CN1005463B - Adjustable cyclonic separator and its use method - Google Patents
Adjustable cyclonic separator and its use method Download PDFInfo
- Publication number
- CN1005463B CN1005463B CN85105962.7A CN85105962A CN1005463B CN 1005463 B CN1005463 B CN 1005463B CN 85105962 A CN85105962 A CN 85105962A CN 1005463 B CN1005463 B CN 1005463B
- Authority
- CN
- China
- Prior art keywords
- fluid
- mentioned
- cyclone separator
- air cell
- separator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Images
Landscapes
- Cyclones (AREA)
Abstract
The present invention relates to a method and a device for changing pressure drops of both ends of a running separator rather than interrupting the running or slightly reducing the running efficiency. The device is carried with suspended particle fluid which is heavier than the device, the fluid flows into the upper part of a common cylindrical vortex chamber along a tangent line, and therefore, particles are separated because of the downward motion facing to outside in a radical direction and facing to a bottom particle outlet. The purified fluid flows to a top discharge opening. When the fluid and the particles flow in the separator which is not interrupted, a vortex flow stabilizer faces to or leaves away from a fluid outlet hole to move, and the pressure drops of both ends of the separator are increased or reduced.
Description
The present invention relates to the using method of adjustable cyclonic separator.
In common cyclone separator, band gas of suspended particles or liquid is from tangential inflow, and forms 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 turning point of eddy current or below slightly.
The vertical length of eddy current can onlinely be regulated in the known cyclone separator, and the flow and the pressure that carry particle fluid motion or change inlet fluid that need not stop in advance handling.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.The present invention seeks to the improvement that utilizes above-mentioned principle to carry out, make the inlet amount of each cyclone separator evenly equate or stop or reduce the flow of some separators for the cyclone separator method of operating of a sets in parallel operation.
Maneuver of the present invention: be that each all accepts the fluid that a part contains suspended particles in the cyclone separator of a sets in parallel operation, the density of this fluid is different with contained suspended particles density, and the feature of this method is: (a) connect a cyclone separator that contains the right circular cylinder minor air cell at least; Can make comprise jljl not mutually and the fluid of the discontinuous and dispersed component of density along the device on tangent line inflow top, minor air cell, make and enter in the fluid heavier component to form one with respect to the eddy current of radially outwards throwing and moving downward than light component; Be located at top, minor air cell or near the heavier component dilution fluid outlet device it; Be located at minor air cell's end opposite or near the fluid issuing device that is rich in heavier component it; Be installed in the removable swirl stabilization device in centre position, minor air cell, but in this position stabilizing vortex; Can be from the device of minor air cell's external control, this device is used to make the swirl stabilization device to move toward or away from top, above-mentioned minor air cell or near the fluid issuing it, and is used to regulate the distance between stabilising arrangement and the heavy ends dilution fluid outlet device; (b) 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 the fluid flow of at least one outlet by above-mentioned each multiple cyclone in parallel be substantially equal to the rate of discharge of another above-mentioned multiple cyclone in parallel at least.
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.
The inventive method has following 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 pipe, 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 the discharge currents of cyclone separator equally, to stop flowing of fluid fully, (4) regulate movably vortex stabiliser, with control drain separator heavy ends 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 enrichment relatively 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 thing phase of different densities.The intensity of eddy current and stability are being all in all aspect the separative efficiency of determining cyclone separator and the abrasion resistance.Reliability, separating property and the abrasion resistance that improves cyclone separator is unusual important commercial target, the modified cyclone separator that has begun one's study and can reduce wearing and tearing and raise the efficiency to obtain, particularly research comprise the cyclone separator internal structure of swirl stabilization device." stabilisation " term is meant eddy flow 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) (PLAXIGLASR) model.The ratio of preference pattern, so that under the same input speed of 25 meter per seconds, Reynolds (Reynolds and Shi Tandun (Strouhal) number of simulation real fluid Cracking catalyst (FCC) cyclone separator.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
9Wi γ 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 110～13) kilobar, 16～19 ℃ and flow be greater than 0.5 meter
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.
Tested the swirl stabilization apparatus of some types, obtained Different Results, found that usually flat board or disc-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 circumference 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 81(area is 5.8 * 10 for 0.076 meter pipe and height 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 28.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 inches.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 can cause the particle of wearing and tearing because cyclonic action is outwards dished out rapidly continuously, therefore basically only along the vortex stabiliser surface or by dilution particle fluid outlet edge flowing liquid 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 to control 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, and the impurity solid is discharged downwards and 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 under 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, to receive carried catalyst waste gas from regenerator by one.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 Particle Density.The present invention can be used to control dilution or be rich in the undercurrent of particle fluid and the shunting between the overflow.The place that particularly comprises undercurrent in the chamber below the separator minor air cell is by changing the pressure drop at cyclone separator two ends, the present invention can be used to control the flow that contains abrasion particle fluid as valve, or stop it in the mode that can avoid the corrosion of any actual wear and flow.
Claims (8)
1, the cyclone separator method of operating of a sets in parallel operation, each all accepts the fluid that a part contains suspended particles in this group cyclone separator, and the density of this fluid is different with contained suspended particles density, and this method of operating is characterised in that it comprises:
(a) be connected with a cyclone separator at least, this separator comprises the right circular cylinder minor air cell;
Can make comprise jljl not mutually and the fluid of the discontinuous and dispersed component of density flow into the device on top, above-mentioned minor air cell along tangent line, make and enter component heavier in the fluid to form one with respect to the eddy current of radially outwards throwing and moving downward than light component;
Be located at the heavier component dilution fluid outlet device of top, above-mentioned minor air cell or its vicinity;
Be located at the fluid issuing device that is rich in heavier component of above-mentioned minor air cell end opposite or its vicinity;
Be positioned at intermediate movable swirl stabilization device among being installed in above-mentioned minor air cell, on this position, can stablize above-mentioned eddy current
The device that can control from outside, above-mentioned minor air cell, this device is used to make above-mentioned swirl stabilization device toward or away from top, above-mentioned minor air cell or near the motion of the fluid issuing it, and is used to regulate the distance between aforementioned stable device and the above-mentioned heavy ends dilution fluid outlet device;
(b) 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.
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 CN85105962A (en) | 1987-02-25 |
| CN1005463B true 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) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| NL1043455B1 (en) * | 2019-11-08 | 2021-07-20 | Cyros B V | Device and method for controlling pressure |
-
1985
- 1985-08-06 CN CN85105962.7A patent/CN1005463B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN85105962A (en) | 1987-02-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4810264A (en) | Process for cleaning and splitting particle-containing fluid with an adjustable cyclone separator | |
| Wang et al. | Hydrodynamics of cocurrent downflow circulating fluidized bed (CDCFB) | |
| FI72889C (en) | ANALYZING AND FARING EQUIPMENT FOR AVAILABLE CATALYST PARTICULAR FOR CATALYTIC FLYING EQUIPMENT FOR GASFORM. | |
| Zhu et al. | Cocurrent downflow circulating fluidized bed (downer) reactors—a state of the art review | |
| US2967618A (en) | Vortical separator | |
| US4789476A (en) | Cyclone separator with two separating zones and static guide mechanisms | |
| Pärssinen et al. | Axial and radial solids distribution in a long and high‐flux CFB riser | |
| US4692311A (en) | Apparatus for the separation of fluid cracking catalyst particles from gaseous hydrocarbons | |
| US3597901A (en) | Gas scrubber, entrainment separator and combination thereof | |
| US20180043292A1 (en) | Swirl tube separators | |
| CN106269508B (en) | A kind of annular fluidized bed separator of granulate mixture and its gas solid reactor system of participation | |
| FI109881B (en) | A method and apparatus for separating a solid from a gas | |
| Baron et al. | Electrostatic effects on entrainment from a fluidized bed | |
| US3767174A (en) | Gas scrubber, entrainment separator and combination thereof | |
| US2981413A (en) | Process for separating solids in liquid suspension | |
| Zhang et al. | Flow development in a gas‐solids downer fluidized bed | |
| CN1005463B (en) | Adjustable cyclonic separator and its use method | |
| CN86108105A (en) | Circulating fluidized bed reactor and from exhaust the method for separating solids material | |
| CN109225689A (en) | A kind of tubular cyclones | |
| US4932594A (en) | Pulverized coal flow control system | |
| GB1401331A (en) | Grader for fine-grained material | |
| US3798883A (en) | Gas scrubber, entrainment separator and combination thereof | |
| CA1259573A (en) | Adjustable syclone separator and process of using the same | |
| CA1258037A (en) | Apparatus for separating solids in a circulating fluidized bed reactor | |
| CN212018227U (en) | High-efficiency large cyclone separation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C13 | Decision | ||
| GR02 | Examined patent application | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |