust-removing demist integral system of embodiment 2 of the present utility model;
Figure 14 is the third program structural representation of the high-effective dust-removing demist integral system of embodiment 2 of the present utility model.
Detailed description of the invention
Embodiment 1
As shown in Figure 1, the first scheme of the high-effective dust-removing demist integral system of the present embodiment is that dedusting demist integral system is arranged in absorption tower, this system comprises fine particle polymerizer 20 and condensation wet film whizzer 30 two parts, and wherein fine particle polymerizer 20 and condensation wet film whizzer 30 are arranged on the section of the flue gas stream containing fine particle.The plane at fine particle polymerizer 20 place is substantially vertical with the direction of flue gas stream with the plane at condensation wet film whizzer 30 place.
Described fine particle polymerizer 20 and condensation wet film whizzer 30 are arranged on one deck brace summer.
Self-stripping system is provided with on the top of the bottom of fine particle polymerizer 20 and condensation wet film whizzer 30.
Described fine particle polymerizer 20 and condensation wet film whizzer 30 are close to (distance is less than 10mm) and form an entirety.
As shown in figs. 2 to 4, the fine particle polymerizer 20 of the present embodiment comprises multiple cyclone 21, each cyclone 21 comprises center column 212, urceolus 213 and s (s >=2) swirl vane 211, and swirl vane 211 can make the air-flow comprising fine particle by forming swirling eddy during cyclone 21.
In the present embodiment, cyclone 21 is set to have 6 swirl vanes 211.The swirl vane 211 of arbitrary neighborhood two cyclones 21 is counterclockwise (overlooking).One end of multiple swirl vane 211 is fixed in center column 212, and the other end is fixed in urceolus 213.The urceolus 213 of the present embodiment has circular cross-section, the axes normal of this circular cross-section and urceolus 213.The height that swirl vane 211 is fixed in the other end of urceolus 213 is substantially identical with the height of urceolus 213, or is less than the height of urceolus 213, and both differences in height are no more than 1/3rd of the diameter of the above-mentioned circular cross-section of urceolus 213.
Urceolus 213 also can have equilateral polygon section in other embodiments, and the axes normal of this regular polygon and urceolus 213, now to be fixed in the height of the other end of urceolus 213 substantially identical with the height of urceolus 213 for swirl vane 211, or be less than the height of urceolus 213, and both differences in height are no more than 1/3rd of the most long-diagonal length of the above-mentioned equilateral polygon section of urceolus 213.
In the present embodiment, multiple cyclone 21 is positioned at same plane, and the axis of multiple cyclone 21 is parallel to each other.In other embodiments, multiple cyclone 21 lays respectively at two and is formed in V-shaped or lambdoid plane, and the axis being positioned at the cyclone 21 of 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 adopts same size, and the interior diameter of urceolus 213 is 32.5mm.
In the present embodiment, cyclone 21 is formed for swirl vane 211, center column 212 and urceolus 213 being injected into a whole.
The fine particle polymerizer 20 of the present embodiment also comprises the fixture 22 for installing cyclone 21, and fixture 22 is provided with the installing hole 221 for installing fixing cyclone 21, multiple cyclone 21 is arranged on fixture 22 by installing hole 211.Fixture 22 is also provided with passage 222, and to reduce the pressure loss of polymerizer 20, and the polymerization of the polymerizer 20 avoided polymerizer to produce hydrops and cause reduces.
Fig. 5 is the fundamental diagram of the fine particle polymerizer 20 of the present embodiment, by the cyclone 21 of particular design (namely swirl vane 211 is designed to almost with the height of urceolus 213), can realize dust with dust polymerization, drop is polymerized with bulky grain with polymerization of fluid drops, bulky grain with polymerization of fluid drops, dust, granule is polymerized with granule, bulky grain is polymerized with granule, and occur once to be polymerized simultaneously, after polymerization is even repeatedly polymerized.
As shown in Figure 5, there are following three large effects and impel above-mentioned polymerization process in the swirl vane 211 in cyclone 21:
First, the effect of chasing that large drop and (or) large dust pursue and attack droplet and (or) little dust causes drop and (or) dust to be grown up.Carry the air-flow of a large amount of fine droplet and (or) fine solid particle after cyclone 21, airflow direction changes, and produces swirling eddy.Swirl vane 211 due to adjacent two cyclones 21 is clockwise or counter clockwise direction, so the coupled zone that crosses of adjacent two cyclones 21 produces gas flow counterflow effect, backwash effect occurs, and cause flue gas flow rate to decline, but (density is 1000 ~ 1200Kg/m due to drop
3) and (or) dust (bulk density is approximately 1600 ~ 2200kg/m
3) density higher than air-flow, (density is 1.1-1.3Kg/m far away
3) density, therefore drop and (or) dust are under higher inertia force effect and with progressive air-flow generation Relative sliding, and there is certain viscosity (under 1 atmospheric pressure, 50 DEG C of operating modes dynamic viscosity about 1.96 × 10 due to air-flow
-5pa.s) viscous force (i.e. viscosity internal friction is produced to drop and (or) dust that Relative sliding occurs, proportional with the surface area of dust and (or) drop) stop this Relative sliding, because the specific area of more small drop and (or) dust is large, so the Relative sliding speed of larger drop and (or) larger dust is higher than compared with droplet and (or) less dust, therefore also very large probability will more droplet and (or) less dust be caught thus are caused drop and (or) dust to be grown up by pursuing and attacking more droplet and (or) less dust effect for larger drop and (or) larger dust.
Secondly, the fine solid particle directly caused in flue gas stream and (or) fine droplet and the fine droplet come head-on in air-flow and (or) fine solid particle directly collide thus realize dust and (or) drop is grown up by adjacent two cyclones 21 the cross backwash effect of coupling regime in opposite directions.Swirl vane due to adjacent two cyclones 21 is clockwise or counter clockwise direction, so the coupling regime that crosses of adjacent two cyclones 21 produces gas flow counterflow effect, a large amount of fine solid particle in air-flow and (or) fine droplet and the fine solid particle in oncoming air-flow and (or) fine droplet collide cause occurring between dust and dust, between dust and drop, between drop and drop being once polymerized, after polymerization even repeatedly be polymerized thus forms large dust and (or) droplet particles greatly.
Again, high velocity air causes the liquid film rested on swirl vane again to be rolled phenomenon (call in the following text and carry phenomenon) and forms newly-increased super large drop, super large droplet capture fine solid particle and (or) drop effect.Drop under condensation wet film whizzer 30 separation of downstream position forms moisture film and can converge under gravity on the swirl vane 211 of cyclone, it can form the liquid film of thin layer on the surface, after cyclone 21, when flue gas flows through the narrow and small runner formed between adjacent two swirl vanes 211, the phenomenon of carrying occurred will form a large amount of super large drops, these newly-increased super large drops, increase in effect will play more huge polymerization at above-mentioned two kinds of drops and (or) dust.
The resolution element of condensation wet film whizzer 30 adopts three curved ripple hollow sheetings 31, and interior stream has recirculated cooling water 32.Adjacent two ripple hollow sheeting interval S are 32.5mm.
Carry the air-flow of drop and dust after the above-mentioned high-effective dust-removing demist integral system of the present embodiment, the remaining droplet content of air-flow will be less than 40mg/Nm
3; When high-effective dust-removing demist integral system Inlet dust concentration is less than 50mg/Nm
3time, outlet dust concentration will be less than 20mg/Nm
3, namely efficiency of dust collection is more than 60%.
As shown in Figure 6, the selectable alternative plan of the present embodiment is that the corrugated plate dst gas-liquid separator 302 that to adopt with solid corrugated plating by condensation wet film whizzer 30 be resolution element replaces, namely high-effective dust-removing demist integral system comprises fine particle polymerizer 20 and corrugated plate dst gas-liquid separator 302 two parts, and with air-flow in being arranged vertically.The resolution element of corrugated plate dst gas-liquid separator 302 can be two curved like sine wave curve without hook-type, as shown in Figure 1 three curved ripple hollow sheetings 31; Or two is curved like sine wave curve band hook-type, the resolution element 132 of buckle as shown in Figure 10; Three curved like sine wave curve without hook-type, three curved like sine wave curve band hook-types, with one or more hole and (or) hook-type etc.
As shown in Figure 7, in the selectable third program of the present embodiment, high-effective dust-removing demist integral system comprises fine particle polymerizer 20 and condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) two parts, in this programme, by fine particle polymerizer 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) adopts and is in tilted layout, namely have angle with flue gas flow path direction structure β (β is greater than 0 °), the angle β that wherein plane at fine particle polymerizer 20 place and the direction of flue gas stream are formed is 22.5 ~ 65 °, its Main Function is the effective area of raising separator and improves developing result.
As shown in Figure 8, in the selectable fourth program of the present embodiment, high-effective dust-removing demist integral system comprises fine particle polymerizer 20 and condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) two parts, and adopting herringbone or V-shaped to arrange fine particle polymerizer 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator), its Main Function is the effective area of raising separator and improves developing result.For large flue gas flow channel (such as diameter is 1.5 ~ 3m), flue gas flow channel adopts steel infrastructure partitions to arrange, correspondingly be provided with fine particle polymerizer 20 in the plane at place, each district, the multiple cyclones 21 being wherein arranged on the fine particle polymerizer 20 in each district lay respectively in two planes forming herringbone or V-shaped.
Embodiment 2
As shown in Figure 9, the dedusting demist integral system of the present embodiment comprises one-level preprocessor 10, fine particle polymerizer 20, condensation wet film whizzer 30 (or corrugated plate dst gas-liquid separator) and hyperfine separator 40, and be all arranged in absorption tower.
Boiler exit gas after electric cleaner dust concentration with≤20mg/Nm
3enter desulfuration absorbing tower 60.Be provided with in absorption tower 60 3 ~ 6 layers of spraying layer 70 and possible 1 ~ 2 layer of pallet or FGD pula this 80, flue gas through pallet or FGD pula this 80 and spraying layer 70 after successively through preprocessor 10, fine particle polymerizer 20, condensation wet film whizzer 30 and hyperfine separator 40.Arrow in Fig. 9 indicates the flow direction of flue gas.
Described preseparator 10 comprises one-level pipe separator 11, one-level thick roof separator 12 and one-level thin roof separator 13.
Tubular demister 11 is horizontally disposed in absorption tower, comprises the pipe 111 that two rows or three rows are staggeredly arranged, and as shown in Figure 10, wherein often arrange pipe 111 and be in level, pipe 111 is free to rotate.Between adjacent pipe 111 in same row, center distance is 90 ~ 120mm, and pipe 111 caliber is
the two ends of pipe 111 have pipe stopper 112, and cover has end plate 113, and on pipe 111, cover has multiple central dividing plate 114.Multiple pipe 111 is fitted together by central dividing plate 114 and end plate 113.Carry the flue gas of a large amount of drop after pipe separator 11, volume ratio 85 ~ 90% drop remove by pipe separator 11, and flue gas obtains effective rectification.
Figure 11 shows thick roof separator 12 and thin roof separator 13, both differences are that resolution element is different, the left module of thick roof separator and the resolution element 121 not buckle of right module, the left module of thin roof separator and right module resolution element 131 buckle.Specifically, thick roof type demister and thin roof demister comprise first wave card assembly 121 and Second Wave card assembly 131 respectively, first wave card assembly 121 and Second Wave card assembly 131 form by multi-disc corrugated sheet, the cross section of corrugated plating has half-sine wave shape, and the distance between adjacent corrugated plate is 20.0 ~ 40mm.Corrugated plating in Second Wave card assembly 131 is provided with hook portion 132, and the opening direction of this hook portion 132 is contrary with the flow direction of flue gas, and this hook portion 132 is positioned at crest place or the trough place of half-sine wave shape.First wave card assembly 121 and Second Wave card assembly 131 are combined to form " people " font and arrange, the thickness of corrugated plating is preferably 2.0 ~ 3.5mm.Flue gas, after meticulous roof type demister 13, has only remained small drop in neat stress, concentration of liquid drops can≤35mg/Nm
3.
The fine particle polymerizer 20 of this high-effective dust-removing demist integral system is identical with the first scheme of embodiment one with condensation wet film whizzer 30.
Hyperfine separator 40 is made up of multi-disc corrugated plating 41, and as shown in figure 12, the cross section of corrugated plating is the sine wave shape at least comprising a wavelength; Arrange porose 411 at the crest place of sine wave shape, the trough place of sine wave shape is provided with hook portion 412; Or arrange porose 411 at the trough place of sine wave shape, the crest place of sine wave shape is provided with hook portion 412.Wherein, the opening direction of hook portion 412 is contrary with the flow direction of flue gas.Distance between adjacent corrugated plate is preferably 20.0 ~ 38mm.Preferably be designed to little in the region that flue gas flow rate is high by the distance between corrugated plating, the distance between corrugated plating is designed to greatly by the region low at flue gas flow rate.Corrugated plating spacing also can adopt constant spacing.Corrugated plating is in being in tilted layout, and be specially in herringbone or V-shaped layout, the angle of inclination (angle of corrugated plating and horizontal plane) of corrugated plating is preferably 28 ~ 39.0 °, and the thickness of corrugated plating is preferably 2.0 ~ 3.5mm.Flue gas is after hyperfine demister, and the drop 100% being greater than 13 microns for particle diameter in neat stress is removed separation; The drop of particle diameter 10 microns is had to the separative efficiency of more than 80%; The drop of particle diameter 8 microns is had to the separative efficiency of more than 60%; The drop of particle diameter 6 microns is had to the separative efficiency of more than 40%.
In the present embodiment, pipe separator 11 and thick roof type separator 12 are arranged on lower layer support beam; Thin roof type separator 13 is arranged on the brace summer of intermediate layer; Fine particle polymerizer 20, condensation wet film whizzer 30 and the hyperfine separator 40 of roof type are arranged on the brace summer of upper strata.
Block for avoiding the high-effective dust-removing demist integral system of the present embodiment, be provided with six layers of rinse-system 50, ground floor rinse-system 51 is used for rinsing the upstream side of pipe separator 11 downstream and thick roof separator 12, second layer rinse-system 52 is used for rushing the downstream of thick roof separator 11, third layer rinse-system 53 is used for the upstream side of thin thick roof separator 13, 4th layer of rinse-system 54 is used for rinsing fine particle polymerizer 20, and take into account the downstream rinsing thin thick roof separator 13, layer 5 rinse-system 55 is used for rinsing hyperfine separator 40 upstream side, and take into account the downstream rinsing thin condensation wet film whizzer 30, layer 6 rinse-system 56 is used for rinsing hyperfine separator 40 downstream.First rinses 51 ~ 56 to layer 5 adopts self-stripping system, and layer 6 rinse-system 56 adopts manual flushing system, also can adopt self-stripping system.
Adopt the present embodiment high-effective dust-removing demist integral system, as entrance dust concentration≤20mg/Nm
3time, the smoke content≤3.5mg/Nm in flue gas can be made
3; When desulfuration absorbing tower Inlet dust is less than 30mg/Nm
3under, can guarantee that dust concentration remaining in air-flow is less than 5.0mg/Nm
3; When desulfuration absorbing tower Inlet dust is less than 50mg/Nm
3under, can guarantee that dust concentration remaining in air-flow is less than 10.0mg/Nm
3; Droplet content will be less than 10.0mg/Nm
3(adopt Mg
2+trace method) or be less than 1.0mg/Nm
3(adopting T ü V>15 micron impingement method to detect).
Be subject to the restriction in space, on-the-spot absorption tower 60, the hyperfine separator 40 of the high-effective dust-removing demist integral system in Fig. 9 can be arranged in horizontal flue 601 (as shown in figure 13).Flue gas (comprises tubular type preseparator 11 through one-level preseparator, 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 fine particle 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, in absorption tower 60, be not provided with the installing space of separator, the present embodiment high-effective dust-removing demist integral system can be arranged in the outlet horizontal flue 601 on absorption tower 60.Wherein flue gas (comprises tubular type preseparator 11 through one-level preseparator, horizontal gas flow coarse separator 12, horizontal gas flow thickness 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.(as shown in figure 14).
No matter hyperfine horizontal gas flow separator 40 or whole high-effective dust-removing demist integral system are disposed in outlet horizontal flue, Insulation can not be taked in order to reduce the overall cost of desulphurization system at the flue shell body of the upstream position of hyperfine horizontal gas flow separator 40 or whole high-effective dust-removing demist integral system, condensed water can catch sub-fraction fine solid particle and mist droplet simultaneously, these condensed waters can be installed in hyperfine horizontal gas flow separator 40 in horizontal flue or whole high-effective dust-removing demist removal that integral system is tackled, therefore improve dedusting on the contrary and remove fog effect.
More than describe preferred embodiment of the present utility model in detail.Should be appreciated that those of ordinary skill in the art just can make many modifications and variations according to design of the present utility model without the need to creative work.Therefore, all technical staff in the art according to design of the present utility model on the basis of existing technology by the available technical scheme of logical analysis, reasoning, or a limited experiment, all should by the determined protection domain of claims.
Claims (32)
1. one kind for being polymerized the polymerizer of fine particle, it is characterized in that, described polymerizer comprises one or more cyclone, described cyclone comprises at least two swirl vanes, center column and urceolus, one end of described swirl vane is fixed in described center column, the other end is fixed in described urceolus, makes the air-flow comprising fine particle by forming swirling eddy during described cyclone.
2. as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, when described polymerizer comprises multiple described cyclone, the setting direction of the described swirl vane in any two adjacent described cyclones is identical.
3. as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, described urceolus has circular cross-section, the axes normal of described circular cross-section and described urceolus.
4. as claimed in claim 3 for being polymerized the polymerizer of fine particle, it is characterized in that, the height that described swirl vane is fixed in the described other end of described urceolus is substantially identical with the height of described urceolus, or be less than the height of described urceolus, and both differences in height are no more than 1/3rd of the diameter of described circular cross-section.
5. as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, described urceolus has equilateral polygon section, the axes normal of described equilateral polygon section and described urceolus.
6. as claimed in claim 5 for being polymerized the polymerizer of fine particle, it is characterized in that, the height that described swirl vane is fixed in the described other end of described urceolus is substantially identical with the height of described urceolus, or be less than the height of described urceolus, and both differences in height are no more than 1/3rd of the most long-diagonal length of described equilateral polygon section.
7. as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, the axis of described multiple cyclone is parallel to each other.
8. as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, described multiple cyclone lays respectively at two and is formed in V-shaped or lambdoid plane, and the axis being positioned at the cyclone of same plane is parallel to each other.
9. as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, the elevation angle of described swirl vane is 12.5 ~ 60 °.
10. as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, the quantity of described swirl vane is 3 ~ 18.
11. is as claimed in claim 10 for being polymerized the polymerizer of fine particle, and it is characterized in that, the quantity of described swirl vane is 6 ~ 8.
12. is as claimed in claim 1 for being polymerized the polymerizer of fine particle, it is characterized in that, described polymerizer also comprises the fixture for installing described cyclone, described fixture is provided with the installing hole for installing described cyclone, described multiple cyclone is arranged on described fixture by described installing hole; Described fixture is also provided with passage.
13. is as claimed in claim 12 for being polymerized the polymerizer of fine particle, it is characterized in that, described fixture is planar structure on the whole, and the described multiple cyclone be arranged on described fixture is in same plane, and the axis of described multiple cyclone is parallel to each other.
14., as claimed in claim 12 for being polymerized the polymerizer of fine particle, is characterized in that, described fixture comprises the plane that two form herringbones or V-shaped, and the axis being arranged on the cyclone in same plane is parallel to each other.
15. 1 kinds of flue gas flow channels, is characterized in that, comprise one or more levels as the polymerizer for being polymerized fine particle in claim 1 ~ 14 as described in any one, described polymerizer is arranged on the section of the flue gas stream containing fine particle.
16. flue gas flow channels as claimed in claim 15, it is characterized in that, the plane at described polymerizer place is substantially vertical with the direction of described flue gas stream.
17. flue gas flow channels as claimed in claim 15, is characterized in that, the plane at described polymerizer place and the direction of described flue gas stream have angle β, and described angle β is 22.5 ~ 65 °.
18. flue gas flow channels as claimed in claim 15, is characterized in that, described flue gas flow channel adopts steel infrastructure partitions to arrange, is correspondingly provided with described polymerizer in the plane at place, each district.
19. flue gas flow channels as claimed in claim 18, is characterized in that, the described multiple cyclone being arranged on the described polymerizer in each district lays respectively at two and formed in V-shaped or lambdoid plane.
20. 1 kinds of dedusting demist integral systems, it is characterized in that, comprise one or more levels as the polymerizer for being polymerized fine particle in claim 1 ~ 15 as described in any one, the upstream of described polymerizer and/or downstream position are provided with curved channel formula separator, and the resolution element in described curved channel formula separator forms multiple bending gas channel.
21. dedusting demist integral systems as claimed in claim 20, is characterized in that, the distance of described polymerizer and described curved channel formula separator is less than 1500mm.
22. dedusting demist integral systems as claimed in claim 21, is characterized in that, the distance of described polymerizer and described curved channel formula separator is less than 50mm.
23. dedusting demist integral systems as claimed in claim 20, it is characterized in that, resolution element in described curved channel formula separator is corrugated plating assembly, corrugated plating that described corrugated plating assembly comprises multiple interval, that be evenly arranged, and multiple described chevron-shaped becomes bending gas channel; Distance described in adjacent two between corrugated plating is 10 ~ 60mm; Described corrugated plating is sinusoidal corrugated plating, and described corrugated plating has hook and/or hole, and described hook and described Kong Jun have one or more; The thickness of described corrugated plating is 1.0 ~ 3.5mm.
24. dedusting demist integral systems as claimed in claim 23, it is characterized in that, described corrugated plating is hollow structure, and interior stream has cooling medium, the temperature of described cooling medium is less than the temperature of described air-flow, and described cooling medium is supplied by cooling medium supply system.
25. dedusting demist integral systems as claimed in claim 20, it is characterized in that, resolution element in described curved channel formula separator is 2 ~ 5 layers of interlaced tube bank, pipe that tube bank described in every one deck comprises multiple interval, that be evenly arranged, pipe in tube bank described in adjacent two layers is interlaced arrangement, forms bending airflow path; The center distance being in the pipe in tube bank described in same layer is 1.2 ~ 4 times of the caliber of this layer of tube bank; The cross sectional form of described pipe is circular, water-drop-shaped or bullet-headed.
26. 1 kinds of dedusting demist integral systems, comprise one or more levels as the polymerizer for being polymerized fine particle in claim 1 ~ 15 as described in any one, the upstream position of described polymerizer is provided with one or more levels preseparator, and/or the downstream position of described polymerizer is provided with one or more levels meticulous separator and/or one or more levels hyperfine separator;
Described meticulous separator has the drop separation performance higher than described preseparator, and described hyperfine separator has the drop separation performance higher than described meticulous separator.
27. dedusting demist integral systems as claimed in claim 26, it is characterized in that, described preseparator comprises curved channel formula separator, or described meticulous separator comprises curved channel formula separator.
28. dedusting demist integral systems as claimed in claim 26, is characterized in that, described preseparator is one or more the combination in tube designs preseparator, slab design preseparator, roof layouts preseparator, horizontal gas flow preseparator; Described hyperfine separator is one or more the combination in the hyperfine separator of slab design, the hyperfine separator of roof layouts, the hyperfine separator of horizontal gas flow.
29. dedusting demist integral systems as claimed in claim 26, it is characterized in that, described in one or more levels, preseparator, polymerizer described in one or more levels and meticulous separator described in one or more levels and/or described hyperfine separator are all arranged in smoke absorption tower, and the flow direction of air-flow is vertical direction.
30. dedusting demist integral systems as claimed in claim 26, it is characterized in that, preseparator, polymerizer described in one or more levels and meticulous separator described in one or more levels and/or described hyperfine separator described in one or more levels are all arranged in absorption tower outlet horizontal flue, and the flow direction of air-flow is horizontal direction.
31. dedusting demist integral systems as claimed in claim 26, it is characterized in that, a part in preseparator, polymerizer described in one or more levels and meticulous separator described in one or more levels described in one or more levels and/or described hyperfine separator is arranged in absorption tower, another part is arranged in absorption tower outlet horizontal flue, in absorption tower, air-flow is vertical direction, and in the Horizontal Exit flue of absorption tower, air-flow in horizontal direction.
32. dedusting demist integral systems as claimed in claim 26, it is characterized in that, meticulous separator and/or described hyperfine separator described in polymerizer described in preseparator, any one-level described in any one-level and any one-level all need to survey in each self-corresponding air flow inlet side and/or air stream outlet to be provided with automatically and/or manual cleaning device according to actual operating mode, and described cleaning device comprises pipeline and flooding nozzle.
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| CN201520618652.1U CN205095604U (en) | 2015-08-17 | 2015-08-17 | Fine particle polymerizer, flue gas runner and high -efficient dust removal defogging integration system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105854428A (en) * | 2016-05-26 | 2016-08-17 | 北京龙腾华创环境能源技术有限公司 | Multistage spiral-flow type ultra-clean dust removal device |
| WO2017028152A1 (en) * | 2015-08-17 | 2017-02-23 | 德梅斯特(上海)环保科技有限公司 | Fine particle aggregator, and efficient integrated system for dust and mist removal |
| CN106693590A (en) * | 2015-08-17 | 2017-05-24 | 德梅斯特(上海)环保科技有限公司 | Fine particle polymerizer and high-efficiency dedusting defogging integrated system |
| CN108201706A (en) * | 2018-03-14 | 2018-06-26 | 重庆东钛化工有限公司 | The heat-engine plant desulfurized tower water cooling coagulating type demister circulatory system |
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| WO2017028152A1 (en) * | 2015-08-17 | 2017-02-23 | 德梅斯特(上海)环保科技有限公司 | Fine particle aggregator, and efficient integrated system for dust and mist removal |
| CN106693590A (en) * | 2015-08-17 | 2017-05-24 | 德梅斯特(上海)环保科技有限公司 | Fine particle polymerizer and high-efficiency dedusting defogging integrated system |
| CN105854428A (en) * | 2016-05-26 | 2016-08-17 | 北京龙腾华创环境能源技术有限公司 | Multistage spiral-flow type ultra-clean dust removal device |
| CN108201706A (en) * | 2018-03-14 | 2018-06-26 | 重庆东钛化工有限公司 | The heat-engine plant desulfurized tower water cooling coagulating type demister circulatory system |
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