CN85105962A - Adjustable cyclonic separator and using method thereof - Google Patents
Adjustable cyclonic separator and using method thereof Download PDFInfo
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- CN85105962A CN85105962A CN85105962.7A CN85105962A CN85105962A CN 85105962 A CN85105962 A CN 85105962A CN 85105962 A CN85105962 A CN 85105962A CN 85105962 A CN85105962 A CN 85105962A
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Abstract
The present invention relates to be used to change the pressure drop at the separator two ends of moving and the method and apparatus of non-interrupt run or not obvious reduction operational efficiency.Be loaded with than himself heavy suspended particles fluid, flow into the top that is generally the cylinder minor air cell, so particle is because radially outward with towards the moving downward and separated of bottom particle outlet, the fluid through purifying then flows to the top outlet along tangent line.When not interrupting separator inner fluid and particle flow,, increase or reduce the pressure drop at separator two ends by making vortex stabiliser toward or away from the motion of fluid issuing hole.
Description
The present invention relates to make fluid stream that the cyclone separator of vortex and centrifugation takes place.Particularly relate to the method and apparatus that does not in fact reduce the cyclone separator separative efficiency and change its two ends voltage drop value.By means of change in pressure drop, the cyclone separator swirl valve of also can doing to resistance to wear uses.
In common cyclone separator, the gas or the liquid of band suspended particles flow into from tangential inlet, and form a basicly stable vertical vortex.The solid of these suspensions or liquid particle are crossed vortex stabiliser downwards and outwards and are separated in radially moving.For enough outward turning and decline expulsion forces being provided for these particles, this vortex stabiliser must be arranged in the intrinsic turning point place of eddy current or below slightly.
The applicant recognizes first, and the vertical length of eddy current can onlinely be regulated in the cyclone separator, and need not stop in advance handling carry the particle fluid motion, also need not change the flow and the pressure of inlet fluid.The applicant also finds, when vortex stabiliser moves up and when making the eddy current contraction in length, its consequence mainly is that the pressure drop at cyclone separator two ends increases.This pressure drop increase has improved the back pressure of inlet fluid.Utilize this phenomenon to regulate or make its commutation, and only cause the separative efficiency of suspended particles that a little decline is arranged entering fluid.
Therefore, the present invention relates to the component of suspension is separated, and the method and apparatus that this fluid is controlled.The suspended particles different with its density are scattered here and there in this liquid.Therefore suspension enters from the top that is generally straight Cylinder chamber, because movably vortex stabiliser is installed in indoorly, forms eddy current above vortex stabiliser, and component the heaviest in the grain that suspends is then done radially outward and moved downward with respect to lighter component.Fluid after the heavier component dilution is by outside top, straight Cylinder chamber or near the outlet delivery chamber it, and the fluid that is rich in heavier component then flows out by bottom, straight Cylinder chamber or near the outlet it.As make the vertical separation device shift near or leave the top outlet of garden column compartment, thus make the pressure drop at these two ends, chamber increase or reduce, then can change by exporting the flow proportional of discharging fluid up and down.The realization of this adjustment process need only mobile vortex stabiliser, and need not change the flow that the garden column compartment is imported and exported fluid.
The present invention is applicable to any suspension that in fact processing can separate in cyclone separator.Suspended particles can be solid-state, liquid state or gaseous state, and the suspended particles fluid also can be gaseous state or liquid state, as long as the fluid that particle is scattered in wherein comprises not jljl phase, its density also is different from Particle Density.
Fig. 1 is the test loop schematic diagram that uses in the testing equipment of the present invention.
Fig. 2 is the concrete device vertical cut-away schematic view of of adjustable cyclonic separator of the present invention.
Comprise in the method and apparatus provided by the invention following new discovery and (or) characteristics: (1) can make the separating property optimization of cyclone separator by the removable vortex stabiliser of vertical adjusting. (2) also can do similar adjusting to the pressure drop that is installed in parallel one group of cyclone separator two ends on a house steward, each flow that passes through separator is equated, perhaps termination or minimizing are by the flow of a certain separator, (3) even without outlet valve, can close equally the discharge currents of cyclone separator, to stop flowing of fluid fully, (4) regulate movably vortex stabiliser, restructuring with the control drain separator divides by the Fluid Volume of enrichment or dilution, (5) cyclone separator of the present invention is particularly conducive to gas or the liquid circulation flow of controlling relatively enrichment or dilution solids, and above-mentioned particle is that a kind of abrasion particle and its proportion are greater than or less than them and are scattered in wherein gas or liquid.
Cyclone separator utilizes a kind of affined high-speed eddy centrifugal force, to separate the phase of different densities. The strength and stability of eddy current is being all in all aspect the separative efficiency of determining cyclone separator and the abrasion resistance. Because improving reliability, separating property and the abrasion resistance of cyclone separator is very important business goal, begun one's study to obtain to reduce the modified cyclone separator that weares and teares and raise the efficiency. Particularly research comprises the cyclone separator internal structure of swirl stabilization device. Employed " stabilisation " term refers to eddy current is remained on the center of cyclone and reduces the turbulent flow energy consumption.
Near under the environmental condition, carried out flow, speed, noise and the drop test of a large amount of cyclone separators.Above-mentioned great majority experiment is to be 0.5 meter with diameter to be with the cyclone separator model of tangential inlet to carry out that this model is that ratio is 31/100 the commercial cyclone separator lucite of second grade fluid Cracking catalyst (FCC) (PLAXIGLAS
) model.The ratio of preference pattern, so that under the same input speed of 25 meter per seconds, the Reynolds (Reynolds) of simulation real fluid Cracking catalyst (FCC) cyclone separator and Shi Tandun (Strouhal) number.This model has nothing in common with each other and tests under the condition installing or do not install vortex stabiliser and stabilizer structure.Roughness with the woven wire simulation wall of being close to 10 orders on the cyclone separator inwall, 0.11 cm thick.This model is the typical cyclone separator that is used for modern catalytic cracking unit, but its extra high device that is efficient.The characteristics of this cyclone separator be inlet with discharge area than big, the inlet tube diameter is little and cylindrical shell is very long.
Many variablees of basic cyclone separator have been tested, to measure the influence of charging hopper geometry, stabilizer geometry and inner wall roughness to eddy motion in the cyclone separator.All experiment all uses air (simulation hydrocarbon gas) to make the work fluid.Air is 1 standard meter by total flow
3300 kilowatts of of/second is of The air blast of three supplied with.Great majority experiments is to be about, 0.6 meter of, 117 kilobars, flow at pressure3Carry out under the condition of/second.The admission velocity that flow is suitable is 17 meter per seconds therewith.Under this flow, calculate (R by the outlet caliber
E2=ρ
gW
il
i/ μ) Reynolds number is similar to 2.8 * 10
5Under high like this Reynolds number, velocity distribution curve is irrelevant with flow basically, therefore allows actual flow to change slightly, and all measurement result all is greater than 0.5 meter at 110～130 kilobars, 16～19 ℃ and flow
3Obtain under the condition of/second.For the ease of comparing, velocity distribution curve is all proofreaied and correct by the inflow velocity of 17 meter per seconds.
Cyclone separator is characterised in that, the big radial pressure gradient of balance eddy current centrifugal force.Therefore at the eddy current center or the whirlpool core exist relative vacuum.This low pressure core is estimated on possibility " absorption " nigh any surface, thereby swirl stabilization is attached on this surface.
The swirl stabilization apparatus is installed, to prevent the unsteady motion of eddy current in the cyclone separator model.
On vortex stabiliser, can install a vertical pin or vortex finder additional, with the restriction eddy current horizontal precessional motion and make its centering.Have been found that in test diameter is the precession that 0.6 centimetre stabilizer pin is not enough to limit eddy current in the cyclone separator.When bigger pin was used for eddy current centering, vortex stabiliser was more effective.Through test, diameter is that 1.9 centimetres pin effect is better.
Test the swirl stabilization apparatus of some types, obtained Different Results.Usually find that flat board or garden disk-shaped structure are satisfied.The diameter of vortex stabiliser should be at least about 1 times of eddy current outlet diameter.Mainly select the maximum gauge of commercial model stability device according to the fluid treatment amount, and this diameter is only limited by the circular passage between the stabilizer that is provided garden week and the chamber wall, and this passage is greatly to allowing catalyst to flow downward and upwards passing through eluent gas simultaneously.
When the vortex stabiliser apparatus arrangement must export not farly from eddy current, when promptly being at least about 2～3 times of eddy current outlet diameter and locating, vortex finder is not most important for the performance of cyclone separator.Yet if vortex finder is positioned at big distance (5-8 times of eddy current outlet diameter), it is good being provided with a vortex finder with vortex stabiliser.Such vortex finder is preferably approximately greater than 1/3 of eddy current length.
According to the aerodynamic studies result, it seems that the swirl stabilization effect be more suitable for improving separative efficiency, and make the pressure loss and wearing and tearing reduce to minimum.Even increase maximum whirling speed widely, vortex stabiliser also makes the pressure drop of model cyclone separator two ends reduce 10-15%.This situation is extremely abnormal in cyclone separator, almost always increases the pressure loss because increase whirling speed.As if along with pressure drop is lowered, the swirl stabilization effect reduces the turbulent flow energy consumption in the cyclone separator.
Fig. 1 shows with lucite (PLAXIGLAS
) test loop of building.With air catalyst is input to lifter 10 bottoms of 4.3 meters of Φ 8 cm x, air then enters by the coaxial nozzle 11 of 0.04 meter of Φ.The pressure reduction at lifter two ends (△ P) 12 is measured and inaccuracy, is approximately 0.25 kilobar.The air mass flow of using in lifter 10 is 1.8～2.9 standard meters
3/ second.This is equivalent to the superficial velocity of 7.2～11.5 meter per seconds in the lifter.Use the spinner survey air mass flow.Catalyst flow in the lifter does not wait from 2-9 thousand Grams Per Minutes.Between catalyst storage tank 15 and lifter 10,, a pinch cock 13 control solid flows are set by being on 0.076 meter the standpipe 14 at diameter.By closing the pinch cock 16 between elution cyclone separator 17 and the catalyst storage tank 15 and measuring in the elution cyclonic separation body material level and advance the speed, measure catalyst flow.In this measures, close the air that leads to elution cyclone separator 17, and the hypothesis density of catalyst is 0.8 gram per centimeter
3
An elbow bend 18 and a reduced pipe 19 are arranged at the top of lifter 10, and this reduced pipe is that to be 0.152 meter wide be that 0.04 meter rectangle cyclone separator tangential inlet 31(area is 5.8 * 10 for 0.076 meter garden Guan Yugao with diameter
-4Rice
2) UNICOM.The gas flow rate at cyclone inlet place does not wait from 5.2～8.4 meter per seconds.
Gas in the elution cyclone separator 17 is 0.076 meter pipeline 20 discharges by diameter.Second level cyclone separator 21 captures from the catalyst in the effluent of elution cyclone separator top.Low mass filter 22 will enter atmosphere after the gas purification, and captures the catalyst that runs leakage from second level cyclone separator.
Catalyst in the elution cyclone separator 17 is discharged by standpipe 23.Pinch cock 16 is used to control the catalyst material level of elution cyclone separator 17 bottoms.Catalyst storage tank 15 below elution cyclone separator 17, having constituted one is that 0.076 meter standpipe 14 is to the groove that holds of lifter charging by diameter.
The detailed vertical cut-away schematic view of elution cyclone separator 17 shown in Figure 2.Vortex region 24 usefulness internal diameters (ID) are that 0.142 meter pipeline is made, in adorn a vortex finder 25 and vortex stabiliser 26, the position of this vortex stabiliser 26 is in a certain specified distance in the bottom of distance cleaned air outlet 20.It is that 0.142 meter pipeline is made that elution district 27 also uses internal diameter (ID).Cleaned air outlet 20 is that wall thickness is that 0.3 centimeter inner diameter is 0.076 meter a pipeline, and runs through vortex generating region 30 to vortex region 24 tops 7 English inch.Catalyst or separation component outlet 23 are that internal diameter is 0.076 meter a pipeline.Carry particle gas and enter vortex 30 by tangential inlet pipe 31.
Vortex stabiliser 26 diameters be 10.2 centimetres (for great majority tests), edge thick be 1.27 centimetres, the center is thick is 2.5 centimetres.Vortex finder 25 6.4 centimetres of length, 1.27 centimetres of base diameters, 0.635 centimetre of top diameter.
As seen, vortex stabiliser 26 is with a sleeve pipe 35 around conduit 36 from the concrete device shown in the figure.Sealing ring 37 is installed in case the fluid stopping body flows between pipeline 35 and 36.Can make vortex stabiliser 26 vertical moving by gear and rack gearing 38.Bearing 39 is supporting gearing shaft, and this axle is with packing ring 37 sealings, on the axle and have can be from the handle or the transmission mechanism 40 of cyclone separator external control.
Example
Such as in the test of many times of using the solids gaseous suspension to carry out in as the equipment of medium, show that pressure drop of cyclone separator two ends and eddy current are closely related to the relative position of top dilution particle fluid issuing.In the test of being done in a vortex diameter is 51 centimetres cyclone separator, eddy current length changes between 91 centimetres and 43 centimetres.The inlet pressure of particle suspension is 117 crust gauge pressures.In eddy current length is under 91 centimetres of conditions, from the ingate to the pressure drop of dilution particle fluid outlet opening be 21 the crust.And the pressure drop of being rich in the particle fluid issuing from entering the mouth to is 12 crust.When eddy current length is 43 centimetres, although the pressure drop of being rich in the particle fluid issuing from entering the mouth to still in 12 Palestine and Israels, and is increased to 72 crust from the pressure drop of the dilution particle fluid issuing that enters the mouth.In those tests, although do not include the undercurrent that is rich in the particle fluid among cyclone separator, shunting changes about 1 times.When being rich in the particle fluid and only flowing in cyclone separator, then this separator does not have fluid and discharges.With this understanding vortex stabiliser is moved to dilution particle fluid Way out, can improve the pressure drop of separator two ends and stop fully until fluid is flowed.In this case, cyclone separator is just moving as a valve.Comprise the place of the suspended particles of the valve seat that is easy to wear and tear at working fluid, use this equipment advantageous particularly.Test of many times to said system shows, even vortex stabiliser is not is not almost worn and torn to vortex stabiliser in cyclone separator quite near dilution particle fluid issuing yet.This is because outside rapidly the dishing out continuously of cyclonic action can cause the particle of wearing and tearing, therefore basically only along the vortex stabiliser surface or by the mobile fluid of dilution particle fluid outlet edge far away, does not in fact contain the particle that this meeting causes wearing and tearing.
In the coal gasification process, the most handy clean recirculated air dilute suspended particles that comprise unconverted coal that cooling produces and (or) gas of flying dust. This cyclone separator is particularly suitable as the valve that resistance to wears, and is used for controlling above-mentioned gasification. Under general high temperature in the coal gasification requirement, the high pressure, most valves will certainly be by the suspended solid heavy corrosion. When using this cyclone separator, can make and carry solid reaction product and flow along tangent line, so the impurity solid resemble they in common cyclone separator to inner rotary. But, when using native system, moving vortex stabiliser by simple vertical, the recycle gas that can control relative clean flows through the top outlet, and cyclone separator is used as swirl valve, makes simultaneously the impurity solid downwards and discharges with being rich in the particle air-flow.
Making the place that is suspended in a large amount of solids separation in a large amount of gases, for example usually in catalytic cracking and various other production technology. Each separator receive a part from house steward carry efflux of solids and separating solids enter in the situation of public charging hopper one group of cyclone separator of parallel running usually. For example, usually see 8 cyclone separators and link to each other according to house steward by one, to receive the carried catalyst waste gas from regenerator. This in service, be difficult to each cyclone separator equivalent charging, from the solid that some cyclone separators captures, often flow through charging hopper and flow back in the waste gas by other cyclone separator. Yet when using this cyclone separator, interrupt run can not regulated vortex stabiliser yet, so that the shunting between the control parallel running separator.
In general, when separating being scattered in solid-state, liquid state in gaseous state or the fluid liquid or vapour particles, the present invention is that effectively the density of above-mentioned fluid is different from the density of particle. The present invention can be used for the control dilution or be rich in the undercurrent of particle fluid and the shunting between the overflow. Comprise in the chamber below the separator minor air cell that particularly the place of undercurrent by changing the pressure drop at cyclone separator two ends, can be used for the flow that control contains abrasion particle fluid with the present invention as valve, or keeping away The mode of exempting from any actual wear corrosion stops it and flows.
Claims (10)
1, be scattered in particle suspension separation method in the fluid different, it is characterized in that with particle density:
Above-mentioned flow of suspension flows into the minor air cell that is generally straight Cylinder of cyclone separator, and this minor air cell comprises fluid issuing hole, upper and lower part and vortex stabiliser movably, so enters fluid locate to form eddy current above vortex stabiliser;
Made component heavier in the suspension radially outwards and move downward by the effect of centrifugal force and gravity, thereby the fluid that is rich in heavier component is discharged from lower part outlet, heavier component dilution fluid is then discharged from the top outlet simultaneously;
By making the motion of vortex stabiliser, change the pressure drop at cyclone separator two ends or change above-mentioned pressure drop simultaneously and the fluid ratio by the upper and lower part flow respectively toward or away from the upper flow outlet.
2, cyclone separator is characterized in that, it comprises:
The straight Cylinder chamber that holds eddy current;
Can make comprise jljl not mutually and the fluid of the discontinuous and dispersed component of density flow into the device of above-mentioned minor air cell along tangent line, make and enter the eddy current that component heavier in the fluid is radially outwards thrown and moved downward with respect to lighter component to form one;
Be located at the heavier component dilution fluid outlet device of top, above-mentioned minor air cell or its vicinity;
Be installed on the removable swirl stabilization apparatus among the above-mentioned minor air cell, above-mentioned eddy current can be stablized in its installation site;
The device that can handle from outside, above-mentioned minor air cell, this device are used to make above-mentioned swirl stabilization device to move toward or away from above-mentioned topmost fluid issuing device.
3, the cyclone separator method of operating of a sets in parallel operation, each in this group cyclone separator is all accepted a part of suspended particles fluid, and the density of this fluid is different with contained suspended particles density, and this method of operating is characterised in that:
In the cyclone separator group of above-mentioned parallel running, be connected with at least one such as claim 2 the sort of cyclone separator of definition,
And in the cyclone separator of at least one above-mentioned parallel running, make at least one movably vortex stabiliser move to a certain position, thereby make fluid flow, be substantially equal to the rate of discharge of another above-mentioned multiple cyclone in parallel at least by at least one outlet of above-mentioned each multiple cyclone in parallel.
4, for making the method for the defined typical cyclone separator optimized performance of claim 2, it is characterized in that, move above-mentioned swirl stabilization device extremely from a certain position of topmost fluid outlet, so that under the essentially identical condition of the pressure that enters fluid, enter in the fluid isolated suspended particles more than the swirl stabilization device when another diverse location from the same suspended ion of separating the fluid that enters.
5, as the desired method of claim 1, it is characterized in that, when making fluid move through pressure that cyclone separator provides obviously not increase, shift near fluid issuing, stop fluid basically by the top outlet by making vortex stabiliser.
6, as the desired method of claim 5, it is characterized in that, enter fluid and contain the suspended particles gas that produces in the coal gasification process.
As the desired method of claim 1, it is characterized in that 7, entering fluid is the solids gaseous suspensions.
As the desired method of claim 1, it is characterized in that 8, entering fluid is the drop liquid suspension light than suspended particles.
As the desired method of claim 1, it is characterized in that 9, entering fluid is the drop gaseous suspension heavier than gas.
As the desired method of claim 1, it is characterized in that 10, entering fluid is the solids liquid suspension heavier than liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85105962.7A CN1005463B (en) | 1985-08-06 | 1985-08-06 | Adjustable cyclonic separator and its use method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85105962.7A CN1005463B (en) | 1985-08-06 | 1985-08-06 | Adjustable cyclonic separator and its use method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85105962A true CN85105962A (en) | 1987-02-25 |
| CN1005463B CN1005463B (en) | 1989-10-18 |
Family
ID=4794799
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85105962.7A Expired CN1005463B (en) | 1985-08-06 | 1985-08-06 | Adjustable cyclonic separator and its use method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1005463B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104226493A (en) * | 2014-07-23 | 2014-12-24 | 江苏宝华环保科技有限公司 | Cyclone dust collector with integrated double air outlet valves |
| CN114929988A (en) * | 2019-11-08 | 2022-08-19 | 赛洛斯私营有限责任公司 | Device and method for regulating pressure |
-
1985
- 1985-08-06 CN CN85105962.7A patent/CN1005463B/en not_active Expired
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104226493A (en) * | 2014-07-23 | 2014-12-24 | 江苏宝华环保科技有限公司 | Cyclone dust collector with integrated double air outlet valves |
| CN104226493B (en) * | 2014-07-23 | 2016-09-28 | 江苏宝华环保科技有限公司 | There is the cyclone dust extractor of the double air vent valve being wholely set |
| CN114929988A (en) * | 2019-11-08 | 2022-08-19 | 赛洛斯私营有限责任公司 | Device and method for regulating pressure |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1005463B (en) | 1989-10-18 |
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