CN104941323A - Multi-stage agglomeration and rotational flow combined method for removing liquid from gas - Google Patents
Multi-stage agglomeration and rotational flow combined method for removing liquid from gas Download PDFInfo
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Abstract
The invention provides a multi-stage agglomeration and rotational flow combined method for removing liquid from gas and belongs to the technical field of gas-liquid separation. The method is particularly used for dehydrating for removing liquid from gas discharged from a wet-process flue gas desulphurization device. According to the method, adopted devices comprise a tower body, an agglomeration zone, a multi-stage rotational flow liquid-removal zone and an exhaust barrel, wherein the agglomeration zone is composed of multi-stage staggered agglomeration plates; the multi-stage rotational flow liquid removal zone comprises a multi-stage cyclone and a connecting barrel; gas from a lower position is discharged from the exhaust barrel after being subjected to liquid removal through the agglomeration zone and the multi-stage rotational flow liquid removal zone and separated liquid is drained through a liquid drainage pipe and then flows into other lower zones.
Description
Technical field
The invention belongs to gas-liquid separation technical field, particularly relate to a kind of multi-stage agglomeration rotational flow gas liquid removing method.
Background technology
What flue gas desulfurization mostly adopted is wet processing, and namely so-called wet processing washs flue gas with the absorbent being mixed with slurries, by the SO in flue gas
2absorb in slurries, react with absorbent, its core apparatus is exactly absorption tower, reaction major part due to absorption tower all adopts fountain to wash, so containing a large amount of droplets in the flue gas processed, if these droplets of leaving take absorption tower out of, droplet will be discharged from chimney with flue gas, and fall around chimney, formed " light rain ", thus contaminated environment.From the angle of energy-conservation, a large amount of slurries are taken out of, and the operation for system is also a kind of loss, so flue gas generally will be added with liquid knockout after passing through washing.Be actually and the water droplet in the flue gas of washing is separated, allow water droplet get back in tower.Liquid knockout is the visual plant of flue gas desulphurization system, and the dehydration mechanism of liquid knockout is mainly divided into gravitational settling, collision separation, centrifugation and isolated by filtration.Now widely used liquid knockout mainly contains electric liquid knockout, silk screen liquid knockout, fiber liquid knockout, spiral board liquid knockout, folded plate type liquid knockout.
Electricity liquid knockout utilizes HVDC electric forming electric field, makes the flue gas that passes through produce ionization, causes electric charge on grit in flue gas and droplet band, move to precipitation level under the ordering about of electric field force, and gas cleaning is clean.Electricity liquid knockout has the advantage that efficiency is high, resistance is little and operating cost is low, but its equipment is complicated, construction requirement is high, the construction period is long, invests the highest.
Silk screen liquid knockout mainly by inertial collision except liquid, have structure simple, take up an area less, reduced investment, separative efficiency are high, resistance is little, quality is light and install the operating maintenance feature such as conveniently.But silk screen liquid knockout easily blocks when processing the flue gas containing dust granule by the gauze pad of weaving filaments, therefore this equipment is also not suitable for processing the large flue gas of dustiness.
Fiber liquid knockout is made up of the single or multiple liquid element that removes; And each element is a certain amount of fibrous by uniform filling between internal, external network cylinder, passed through by inner side containing fog body, droplet detention is on fiber, after drop increases, along the air-flow of blowing under gravity, discharging tube place can be collected to and flow out, thus reach the object of gas-liquid separation.Fiber liquid knockout except high, the structure of liquid rate is simple, handling ease, reduced investment, easy to operate, but equipment is comparatively large, pressure drop is larger.
Baffle plate type liquid knockout utilizes in the flue of flue gas by a baffling, and due to the effect of inertia of droplet, droplet and deflection plate collide and be attached to deflection plate on the surface, reach except liquid object.For this mechanical type except liquid, the trapping of drop is subject to the physical property of drop self as the impact of viscosity, speed, is also subject to the structural parameters of flap as the impact of flap angle, flap spacing simultaneously, under various factors, usually causes except liquid efficiency reduces.
Spiral board liquid knockout utilizes inner fixed blade to make flow rotation, thus be separated by water droplet under the influence of centrifugal force.Whirlwind board separator pressure drop is little, and except liquid is effective, and structure is simple, handling ease, and the waste gas be especially applicable to solid or band salinity in those smog removes liquid.
The pluses and minuses of relatively above several liquid knockout, we can find out: spiral board liquid knockout structure is simple, droop loss is little, cost is low, occupation of land is few, is very suitable for flue gas desulphurization system.The principle of spiral board liquid knockout is: gas-liquid mixture produces rotary motion through during swirl vane at a high speed, when liquid particles, when the active force that eddy flow field is subject to is greater than Stokes resistance, centrifugal sedimentation occurs, move to surrounding, fall on barrel, due to wall effect and Action of Gravity Field, separated liquid runs down barrel influent shunt cylinder reaches the object of gas-liquid separation.Affect spiral board liquid knockout except the principal element of liquid efficiency be the sinking speed of droplet, disengaging time and the time of staying.Only have the disengaging time when droplet to be less than gas just can reach separation object in the eddy flow field time of staying, the increasing length adding large cylinder adds the time of staying of fluid at eddy flow field, improve the efficiency except liquid, but along with the increase of axial distance, hoop speed reduces gradually, the detachment dynamic that drop is subject to is more and more less, and eddy flow effect just weakens; Secondly because liquid still contacts with gas, the gas of flowing can will gather the liquid crushing of wall region at any time, makes liquid return in gas; In addition due to the mobility of liquid, after liquid is agglomerated into larger volume along wall, Action of Gravity Field also can break surface tension naturally, even if form granule to return in gas. so prior art employs eddy flow scheme, because liquid cannot well be drawn at any time, cause the liquid fragmentation again under the effect of air-flow separated, become droplet, be again involved in flue gas.
We improve spiral board liquid knockout for this reason, become a kind of novel gas-liquid separator, have both kept the centrifugal effect in cylinder, the liquid separated can be drawn in time again, make it both have good in liquid effect, too much droop loss can be avoided again, and structure is simple, handling ease.
Goal of the invention:
The object of the present invention is to provide a kind of multi-stage agglomeration and eddy flow combination defogging method, coalescent and the centrifugation Combination Design by surface, reduce the liquid that gas carries, it is made both to have had good consuming except liquid effect reduces water, too much droop loss can be avoided again, and structure is simple, easy to manufacture.
Summary of the invention
The invention provides the defogging method of a kind of multi-stage agglomeration and eddy flow combination, comprise tower body, coalescent district, Multi-stage spiral is except liquid zone and aiutage, gas-liquid mixture from below removes liquid zone by coalescent district and Multi-stage spiral successively and carries out gas-liquid separation, first the gas of carrying of liquids enter coalescent district, droplet is caught on coalescing-plate, form coalescent liquid and flow under the influence of gravity into other districts below tower body, then gas enters the coaxial Multi-stage spiral device installing series connection and carries out gas-liquid separation further, the isolated liquid of cyclone at different levels is pooled to independently fluid zone after cyclone outlet at the corresponding levels, this fluid zone and gas barrier, and get rid of from the discharging tube being arranged on this isolated area, gas enters next stage cyclone successively and proceeds gas-liquid separation, liquid is drawn successively, qualified gas is arranged outward through aiutage.
Coalescent district of the present invention is located in tower body, outside Multi-stage spiral device or below.Coalescent district is made up of the barrier or dividing plate forming separation community air ventilation passage, and barrier or dividing plate can multilayer be installed up and down, and barrier or dividing plate adopt water wetted material.
Multi-stage spiral of the present invention removes liquid zone and comprises Multi-stage spiral device, connecting cylinder and aiutage.Multi-stage spiral device is arranged in around aiutage, organizes arrangement more, adopts parallel mode to carry out gas-liquid separation.Be connected with connecting cylinder below Multi-stage spiral device, connecting cylinder is connected with aiutage.Smoke inlet is arranged on the entrance of Multi-stage spiral device, exports as flue gas exhaust cylinder.
First order cyclone of the present invention is located at topmost, other are at different levels is arranged successively straight down, flue gas enters first order cyclone downwards in the top, after exclusive segment separating liquid, enter other downwards at different levels, other cyclones at different levels from top to bottom diameter reduce successively, and the guiding gutter of liquid pooling zone and discharging tube are located at outside next stage cyclone inlet, flue gas enters aiutage through interface channel, turns to 180 ° of backward upper eliminatings.
First order cyclone of the present invention can be located at foot, other are at different levels is arranged successively straight up, flue gas upwards enters first order cyclone in bottom, after exclusive segment separating liquid, upwards enter other at different levels, other cyclones at different levels from bottom to top diameter increase successively, and the guiding gutter of liquid pooling zone and discharging tube are located at outside previous stage cyclone outlet, and flue gas enters aiutage through interface channel and upwards gets rid of.
Described Multi-stage spiral device, is made up of some grades of cyclones, the upper and lower arranged in series of every one-level cyclone, and will have certain insertion height h and annular space thickness S when connecting, and inserts and highly has significant impact to except liquid efficiency.After gas-liquid mixture enters first order cyclone inlet, under centrifugal force and Action of Gravity Field, separate a part of liquid, then gas enters next stage cyclone, carries out next stage gas-liquid separation.Through Multi-stage spiral except liquid, improve except liquid efficiency.
Described cyclone is made up of cylindrical shell, eddy flow parts, liquid collection region.Gas-liquid mixture enters by above cyclone cylindrical shell, then flow direction is changed by eddy flow parts, the little water droplet carried in gas gets rid of to wall under the effect of centrifugal and gravity, coalescent and to dirty along wall, enter liquid pooling zone, collected by the guiding gutter of liquid pooling zone, discharged by discharging tube, gas is discharged by below cyclone cylindrical shell again.
Described cylindrical shell, cylindrical shell height L has certain scope, and fluid separation applications should be guaranteed to get off, and can ensure that again gas is in centrifugal effective district, prevents the coalescent liquid got off again broken under the effect of air-flow, causes reentrainment.
Described eddy flow parts, comprise swirl vane and blind plate district, blind plate district is positioned in the middle of swirl vane, is connected with each swirl vane.
Described swirl vane, have certain blade quantity N and enough width W to ensure that adjacent blades has certain lap, should improve separative efficiency, prevent the too much increase of pressure drop again.
Described blind plate district, is positioned in the middle of swirl vane, plays a part to connect blade and support blade, also plays liquid collecting and dispense liquid simultaneously.
Described liquid pooling zone, is positioned at the end of every one-level cyclone, is made up of liquid guide flow groove and discharging tube, for collecting, discharging the water droplet separated.
Described guiding gutter, is positioned at the end of every one-level cyclone cylindrical shell, is connected with discharging tube, and the range of tilt angles of guiding gutter is 0 ~ α.
Described connecting cylinder, inserting blast pipe has certain length H, has the effect of retaining ring and reduction turbulent flow, thus reduces the pressure loss of whole device.
Described aiutage, is positioned at equipment center, arranges a discharging tube below aiutage, for discharging the liquid fallen in aiutage, is flue gas discharge opening, for discharging the dry flue gas after gas-liquid separation above aiutage.
Multi-stage agglomeration eddy flow combination liquid removing method of the present invention compared with prior art, has following technical characterstic:
(1) adopt coalescent and eddy flow series multistage liquid removing method, improve except liquid rate.
(2) adopt porous or improve surface area hydrophily coalescence material, catching the droplet in gas in time and be condensed into large drop and be separated, improve except liquid efficiency.
(3) adopt Multi-stage spiral except liquid, in time the coalescent liquid got off is drawn, decrease the reentrainment of gas.Keep centrifugal effect in cylinder, improve except liquid efficiency.
(4) structure is simple, handling ease.
(5) pressure drop is little.
Accompanying drawing explanation
Fig. 1 is a kind of structural representation of the present invention.
Fig. 2 is a kind of top view in coalescent district in Fig. 1.
Fig. 3 is a kind of top view in coalescent district in Fig. 2.
Fig. 4 is a kind of structural representation that in Fig. 1, Multi-stage spiral removes liquid zone.
Fig. 5 is a kind of top view that in Fig. 3, Multi-stage spiral removes liquid zone.
Fig. 6 is a kind of structural representation of eddy flow parts in Fig. 3.
Fig. 7 is the structural representation of Multi-stage spiral device coupling part.
In figure: 1, coalescent district, 2, Multi-stage spiral device, 3, connecting cylinder, 4, aiutage, 5, tower body, 6, cyclone, 7, eddy flow parts, 8, liquid pooling zone, 9, cylindrical shell, 10, swirl vane, 11, blind plate district, 12, guiding gutter, 13, discharging tube, 14, dividing plate or barrier, 15, Multi-stage spiral is except liquid zone, 31, the gas entered, 32, the gas of discharging, 33 liquid, α, the angle that guiding gutter tilts, D, (first order is D1 to single-stage barrel diameter, the second level is D2, analogize with this), L, (first order is L1 to single-stage barrel lenght, the second level is L2, analogize with this), H, insert height (liquid pooling zone height), S, annular space thickness, d, aiutage diameter, in figure, arrow represents the flow direction of gas and liquid respectively.
Detailed description of the invention
In order to make those skilled in the art better understand technical scheme of the present invention, below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.
As shown in Figure 1, a kind of multi-stage agglomeration eddy flow combination liquid removing method, comprises tower body, coalescent district 1, Multi-stage spiral except liquid zone 15 and aiutage.Coalescent district 1 is arranged in tower body 5, and Multi-stage spiral is except liquid zone 15 or below it.
As shown in Figure 2, coalescent district 1 is made up of the dividing plate of multistage staggered arrangement or barrier 14.
As shown in Figure 3, Multi-stage spiral comprises Multi-stage spiral device 2, connecting cylinder 3 except liquid zone 15.Multi-stage spiral device 2 is made up of multistage cyclone 6 of connecting up and down.Cyclone 6 comprises eddy flow parts 7, liquid pooling zone 8 and cylindrical shell 9.
As shown in Figure 4, many group Multi-stage spiral devices 2 are arranged in around aiutage 4, multiple arrangement, and Multi-stage spiral device 2 is connected with connecting cylinder 3, and connecting cylinder 3 is connected with aiutage 4, adopts parallel mode to carry out gas-liquid separation.
As shown in Figure 5, eddy flow parts 7 are made up of swirl vane 10 and blind plate district 11.
As shown in Figure 6, liquid pooling zone 8 is made up of guiding gutter 12 and discharging tube 13.
As shown in Figure 6, when upper level cyclone is connected with next stage cyclone, there are certain insertion height H and annular space thickness S.
Gas-liquid mixture removes liquid zone 15 by coalescent district 1 and Multi-stage spiral successively and carries out gas-liquid separation.First the gas of carrying of liquids enter coalescent district 1, and by droplet seizure, on coalescing-plate 14, also under gravity liquid being discharged coalescing-plate 14 isolates a part of liquid, and then gas enters Multi-stage spiral except carrying out gas-liquid separation further in liquid zone 15.Gas-liquid mixture removes in liquid zone 15 at Multi-stage spiral, entered by Multi-stage spiral device 2 entrance, through eddy flow parts 7, rotary motion is produced by swirl vane 10, under centrifugal force and Action of Gravity Field, the droplet carried in gas moves to surrounding, fall on barrel, along barrel influent pooling zone 8, collected by guiding gutter 12 and separate a part of liquid and discharge through discharging tube 13, gas enters next stage cyclone and carries out next stage gas-liquid separation, through Multi-stage spiral except the gas after liquid enters connecting cylinder 3, discharge from flue gas exhaust cylinder 4, the liquid fallen in aiutage is discharged through discharging tube 13.
Embodiment
Dewater for wet flue gas desulfurizer flue gas.Exhaust gas volumn 200,000 standard cube m/h, the moisture 97099kg/h of flue gas, tower body diameter 6000mm, coalescent district adopts barrier form, 150mm below Multi-stage spiral liquid knockout, channel size 30mm, height 1000mm, material is hydrophilic plastic, six groups of multistage cyclonic fluid separators of same size are set between aiutage and tower body, often organizing separator is three grades, diameter of the housing D1=800mm, height L1=1440mm, D2=680mm, L2=1224mm, D3=560mm, L3=1008mm, d=2750mm, H=420mm, α=0 °, S=60mm, every grade of swirl vane is 4, dehydrator overall presure drop 1085Pa, discharge flue gas water content almost nil.
Claims (10)
1. a multi-stage agglomeration eddy flow composition gas liquid removing method, comprise tower body, coalescent district, Multi-stage spiral is except liquid zone, aiutage, gas-liquid mixture from below in tower body removes liquid zone by coalescent district and the vertical Multi-stage spiral installed successively and carries out gas-liquid separation, first the gas of carrying of liquids enter coalescent district, droplet is caught on coalescing-plate, coalescent liquid under gravity sedimentation is separated from the gas, then gas enters the Multi-stage spiral device be coaxially installed in series and carries out gas-liquid separation further, the isolated liquid of cyclone at different levels is pooled to independently fluid zone at cyclone outlet at the corresponding levels, this fluid zone and the gas barrier entering next stage cyclone, and discharge from the discharging tube being arranged on this fluid zone, gas enters next stage cyclone successively and proceeds gas-liquid separation, liquid is drawn successively and is flowed into other districts below tower body, qualified gas enters aiutage from afterbody and arranges.
2. as claimed in claim 1, it is characterized in that, coalescent district is located in gas tower body, outside Multi-stage spiral device or below, and part covers or all covers the space between tower body and Multi-stage spiral device.
3. as claimed in claim 1 or 2, it is characterized in that, coalescent district is made up of the barrier or dividing plate forming separation community air ventilation passage, and barrier or dividing plate can multilayer be installed up and down, and barrier or dividing plate adopt water wetted material.
4. as claimed in claim 3, it is characterized in that, air ventilation passage in tower is separated into numerous trellis or bar shaped community circulation passage by barrier or dividing plate.
5. as claimed in claim 1, it is characterized in that, Multi-stage spiral removes liquid zone and comprises Multi-stage spiral device, multistage liquid pooling zone, gas connecting cylinder, cyclone at different levels is by housing, eddy flow parts, liquid pooling zone, gas access and outlet composition, cyclone at different levels is vertically arranged up and down, upper level cyclone gas vent is different with next stage cyclone gas access diameter, swirl vane is provided with in cyclone at different levels, cyclone outlet at different levels is connected with next stage cyclone inlet, upper level cyclone housing outlets is different with next stage cyclone housing entrance height, independently enclosed liquid pooling zone is formed between this difference in height and diameter difference, this pooling zone arranges liquid guide flow groove and discharging tube.
6. as claimed in claim 5, it is characterized in that, Multi-stage spiral device first order cyclone is located at topmost, and other are at different levels is arranged successively straight down, and flue gas enters first order cyclone downwards in the top, after discharge section separating liquid, enter other downwards at different levels, other cyclones at different levels from top to bottom diameter reduce successively, and the guiding gutter of liquid pooling zone and discharging tube are located at outside next stage cyclone inlet, flue gas enters aiutage through interface channel, turns to 180 ° of backward upper discharges.
7. as claimed in claim 5, it is characterized in that, Multi-stage spiral device first order cyclone is located at foot, other are at different levels is arranged successively straight up, and flue gas upwards enters first order cyclone in bottom, after exclusive segment separating liquid, upwards enter other at different levels, other cyclones at different levels from bottom to top diameter increase successively, and the guiding gutter of liquid pooling zone and discharging tube are located at outside previous stage cyclone outlet, and flue gas enters aiutage through interface channel and upwards gets rid of.
8. as described in claim 1 or 5, it is characterized in that, be set up in parallel many group Multi-stage spiral liquid knockouts, share an aiutage, aiutage is arranged in the center of each group of Multi-stage spiral liquid knockout.
9. as described in claim 5 or 6 or 7, it is characterized in that, bottom cyclone separator liquid pooling zone at different levels, guiding gutter is designed to the angle of inclination of α.
10. as described in claim 1 or 6, it is characterized in that, coalescing-plate surface and/or cyclone inwall arrange liquid coalescence material, and this material is porous or the hydrophilic material increasing surface area.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108371846A (en) * | 2018-03-30 | 2018-08-07 | 张维国 | Gas-liquid separation device |
| CN109499190A (en) * | 2018-09-28 | 2019-03-22 | 长沙吉天环保科技有限公司 | It is a kind of just to imitate preprocessor |
| CN110358595A (en) * | 2019-07-30 | 2019-10-22 | 四川长仪油气集输设备股份有限公司 | A kind of high-efficiency multi-stage whirlwind, which adds, catches mist separator |
| CN110841378A (en) * | 2019-12-16 | 2020-02-28 | 华中科技大学 | Rectifying device for improving physical agglomeration effect |
| CN111714967A (en) * | 2020-06-16 | 2020-09-29 | 上海建工四建集团有限公司 | Gravity type precipitation device and method |
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| CN111714967B (en) * | 2020-06-16 | 2022-06-21 | 上海建工四建集团有限公司 | Gravity type precipitation device and method |
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Application publication date: 20150930 |