CN101059313A - Reverse dust collector with eddy plate - Google Patents
Reverse dust collector with eddy plate Download PDFInfo
- Publication number
- CN101059313A CN101059313A CNA2006101625265A CN200610162526A CN101059313A CN 101059313 A CN101059313 A CN 101059313A CN A2006101625265 A CNA2006101625265 A CN A2006101625265A CN 200610162526 A CN200610162526 A CN 200610162526A CN 101059313 A CN101059313 A CN 101059313A
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- baffle plate
- dust
- flow
- upstream side
- dust arrester
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
- Y02P40/121—Energy efficiency measures, e.g. improving or optimising the production methods
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
Abstract
The invention provides a reverse rotation dedusting device, comprising a main unit. The main unit is a rectangle box. An ash hopper is arranged on the lower part of the main unit and comprises four inclined surfaces. The upper space of the main unit is divided into an air inlet chamber and a separation chamber through a baffle plate. The lower space of the main unit is provided with a plurality of vertical baffles basically along an inclined surface of the ash hoppers; a gas flow route is formed between all baffle plates and the inclined surfaces, in convenient for wide upstream side and a narrow downstream side. The baffle plate on the upstream side is long in the vertical direction; furthermore, the interval between all baffle plates has narrow upstream side and wide downstream side. The airflow in the gas flow route ascends along the baffle plate and is rectified on the upstream side through the baffle plate; the baffle plate is long in the vertical direction, so as to lead the airflow to be basically a lamellar flow and to flow into the separation chamber. The flowing speed of the airflow is restricted by flow resistance between the baffle plates, thus leading the flowing speed to be more uniform.
Description
Technical field
The present invention relates to a kind of dust arrester, described dust arrester is used for removing the dust from the gas that the heat material cooler of the band WHRS in for example cement plant is discharged.
Although the present invention relates to be generally used for the dust arrester of the waste gas system in cement plant, the present invention is applicable to the waste gas system of other factory such as steel mill, and described waste gas system is equipped with the boiler that is used for reclaiming from the waste gas that wherein is mixed with hard dust used heat.
Background technology
The schematic diagram in cement plant is shown in Figure 1, and generally known.In the cement plant, the research and the propagation of heat recovery technology have been promoted for the conservation of energy.Its example is shown in Figure 1.
In cement plant shown in Figure 1, the used heat of the gas that discharges from preheater is to reclaim by a PH (preheater) boiler, and the used heat of the gas that discharges from air quenched cooler (AQC) Q such as clinker cooler is collected by AQC boiler B.
In addition, in the downstream of AQC boiler B dust-precipitator (dust-precipitator is used for air conservation) and exhaust blower F are installed, and waste gas passes through exhaust blower F from smoke stack emission.
Therebetween, if the waste gas that comes out from air quenched cooler (AQC) Q wherein a part be supplied to interim stove as combustion air, and remaining waste gas is fed to AQC boiler B, for example, have under the cement plant situation that grog production capacity is 3200t/d, the waste gas flow velocity that then is fed to AQC boiler B is about 110 * 10
3Nm
3/ h, and the exhaust capacity of the exhaust blower F on the downstream of AQC boiler B is 240 * 10
3Nm
3/ h, and power consumption is about 500kw.
Therebetween; the waste gas of discharging from air quenched cooler Q contains a large amount of hardening oxidation calcium (CaO) dust, and it is serious to wear away and damage AQC boiler B, therefore; dust arrester C must be installed in the upstream side of air quenched cooler Q, so that protect described air quenched cooler Q.
Generally, when dust arrester C is installed, because the pressure loss of the dust arrester that relates to is big, so must increase the exhaust capacity of exhaust blower F.Therefore, can not avoid increasing equipment cost and increase exhaust blower power consumption.By the way, have under the situation that grog production capacity is 3200t/d in the cement plant, the year power consumption of exhaust blower F is about 3,700,000kwh/y or more.When the power consumption of exhaust blower F owing to deduster C being installed having increased, the energy recovering effect of AQC boiler B reduces.
Therefore, when on the upstream side of AQC boiler B, dust arrester C being installed, must avoid increasing the exhaust capacity of exhaust blower F.So, must reduce the pressure loss as much as possible by the caused waste gas of dust arrester C.
Therebetween, the pressure P that is applied on exhaust blower (the comprising blower fan) F represents with V * Δ p, and when exhaust boiler B not being installed and when exhaust boiler and dust-precipitator were installed, blower pressure was as following represented.
1) the blower pressure p1 when exhaust boiler B is not installed
P1=V1 * Δ p1............ formula (1)
＝[100?000×(270+273)/273]×200
＝3.98×10
7
Herein: gas temperature: 270 ℃
Pressure loss Δ p1:200mm water column (pressure loss of EP) (EP: electrostatic precipitator) and
Gas flow: 100 000Nm
3/ h
(in addition, the V1 that provides in the formula (1) represents the real gas amount).
2) the blower pressure p2 when boiler and dust-precipitator are installed
P2=V2 * Δ p2............ formula (2)
＝[100?000×(80+273)/273]×(200+100)
＝3.88×10
7
Herein; Gas temperature: 80 ℃, temperature descends by boiler,
Pressure loss Δ p2:200mm water column (pressure loss of EP)+100mm water column (boiler, the pressure loss of dust-precipitator) and
Gas flow: 100 000Nm
3/ h
(in addition, the V2 that provides in the formula (2) represents the real gas amount).
3) because p1 ≈ p2, so, but when the increase of the pressure loss being suppressed to about 100mm water column, the load of blower fan F will not changed even boiler and dust-precipitator are installed.
On the other hand, the dust-precipitator as effective dedusting from the waste gas of different factories has the cyclone dust collectors system, electric dust removing system (JP 8-155335A) and impingement plate system (JP11-132429A).Cyclone dust collectors system and impingement plate system have the pressure loss of big waste gas stream.In addition, although electric dust removing system has the little pressure loss, because dust is charged, so it is not suitable as on the upstream side that dust-precipitator is installed in boiler.
On the other hand, for the above-mentioned dust arrester C that is used to protect AQC boiler B, require the high dedusting degree of accuracy and high efficiency of dust collection.Yet, for the attainment of one's purpose, must be increased in the dedusting degree of accuracy under different-grain diameter (for example, 0.3mm or the bigger) situation, the dust of above-mentioned different-grain diameter makes the boiler abrasion and damages.On the other hand, (for example, less than 0.3mm) dust is removed and when having only fine dust to keep fully, and fine dust adheres to and is layered on the heat exchange surface of boiler and proceeds significantly, finds that therefore heat exchanger effectiveness early descends when medium particle diameter.
As mentioned above, be to reduce the pressure loss as much as possible to the requirement of above-mentioned dust arrester, and pin-point accuracy ground is only removed and is had predetermined particle diameter or bigger dust.
Patent documentation 1:JP 8-155335A
Patent documentation 2:JP 11-132429A
Summary of the invention
Therefore, the present invention plans, in WHRS with dust arrester C, described dust arrester C is installed on the upstream side of AQC boiler B, be used for reclaiming the used heat of the gas that the air quenched cooler Q as the clinker cooler in cement plant discharges, so that create a kind of be used for suppressing as much as possible the dust arrester of the pressure loss that produced by dust arrester C and only really high accuracy remove and have predetermined particle diameter or bigger dust.
Major technique thought of the present invention is:
On the upstream side of heat recovery boiler, be equipped with in the WHRS of dust pelletizing system C, the rate of climb of waste gas is adjusted to the sinking speed that is lower than predetermined particle diameter or bigger dust, therefore make dust settling with to be separated and remove, and
By a plurality of vertical baffles in the dust arrester, (for example make at the glide path section in the precalculated position of dust arrester, cross section A-A shown in Fig. 3 (a)) waste gas of locating rises to flow and becomes laminar flow basically, and it is even that upwelling becomes basically, thereby suppress the pressure loss as much as possible, and only remove to high accuracy and have predetermined particle diameter or bigger dust.
The present invention is described for realizing being constructed as follows of above-mentioned technological thought.
Being used for the formant that dust arrester gathers dust is square box, and on the bottom of formant, an ash bucket is arranged, and described ash bucket comprises 4 inclined-planes.The upper space of formant is divided into inlet plenum and separation chamber by a dividing plate.In the lower room of formant, with one of them inclined-plane of ash bucket, some vertical baffles are installed basically.Gas flow route between the inclined-plane of each baffle plate and ash bucket so forms, so that wide and narrow in the downstream at upstream side.
Baffle plate on the vertical baffle middle and upper reaches side is long in vertical direction, and between each baffle plate is narrow on the upstream side and wide on the downstream at interval.
Air-flow along the gas flow path flows moves up along baffle plate, and on the upstream side by vertical direction on long baffle plate rectification so that air-flow becomes laminar flow basically and flows into the separation chamber.
Flowing velocity is limited by the flow resistance at the interval between each baffle plate, and flow velocity is become evenly.
[operation]
From the upper end of inlet plenum, add the waste gas of clinker cooler, and flow in the inlet plenum downwards.And waste gas flows downward in the formed glide path between the inclined-plane by a plurality of baffle plates and ash bucket.And the air-flow that flows downward between the inclined-plane of each baffle plate and ash bucket upwards turns to (putting upside down) at the lower end of each baffle plate, so that upwards flow through the interval between each baffle plate.
Although flow downward in the glide path of waste gas between the inclined-plane of each baffle plate and ash bucket, a part of waste gas flows into the separation chamber by the interval between each baffle plate on the road.Thereby the waste gas stream energy in glide path is (on upstream side) grow in position upwards, and in upper/lower positions (on the downstream) die down.Therefore, if the interval between each baffle plate is identical, then at interval and the gas that is blown into separation chamber energy grow and in upper/lower positions, dying down in the position that makes progress by each.
Yet by using this means, the interval above each between the baffle plate is narrow, and the interval between the baffle plate is wide below each, therefore owing to the flow resistance that produces at interval is upwards little greatly and downwards.And, air-flow between up and down energy difference and the flow resistance difference balance in the interval between each baffle plate.The result, it almost is uniform making the flowing velocity of passing the air-flow that upwards blows at the interval between each baffle plate, and the flowing velocity of the uprising gas that the glide path section (for example, the cross section A-A shown in Fig. 3 (a)) at each place, separation point position above the baffle plate blows changes seldom.
On upstream side, flowed energy is strong, and by the baffle plate on the upstream side, and air-flow turns very big curved and be blown in the separation chamber.Therefore, turn round by the baffle plate on the upstream side and be blown into air-flow in the separation chamber and in the separation chamber, produce end stream.Yet in dust arrester of the present invention, the baffle plate on upstream side is long in vertical direction and it is narrow at interval, so that air communication is crossed the baffle plate rectification, and suppresses air-flow disturbance in the separation chamber.Therefore, the sedimentation of dust is not subjected to the obstruction of flow perturbation in the separation chamber.
On the other hand, the particle size of sedimentation depends on the rate of climb of locating waste gas at the glide path section (cross section A-A as shown in Fig. 3 (a)) at place, separation point position in the separation chamber, and the rate of climb in the separation chamber almost is uniform at the section place of gas flow route.Therefore, even the rate of climb is increased to the limit flowing velocity of the dust settling of predetermined diameter, also remove than the dust that predetermined diameter is big pin-point accuracy.Therefore, the flowing velocity of waste gas in dust arrester increases, and suppressed as much as possible by the caused pressure loss of dust arrester, can make the pressure loss littler like this.
On the other hand, the magnitude of load of exhaust blower that is used for discharging the waste gas of the heat recovery boiler by clinker cooler waste gas is directly proportional with the flowing velocity and the pressure loss of waste gas.Be equal to when the increase that increases the exhaust load that causes owing to the pressure loss that dust arrester produced owing to make the flow velocity of waste gas reduce the minimizing of the exhaust load that (volume reduces because temperature descends) cause, so because the in fact vanishing of increase of the exhaust blower load that installation heat recovery boiler and dust arrester cause by heat recovery boiler.The pressure loss of dust arrester of the present invention is little, and in fact is suppressed at heat recovery boiler and in the scope that the discharging load that causes reduces.Therefore, the discharge capacity of exhaust blower can be equal to the discharge capacity when heat recovery boiler is not installed.
In addition, Yu Ding dust size is the particle diameter that is used for promoting the heat transfer pipe abrasion of AQC boiler (heat recovery boiler).Be used for promoting that significantly the particle diameter of abrasion is 0.3mm or bigger, pass through the flowing velocity of AQC boiler, depend at the ordinary cement factory and adopt the AQC boiler but above-mentioned particle diameter depends on waste gas.
That is to say that waste gas stream almost is 15m/s by the flowing velocity of the heat recovery boiler of waste gas in the clinker cooler in the cement plant.Under this exhaust-gas flow speed, particle diameter is the heat transfer pipe that 0.3mm or bigger dust wore away and damaged boiler significantly, and when particle diameter during less than 0.3mm, the abrasion of heat transfer pipe and damage few.On the other hand, when in waste gas, containing particle diameter less than the dust of 0.3mm by the AQC boiler, suppressed that fine dust adheres to and the heat exchange surface of the boiler that is added on, therefore confirm, suppressed the decline of the heat exchange performance of boiler.Can infer that when adopting the above-mentioned gas flow velocity, particle diameter has little inertia force less than the dust of 0.3mm, so it is carried along heat transfer pipe periphery flow air stream.Like this, prevent that dust from colliding with the surface of strong impact force and heat transfer pipe, and the surface of cutting heat transfer pipe.On the other hand, particle diameter is always removed the fine dust that adheres on the heat exchange surface less than the dust of 0.3mm, adheres to and is superimposed upon on the heat exchange surface to prevent fine dust.
As mentioned above, the present invention has suppressed the increase of the waste gas resistance (pressure loss of waste gas) that causes owing to dust arrester as much as possible, basically the load of having eliminated exhaust blower increases, suppress the abrasion that cause owing to the dust in the waste gas and damaged the AQC boiler, therefore improved the useful life of boiler, and suppressed decline owing to the heat exchange performance that adheres to the AQC boiler that dust causes, therefore can reduce the maintenance cost of AQC boiler.
Description of drawings
Above-mentioned and other purpose of the present invention, characteristics and the explanation of advantage from being done with reference to the accompanying drawings, it is more apparent to become.
Fig. 1 is the schematic diagram of ordinary cement factory WHRS.
Fig. 2 is according to the thimble-tube boiler of embodiment of the present invention and the side view of dust arrester.
Fig. 3 (a) is the vertical sectional view of embodiment, and Fig. 3 (b) is the sectional view of described embodiment, and Fig. 3 (c) is the cutaway view of line segment A-A shown in Fig. 3 (a).
Fig. 4 is the cutaway view by vector representation, the flowing velocity distribution of waste gas stream in the formant of dust arrester is shown simultaneously, if remove baffle plate from the dust arrester of embodiment.
Fig. 5 is the cutaway view by vector representation, and the flowing velocity distribution of waste gas stream in the formant of the dust arrester of embodiment is shown simultaneously.
The specific embodiment
Below, embodiments of the invention are described with reference to the accompanying drawings.
This embodiment is a system, and described system is that the waste gas under the higher temperature of will discharge from the intergrade as the air quenched cooler Q of clinker cooler is handled by dust arrester (dust-precipitator) C, so that dedusting, as shown in Figure 2.Then, waste gas is fed to AQC boiler B, turns back to discharge duct again, discharge by exhaust blower F, and from smoke stack emission.
From the intergrade of air quenched cooler (AQC) Q discharge and be fed to AQC boiler B waste gas (about 360 ℃ down and flow velocity be 1800Nm
3/ min) comprise that a large amount of dust, described dust have the diameter of various different sizes, be 1.0mm or littler as particle diameter.The waste gas flow velocity is about 1800Nm
3/ min, and on the downstream of AQC boiler B, discharge by the flow velocity of exhaust blower with 15m/s.
As shown in Figure 3, the formant H of the dust arrester C of this embodiment is the casing of the one-tenth flat shape of rectangle, and an air flow inlet i is installed on half on the left side of the top board of casing and an air stream outlet o is installed on its right side on half.The top of formant H is divided into inlet plenum 2 and separation chamber 3 by a dividing plate 1, and aforementioned barriers 1 comprises skew wall 1a and vertical wall 1b.On the bottom of formant H, that is, an ash bucket 4 is installed at the lower position place that is lower than dividing plate 1 lower end.Ash bucket 4 comprises 4 inclined-planes, and a pair of inclined- plane 4a and 4a and a pair of inclined- plane 4b and 4b with wide width with narrow width wherein arranged.
From the position, lower right of vertical wall 1b, almost be an inclined-plane 4a along ash bucket 4, some baffle plates are installed above this inclined-plane 4.Baffle plate comprise many vertical baffle plates (from top to bottom, be 5a, 5b, 5c---5n), and between an inclined-plane 4a and above-mentioned each baffle plate of ash bucket 4, forms glide path 6.Glide path 6 flows along the downward exhaust gas routing of inclined-plane 4a in inlet plenum 2.It is to comprise the i.e. glide path that phases down of inclined-plane 4a and two inclined- plane 4b and 4b in 3 inclined-planes.At the front end place of glide path 6, can guarantee required air velocity in addition.
In addition, each baffle plate 5a-5n extends between the relative inwall of formant H.And the upper end of the lower end of vertical wall 1b and uppermost baffle plate 5a almost is under sustained height, and between them, forms a rise interval 7a.Equally, the lower end of the upper end of next baffle plate 5b and baffle plate 5a almost is under sustained height, and between forms an interval 7b.After this manner, baffle plate 5a-5n is under the situation of vertically not separating mutually, successively, and vertical and installation continuously.
Suppose that a kind of situation is that baffle plate is not installed, then the stream of a part of waste gas in the inlet plenum 2 circles round mobile (upset) and flows into separation chamber 3 at the lower end of vertical wall 1b.Remaining waste gas changes its direction that flows to separation chamber 3 lentamente by the center that flows to 3 bottoms, separation chamber.Then, waste gas flows into separation chamber 3, and moves up in separation chamber 3.At this moment, the flowing velocity distribution of waste gas in the separation chamber as shown in Figure 4.Near the strong turbulent flow of generation one vertical wall 1b.Flowing velocity in the separation chamber 3 central part office the highest, and near the flowing velocity the inwall of formant H on the opposite side of vertical wall 1b is minimum, the two speed difference is very remarkable.Like this, large diameter dust is blown afloat by the high velocity air of near turbulent flow the adjacent vertical wall 1b and central part office.When peak flow rate (PFR) is reduced to limit velocity (for example, the limit gas flow rate when predetermined particle diameter is the dust settling of 0.3mm) or when lower, above-mentioned turbulent flow dies down, therefore separate certainly and remove to have predetermined diameter or bigger dust.Yet, must amplify the sectional area of the glide path of separation chamber 3 greatly, and make separation chamber's vertical direction bigger.Like this, formant H is made bigger, and in the low part of flowing velocity, also remove and have medium particle diameter or littler dust.
The situation that baffle plate is not installed as mentioned above.Yet baffle plate 5a-5n of the present invention has suppressed near the turbulent flow vertical wall 1b, and to make separation point position (cross section A-A shown in Fig. 3 (a)) locate the rate of climb almost be uniform under the limit flowing velocity with predetermined diameter or bigger dust settling.Be used for the sort of occasion baffle plate be formed in following set forth in detail.
Topmost the upper end of the lower end of baffle plate 5a and next baffle plate 5b almost is in sustained height and forms rise interval 7b similarly.And topmost the length 8a of baffle plate 5a is the longest, and the length 8n of nethermost baffle plate is the shortest.And aspect the rise interval between each baffle plate, uppermost rise interval 7a is minimum, and nethermost rise interval 7n is maximum.As shown in Fig. 3 (c), each rise interval linear array and being parallel to each other, and broaden gradually to interval 7n direction from interval 7a.
The optimum value of the waste gas rate of climb that (in the cross section A-A shown in Fig. 3 (a)) located in above-mentioned separation point position and the superfluous difference of flowing velocity distribution change with each dust arrester is different, and the formation that not only depends on baffle plate, but also depend on the flowing velocity of waste gas, the temperature of waste gas, the formant structure of dust arrester and the inclination angle of ash bucket.Suppose their disposal abilities according to each dust arrester, the above-mentioned turbulent flow of essential inhibition, and make the speed of rising almost even.Essential controllable register 5a-5n, the vertical length 8a-8n of baffle plate, and the arrangement of the width 7a-7n of rise interval.The example of described arrangement is as described below.
When the flow velocity of waste gas is 110 * 10
3Nm
3During/h, this embodiment rate of climb that (cross section A-A shown in Fig. 3 (a)) located in the separation point position is at center average out to 3m/s, and hour is 1m/s near the wall surface of formant H.
It is 0.3mm or bigger dust (calcium oxide (CaO)) that this dust arrester is intended to only remove particle diameter.Yet the particle diameter of actual dedusting distributes and is, for example, to 0.3mm or bigger particle diameter, content is 40%, and to the particle diameter between 0.3mm and the 0.2mm, content is 20%, and to the particle diameter less than 0.2mm, content is 40%.Included particle diameter is that 0.3mm or bigger dust residual quantity are intimate 5% in the waste gas of air stream outlet o.Particle diameter is that 0.3mm or bigger dust dust removal efficiency are 87% or higher.
Although the present invention has been described in a preferred embodiment, to a certain extent, it is possible wherein specifically and significantly carrying out many changes and change.Therefore, should be appreciated that under situation about not departing from the scope of the present invention with spirit, the present invention can implement with specifying other different methods with the present invention.
Claims (4)
1. a WHRS comprises dust arrester, and described dust arrester is installed in the upstream side of heat recovery boiler,
Wherein the rate of climb of waste gas in the dust arrester is transferred to the sinking speed of the dust that is lower than predetermined particle diameter, make to have predetermined particle diameter or bigger dust settling so that separate and remove, and
A plurality of vertical baffle plates wherein are installed in dust arrester, so that be laminar flow basically at the air-flow of the rising of the pre-position of dust arrester glide path segmentation place, and the rate of climb of ascending air is uniformly in glide path segmentation place basically, thereby has only predetermined particle diameter or bigger dust very accurately to remove.
2. a reverse dust collector comprises a formant and an a plurality of vertical baffle that is installed in formant that is used for collecting dust,
Wherein formant is a square box, and an ash bucket is arranged on the bottom of formant, described ash bucket comprises 4 inclined-planes, and the upper space of formant is divided into inlet plenum and separation chamber by a dividing plate, and in the lower room of formant, along one of them inclined-plane of ash bucket some vertical baffle plates are installed basically, and between the inclined-plane of each baffle plate and ash bucket, are formed a gas flow route, so that wide on the upstream side and narrow on the downstream
Wherein in each baffle plate, long on the baffle plate vertical direction on the upstream side, and the interval between each baffle plate is narrow on the upstream side and wide on the downstream,
Wherein the air-flow in the gas flow route rises along baffle plate, and passes through the baffle plate rectification on upstream side, and above-mentioned baffle plate is long in vertical direction, so that air-flow becomes laminar flow basically, and flows in the separation chamber, and
Wherein the flow resistance by the interval between the baffle plate limits the flowing velocity of air-flow so that flowing velocity is even.
3. according to the described reverse dust collector of claim 2, wherein the rate of climb of waste gas in the separation chamber is that 0.3mm or bigger dust settling speed are corresponding with having particle diameter.
4. WHRS that is used for the cement plant clinker cooler comprises: dust arrester as claimed in claim 3, above-mentioned dust arrester are installed on the upstream side of heat recovery boiler (AQC boiler) of clinker cooler.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2005339617A JP3807741B1 (en) | 2005-11-25 | 2005-11-25 | Reversing dust removing device with a large number of current plates |
| JP2005339617 | 2005-11-25 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101059313A true CN101059313A (en) | 2007-10-24 |
| CN100581638C CN100581638C (en) | 2010-01-20 |
Family
ID=36968149
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200610162526A Active CN100581638C (en) | 2005-11-25 | 2006-11-27 | Reverse dust collector with eddy plate |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JP3807741B1 (en) |
| CN (1) | CN100581638C (en) |
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| CN101732928B (en) * | 2009-12-31 | 2012-09-19 | 安徽海螺建材设计研究院 | Waste gas-dust separator for cement kiln head and waste gas-dust separation method thereof |
| CN103225959A (en) * | 2013-04-10 | 2013-07-31 | 中建材（合肥）粉体科技装备有限公司 | Air cooler |
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| JP4966290B2 (en) * | 2008-12-17 | 2012-07-04 | 本田技研工業株式会社 | Exhaust gas recirculation device for internal combustion engine |
| KR101225020B1 (en) * | 2010-12-02 | 2013-01-22 | 니혼 스핀들 세이조 가부시키가이샤 | Dust collector |
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| JP7441014B2 (en) | 2019-09-03 | 2024-02-29 | 日鉄テックスエンジ株式会社 | pre duster |
-
2005
- 2005-11-25 JP JP2005339617A patent/JP3807741B1/en active Active
-
2006
- 2006-11-27 CN CN200610162526A patent/CN100581638C/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101732928B (en) * | 2009-12-31 | 2012-09-19 | 安徽海螺建材设计研究院 | Waste gas-dust separator for cement kiln head and waste gas-dust separation method thereof |
| CN103225959A (en) * | 2013-04-10 | 2013-07-31 | 中建材（合肥）粉体科技装备有限公司 | Air cooler |
| TWI725529B (en) * | 2018-09-13 | 2021-04-21 | 日商日鐵技術股份有限公司 | Dry quenching equipment and dust removal method in dry quenching boiler |
| CN110623295A (en) * | 2019-09-27 | 2019-12-31 | 云南省烟草农业科学研究院 | Intensive high-efficient biomass energy bulk curer heating device of collection |
| CN110623294A (en) * | 2019-09-27 | 2019-12-31 | 云南省烟草农业科学研究院 | Integrated built-in heat supply device of biomass energy bulk curing barn |
| CN110623294B (en) * | 2019-09-27 | 2021-12-07 | 云南省烟草农业科学研究院 | Integrated built-in heat supply device of biomass energy bulk curing barn |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2007147119A (en) | 2007-06-14 |
| JP3807741B1 (en) | 2006-08-09 |
| CN100581638C (en) | 2010-01-20 |
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