CN1622860A - Technique of separating fine particulates from gas steam - Google Patents
Technique of separating fine particulates from gas steam Download PDFInfo
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- CN1622860A CN1622860A CN02828591.3A CN02828591A CN1622860A CN 1622860 A CN1622860 A CN 1622860A CN 02828591 A CN02828591 A CN 02828591A CN 1622860 A CN1622860 A CN 1622860A
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
- B01D45/14—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by rotating vanes, discs, drums or brushes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
- B04C3/04—Multiple arrangement thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
- B04C3/06—Construction of inlets or outlets to the vortex chamber
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
- B04C2003/006—Construction of elements by which the vortex flow is generated or degenerated
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Cyclones (AREA)
Abstract
The present invention relates to a cyclone separator for use between an upper (102) and a lower tube sheet (104), the cyclone (100) comprising: a substantially vertical cyclone body (106) having a closed bottom end (108) and a top end (110) fixed with respect to the upper tube sheet (102), the cyclone body (106) defining a feed gas inlet (112) at its top end (110), the feed gas inlet (112) extending above the upper tube sheet (102) for receiving a particle-contaminated gas stream therefrom, the cyclone body (106) further defining a sidewall of the cyclone body, the sidewall defining a plurality of discharge openings (114) located between the upper (102) and the lower tube sheets (104) for discharging particles and a minor amount of an underflow gas stream; one or more swirl vanes (116) located proximate the gas inlet (112) to induce centripetal acceleration of the particle-contaminated gas stream; a gas outlet tube (118) defining a clean gas inlet (120) end located centrally within the cyclone body (106) for receiving a purified gas stream and further defining a clean gas outlet (122) located below the lower tube sheet (104) for discharging the purified gas stream, the gas outlet tube (118) extending through the closed bottom end (108) of the cyclone body (106) and further extending through the lower tube sheet (108).
Description
Technical field
The present invention relates to a kind of novel cyclone separator, it is used for removing trickle solid granulates from air-flow.This separator is particularly suitable to be used in the third level separation equipment, and it is used to usually to purifying from oil plant fluid catalystic cracking (FCC) catalyst regenerator flue gas stream that discharge, that contain catalyst fines.
Background technology
According to being to reduce the rules that pollutant emission is issued, must strictly control the particle emission in the industrial gas by federation, state and local government.In the engineering field that runs oil, the key link that relates to particulate emission is from the flue gas of the catalyst regenerator section discharge of fluid catalystic cracking (FCC) unit.The limit of United States federal regulations is at present: the solid particle that 1000 kilograms of coke of every burning produce in the catalyst regenerator is 1kg, perhaps is equivalent to be about 80-110mg/Nm
3The granule density of flue gas.Corresponding therewith European directive is also carrying out great change at present, the present 80-500mg/Nm that is defined as
3, but estimate that this numerical value might be reduced to 50mg/Nm
3
FCC technology has had the applicating history in more than 50 year, and for many years, people are improving this technology always, and at a lot of oil plants, this technology remains the main source of gasoline production.Gasoline and other light-end products to heavier (being that molecular weight is bigger), be worth that less hydrocarbon material is carried out cracking and the product that makes, raw material wherein for example is a diesel oil.Although FCC is a kind of huge and complicated processing procedure that relates to several factors, because the present invention is relevant with it, this paper will make a presentation the basic principle of this technology.
In the form of most conventional, FCC technology comprises a reactor, and itself and a catalyst regenerator closely couple together, and separates the nytron Tetramune at downstream part more subsequently.A main distinction of this technology is characterised in that the fluidization that a large amount of catalyst continue and circulates that wherein, the average particulate diameter of these catalyst is between the 50-100 micron, and aspect particle size and outward appearance, catalyst is equal to the very thin grains of sand.One ton of oil product is produced in every cracking, needs 5 tons of catalyst approximately, thereby, recycling of catalyst had quite high requirement.Need use the catalyst of very big total amount and recycle for the demand of small particle diameters catalyst for this, relevant therewith, a very urgent challenge just is: prevent that these catalyst from entering into the air-flow of discharge from reactor/regenerator system.
Generally speaking, adopt cyclone separator solid catalyst to be had 99% separative efficiency in the inside of reactor and regenerator.Generally speaking, regenerator comprises first order separator and second level separator (promptly main separator and auxilliary separator), in order to prevent the catalyst contamination of catalyst to regenerator flue gas, wherein, the flue gas of regenerator is the aerial combustion product of catalyst coke basically.Although particle size separates effectively for the cyclone that the catalyst granules of general value can be reproduced device inside, but trickle material (normally size is less than 50 microns catalyst particle, and the reason that these particles occur is friction effect and the corrosiveness in the reactor/regenerator environment of coarse abrasion) then is difficult to separated going out basically.The result is exactly that the granule density of FCC flue gas is usually at 200-1000mg/Nm
3Scope in.Whether for reach executed legal discharge standard, still wish to recover energy from flue gas stream, such content levels all can cause difficulty.In the latter case, if in fact select the energy recovery process, then the solid content in the FCC flue gas may be enough to the turbo blade of air blast in the regenerator is caused damage.
Thereby, need guarantee that usually the thin dust content in the FCC flue gas can be further reduced, and can utilize third level separator (TSS) device that has the multi-cyclone device to realize this purpose.Be well known that: precipitron can be finished this gas/solid detached job effectively, but its cost will be far above TSS, wherein, the work of TSS depends on the effect of the centripetal acceleration that is rich in the particle air-flow, and this centripetal acceleration forces the higher solid of density to move to the outer edge of vortex flow.In order to raise the efficiency, be used for the cyclone separator that FCC flue gas stream discharges is generally comprised many (may be 100) individual independently small cylinder cyclone body, these cyclone body are installed in the single container as multitube.The tube sheet of fixing the cyclone top and bottom has dusty gas is assigned to effect in the cyclone inlet, and have with the interval in the container be separated into several sections, the gas phase separated with collection and the function of solid phase.
In the technical field of relevant cyclone design, on important research all concentrates on so-called " back adverse current " the type cyclone, in this cyclone, the gas that will become a mandarin joins in the cyclone round a gas outlet tube, and gas outlet tube extends from the inlet side of cylindrical shape cyclone body.Can extract the gas be rich in particle from the perforate on the cyclone body sidewall, the gas of cleaning then basically from it flow path reverse flow when initial on cyclone body the one end-reverse flow opposite with air inlet to the gas outlet.The gas outlet is a body, and it is general coaxial with cyclone body, and is set in the cyclone body.The cyclone of these types has been described in patent US 5514271 B1 and US5372707 B1, in these two patents, the technical theme of invention concentrates on the shape and the distribution of perforate on the sidewall, so that the minimizing meeting is transported to turbulent eddy phenomenon in the clean air outlet again with solid.In U.S. Pat 5643537B1 and US 5538696B1, designed and be used for the device that is used with this basic cyclone, so that expand the flow pattern of eddy current further or improve the uniformity of eddy current flow pattern, and then improve separative efficiency.
But unfortunately, make air-flow oppositely can cause disturbance to flowing for itself, and this disturbance is not easy to be overcome from the design requirement that an effluent identical with air inlet goes out cyclone body.Described so-called " unidirectional straight-through " type cyclone separator in patent US 5690709B1, this separator has been eliminated the solid relevant with the gas reverse flow and has been sneaked into problem again.In the case, the gas of purification flows downward constantly, and discharges from cyclone body below lower perforated plate, and lower perforated plate is the physical boundary between the gas as the particle that is separated and after purifying.But such design also can aggravate astable flow pattern, and in the case, flow pattern heterogeneous is relevant with such phenomenon: through the open bottom of cylinder cyclone body, be substantially the angle at right angle with the particle dispatch to the air whirl that contains particle.In addition, the groundwork process of cyclone can relate to the change of airflow direction in the case, and in the ideal case, should avoid occurring the change of direction.In addition, in an overall device of being made up of a plurality of cyclones (for example TSS), the design form of open bottom can enter into adjacent cyclone body relatively large surface area is provided for " dirty " gas effluxes.The design form of this permission gas intercommunication between each Whirlwind barrel can reduce the efficient of separation.
Except the general item (uniformity of for example introducing centripetal acceleration and keeping flow pattern) that above design need be considered at cyclone, as improving usefulness further, then must come improvement is verified by actual tests at any special cyclone structure.In fact, some is being considered to alleviate non-homogeneous flow pattern and is limiting design being very poor in laboratory test that eddy current forms on the principle.In some cases, the hydrokinetics calculation machine software of discovery even complexity is also very poor to the prediction of TTS separative efficiency.Thereby, pass through a large amount of repetition tests and correction, and be aided with the overall goal of cyclone internal flow pattern being carried out Study on thinning, the technology of fine particle separation has obtained significant improvement from air-flow at present.
Summary of the invention
The present invention relates to a kind of improved cyclone, it is used for solid granulates is separated from air-flow.Many such cyclones can be combined in the container, so that be used as third level separator, be used for the air-flow that is subjected to solid pollution (refer in particular to the flue gas of discharging from the oil plant fluid catalytic cracking unit or other by the air-flow of solid pollution) is handled.In this cyclone, owing to make the gas that contains particle produce vortex, and make gas swirl its flow pattern when flowing through device minimum that is disturbed, so this cyclone separator has very high separative efficiency.In whole separation process, air inlet is all moved on same direction with the clean air that effluxes, and the clean air that utilizes a blast pipe will occupy most of volume in air inlet is removed from the centre of eddy current, and wherein, this blast pipe extends along cyclone body.In addition, solid granulates is sent by the perforate from the cyclone body sidewall, and is not to discharge vertically, so just can prevent that it from refluxing, and can prevent to occur between adjacent cyclone the gas phenomenon that communicates.
Adopt a plate or other structure to seal the bottom of cyclone body, this just means: the gas that contains particle can only be discharged in the perforate on cylindrical wall.Thereby the situation that will be higher than the bottom design of opening usually falls in the pressure by the gas discharging area.Pressure fall increase with gas velocity can cause particle stronger through the effect that the cylindrical wall spray discharges, thereby can prevent that solid from entering into cyclone body once more or adjacent cyclones is moved based on identical operation principle.Effectively, the gas that contains particle is discharged from some slits, and these slits have played the effect of " check valve ", and it can prevent that gas from taking place to reflux and particle enters in the Whirlwind barrel once more.
Cyclone of the present invention has such effect: the very trickle grit that diameter can be reached for a short time the 4-5 micron is separated from inlet air flow.If not, such solid contaminant will make contaminated gas can't meet environmental legislation, perhaps also may cause damage to the operate as normal of Power Recovery turbine.
Description of drawings
Fig. 1 has represented the rough schematic view of FCC unit in the prior art;
Rough schematic view among Fig. 2 has been represented third level separator in the prior art;
Fig. 3 is the cutaway view of cyclone of the present invention;
Fig. 4 is the profile of being done along the A-A line among Fig. 3;
Figure line among Fig. 5 shows that cyclone of the present invention is improved than its separating property of cyclone of the prior art; And
Fig. 6 has represented the improvement that the present invention realized aspect the d50 value, and d50 value wherein is meant the diameter measurement value that can be removed 50% particle.
The specific embodiment
The present invention is suitable for the interior very on a large scale gas stream of pollution that contains solid is carried out isolation of purified, is particularly suited for contained grit is handled at the air-flow of 1-10m scope.In the description of this paper, can mention a variety of productive gas purification operations, these operations comprise the processing that the air-flow of discharging from solid catalyst fluidized-bed process, coal combustion heater and heat power station is done.Some known oil refining work depends on fluidization, and for example described at file US 6137022B1, as to be used for methyl alcohol is changed into the technology of light olefin preferred implementation has just adopted solid-state zeolite catalyst composition.The present invention another especially at the field be: the air stream efflux to fluid catalytic cracking (FCC) purifies, be embedded catalyst granules in this discharge air-flow, these particles then come from friction, burn into and/or the corrasion under the process conditions in the reactor.
As mentioned above, fluid catalytic cracking (FCC) technology is known oil refinery technology, in most of the cases, relies on this technology and produces gasoline.Process variables generally comprises: the cracking reaction temperature, and this temperature is in 400-600 ℃ scope; Catalyst regeneration temperature, this temperature is in 500-900 ℃ of scope.No matter be cracking reaction, or regenerative process, all be lower than under 5 atmospheric environment and carry out in absolute pressure.Fig. 1 has represented a kind of typical FCC process equipment in the prior art, in this equipment, heavy hydrocarbon feed that pipeline 12 transports or crude oil with from regeneration catalyst standpipe 14 catalyst that enter, that just be reproduced contact.Along such contact taking place from the extended narrow section in reactor 10 bottoms (it is called as reactor riser 16).The heat that catalyst carries evaporates oil plant, then, exists under the condition of catalyst, oil is cleaved, in this process, oil plant and catalyst move up and enter into reactor 10 bodies along reactor riser, and operating pressure herein is a little less than the pressure in the riser 16.Then, utilization is positioned at the first order cyclone separator 18 and the second level cyclone separator 20 of inside reactor the lightweight nytron product and the catalyst separation that form after the cracking is opened, and the lightweight nytron product that forms after the cracking discharged from reactor 10 through pipeline 22, so that carry out the fractionation operation of postorder.In this, some side reaction meeting that takes place inevitably in reactor riser 16 stays harmful deposits of coke on catalyst, and this will reduce activity of such catalysts.Afterwards, catalyst is called used catalyst (or being partially used at least), need regenerates so that reuse catalyst.Used catalyst in this section, sprays into steam by pipeline 26, so that dispose the hydrocarbon vapor of any remnants dropping in the stripping section 24 after separating with hydrocarbon.Through after the stripping process, utilize a used catalyst standpipe 32 that used catalyst is transported in the catalyst regenerator 30.
In catalyst regenerator 30, the air draught that transports from pipeline 34 is directed by an air distributor 28 and contacts with used catalyst, and the coke that will be deposited on the catalyst burns, thereby the catalyst after the regeneration can be provided.Catalyst regeneration process provides a large amount of heats to catalyst, and these heats provide energy to offset the cracking reaction process of the heat absorption that is taken place in the reactor riser 16.Add some new catalyst from pipeline 36 to the bottom of regenerator 30, to replenish those catalyst that from reactor, run off away with the form of smalls or entrained particles.Catalyst and air-flow upwards flow together along the burner riser 38 in the regenerator 30, afterwards through regeneration (being about to coke burns), by making the mixed flow T-shape hopper 40 of flowing through come they are tentatively separated, wherein, top hopper 40 also is arranged in regenerator 30.It is to be finished by the first order that is positioned at catalyst regenerator 30 inside and second level regenerator cyclones 44 and 46 that the regeneration rear catalyst of discharging from top hopper 40 is carried out the meticulous work that separates with flue gas.Catalyst after the regeneration is transmitted back in the cracker 10 once more through regeneration rear catalyst standpipe 14.The coke owing to burnt comprises carbon dioxide and water from the cigarette steam that regenerator overhead line 42 is discharged, and has a small amount of other composition.Although first, second grade regenerator cyclones 44 and 46 can will be separated in the cigarette steam of catalyst from pipeline 42 after the overwhelming majority regeneration, trickle catalyst granules (great majority are produced by friction effect) always can pollute this air stream efflux.Thereby, contain in the flue gas of pollution of thin dirt and generally contain 200-1000mg/Nm
3Particle, the diameter of most of these particles is less than 50 microns.In view of this contamination level, owing to both needed the taking environmental conservation into consideration rules, also need to look after the selectivity design that recovers energy from flue gas, it is very urgent utilizing a third level separator (TSS) that flue gas is carried out the requirement that further purifies.
Fig. 2 has represented a kind of typical TSS in the prior art, and it comprises numerous individual cyclones.The inside of TSS container 50 is lined with refractory material 52 usually, is carried secretly the corrosiveness of catalyst granules to the metal surface to alleviate.Enter into the top of TSS from FCC regenerator flue gas that discharge, that contain thin dirt from the inlet 54 at top, inlet 54 is positioned at the top of upper perforated plate 56, and upper perforated plate 56 is keeping the upper end 58 of each cylindrical shape cyclone body 62.Then, the air-flow that contains thin dirt is assigned in the gas access 60 of each cyclone, and contacts with one or more volution blades 64 of close these inlets, so that impel the gas that contains particle to produce certain centripetal acceleration.Volution blade is the structure that is positioned at cyclone body, and it has the characteristic that the passage of flowing through to the gas that becomes a mandarin limits, and makes the mobile acceleration of air-flow thus.Volution blade can also change the flow direction that contains thin dirt air-flow, makes air-flow form for spiral flow or eddy current in the length range of cyclone body of flowing through.This eddying motion meeting of gas is with the highdensity solid-state wall that gets rid of mutually to cyclone body 62.
Cyclone design liaison shown in Figure 2 so-called " way flow " equipment, in this equipment, the bottom 66 of cyclone body 62 is openings, so just makes that being thrown near this Whirlwind barrel barrel solid granulates drops in the space 68 between the upper and lower tube sheet.The clean air that flows along the cyclone body center line then flow through earlier in the import 70 of a blast pipe 72 before the bottom 66 that arrives cyclone body 62.Then, clean air flows to the below of lower perforated plate 74 from blast pipe 72.Then, accounting for the mixed airflow that contains the cleaning of most volumes in the thin cloud of dust gas discharges from the exhaust outlet 76 that is positioned at TSS container 50 bottoms.The particle that is separated and a small amount of (usually less than contain thin cloud of dust gas 10%) underflow gasses then discharges from the separating particles and the underflow gasses outlet 78 that are positioned at the TSS50 bottom.
Represented among Fig. 3 that it also is fixed between upper perforated plate 102 and the lower perforated plate 104 according to a cyclone separator 100 independently of the present invention.Cyclone 100 comprises on end a cyclone body 106 basically, and its bottom 108 is sealed, and the upper end 110 of cyclone body is fixed on the upper perforated plate 102.Preferably: the bottom 108 of sealing is the form of horizontal plate.Cyclone body 110 places in the top defines an air inlet 112, is used for receiving the air-flow (flue gas stream that promptly contains thin dirt) that contains particle from the top of upper perforated plate 102.In addition, also define a plurality of apertures 114 that are used to discharge gas on the cyclone body.These apertures 114 are between upper perforated plate 102 and lower perforated plate 104, and the present position is located substantially on the bottom of cyclone body 106.Preferably, these apertures 114 extend upward near bottom 108 and from the bottom.These apertures allow particles and a spot of underflow gasses (in containing granular gas shared volume usually less than 10%) to be discharged between upper perforated plate 102 and the lower perforated plate 104.Because bottom 108 is closed, so, for the surface that loss provided of efflux gas just less relatively, thereby cause gas flow rate very high, the pressure of delivery port 114 both sides falls very big.This will bring the improvement of separating effect.
Near the air inlet that is positioned at the cyclone top, be provided with one or more volution blades 116, so that make the air-flow that contains particle produce centripetal acceleration.Blast pipe 118 positions are coaxial with cyclone body 106, and it extends through the bottom 108 of sealing, and extend through lower perforated plate 104 downwards further.The top and bottom of this blast pipe 118 define a clean gas inlet 120 and clean air outlet 122 respectively, clean gas inlet 120 is used to receive in the cyclone body 106, near air-flow after the purifications of its center line, clean air outlet 122 is positioned at the below of lower perforated plate 104, is used to discharge the air-flow after the purification.Clean gas inlet 120 is usually located at the top of delivery port 114.Clean air outlet 122 can be positioned at any position, as long as it is lower than lower end 108.As mentioned above, the directed state of cyclone body 106 is erect basically, thereby, can also obtain the assistance of gravity effect to the separation of solid-state phase.Preferably, cyclone body is the form of vertical cylinder, and still, other shape also is feasible certainly, and these shapes for example comprise taper.
As noted above like that, the major advantage of this design is: make rotational flow gas form vortex very uniformly, in the process that this vortex moves down along cyclone body and blast pipe, it can not be subjected to any interference basically.Advantage on the other hand is relevant with the increase that pressure falls, and the pressure when this pressure falls and is meant the gas that is rich in particle outwards spray in the aperture on cylindrical wall falls.Bigger base circle surface between cyclone body and the blast pipe in the through-type cyclone design mentioned above, these apertures are less for the surf zone that discharge provided of gas among the present invention.The result is exactly, and each aperture has all formed a kind of " non-return valve " structure, and it can stop the adverse current of discharging gas basically, and the adverse current of discharging gas then is the reason that separative efficiency reduces.
It is being by being provided with a plurality of apertures at the cylinder cyclone on this on the part that air-flow is kept inhomogeneity reason, and these apertures are used to discharge particle and a spot of underflow gasses.In fact the aperture can be Any shape, and can be positioned at any position of cylinder cyclone body, but preferably:, accumulate in this zone near the closed bottom end of cyclone to the small part aperture to prevent solid granulates.The aperture can also be a different shape, for example is slit or hole, and can be on each height of cyclone body.As shown in Figure 3, preferably: to the small part aperture is the shape of rectangular channel, and its bigger size (length) is arranged essentially parallel to the axis of cyclone body.These slits along the circumference of cyclone body with distributing evenly and at intervals of equating.In addition, the vertical length of slit is in 5% to 25% scope of cyclone body length.In a preferred embodiment, the lower end of rectangular slot is near the bottom of cyclone body sealing.
For the further overall separation efficiency that promotes the uniformity that flows and then improve solid-state-gaseous state, vent ports is arranged to tilt with respect to radial direction.This just make gas can be along the tangent line flow direction, do not change eddy flow state ground basically and from Whirlwind barrel, discharge, just as in cyclone body, flowing.Fig. 4 has expressed a kind of example of this ideal structure, and in Fig. 4, the edge 200 of slit 114 is inclined-plane (promptly and non-perpendicular to the tangent line at slit 114 present positions places cyclone body 106 circular cross sections).This inclined-plane with respect to cyclone body 106 curvature has produced such ideal effect: make gas have very big tangential speed component from cyclone body 106 when discharging, the flow direction of gas in cyclone body the time is also only by change in a small amount.In addition, the preceding limb of each rectangular slot principal length direction can be from cyclone body general curvature projection slightly, so that make air-flow turn to desirable tangential direction.Measure or collateral measures as an alternative also can be designed to the back edge of slit be trapped in the general curvature, to realize similar effects.
In addition, determine: when the aperture is arranged on the below of clean gas inlet, then can obtain good solid-state/gas separative efficiency, also represent such situation among Fig. 3.Preferably, allowing rotational flow gas is 0.05% to 5% of cyclone body surface area through the total open area of this discharge.Certainly, this parameter depends on several factors, and these factors comprise: the concentration of solid pollutant, average particle size particle size, air-flow velocity and pressure.When a plurality of cyclones of the present invention were used in the third level separator (TSS) of FCC oil refining unit, the effectiveness of performance of this separator was preferably its d50 particle size less than 5 microns.As defining in the prior art, the representative of d50 value can be by the diameter of the grit of removal 50% from the TSS underflow gasses.Therefore, in a preferred embodiment, purify the concentration that has particle more than 5 microns or 5 microns in the air-flow of back, this concentration is less than 50% of the granule density more than 5 microns or 5 microns in the flue gas stream that contains the catalyst micronic dust.
Can know further from example hereinafter and to understand the feature performance benefit that adopts cyclone of the present invention to reach, example hereinafter provides some laboratory tests data based on experiment, and experiment wherein is designed to simulate the condition of FCC flue gas when effluent stream.Although following example has been represented several concrete embodiments of cyclone separator of the present invention, these embodiments can not be used to limit the overall range of the present invention that is defined by the following claims.
Comparison example 1-7
" unidirectional straight-through " mentioned above, of the prior art type cyclone separator is carried out performance relatively with various cyclone separators according to the present invention.Studied from airflow flowing the situation that diameter is 40 microns or littler particle of separating.In each experiment, cyclone separator all comprises the cylinder of a 280mm inside dimension (i.d.) and the blast pipe of a 130mm, and blast pipe is coaxial with cylinder, and bottom cylinder above extend to below 250mm.
In comparative tests, except the development length of blast pipe, although the bottom of cylinder be made into to open-disk body has been installed in the outside of blast pipe, it is positioned at the 130mm place of below, cylinder bottom.The particle and a spot of underflow gasses that are separated are collected in the grit funnel around cyclone body, and wherein, isolated particle is basically to discharge with the rectangular angle of eddy flow inlet air flow.To containing granular gas and analyzing, to determine the distribution situation of particle size in its solid contaminant level and these pollutants from the clean air (overflow gas) that blast pipe is discharged.Similarly, similar analysis is also carried out in air inlet.
In separating experiment each time, the cyclone induction air flow ratio all is retained as 0.45-0.50Nm
3/ s.Solids content in this air inlet is 300-400mg/Nm
3, and the average diameter of particle is the 10-20 micron.From after, because blade has metering function to air-flow, so the speed of air-flow has increased near outflow the volution blade of air inlet.Be called as in the exhaust of underflow gasses and contain the solid that major part is separated, this part air-flow only accounts for 1% to 3% of charge volume, and concrete numerical value depends on specific experiment.After each experiment, calculate the weight ratio that solid that the removal efficient of solid granulates-be in the underflow gasses removed accounts for the input solid.Also determine diameter less than 10 microns the proportion of solid granulates in air-flow, and calculate the particle that estimates much diameters and can reach 50% clearance (d50 value).
Table 1 has been listed the experimental result of these comparison example.
Table 1
| Comparison example | Underflow gasses (percent by volume) | Blade exit air velocity (ms) | Separative efficiency (%) | Particulate percentages (%) less than 10m | D50 value (m) |
| ????1 | ????1 | ????24.1 | ????76.3 | ????78.5 | ????7.5 |
| ????2 | ????1 | ????39.3 | ????82.8 | ????84.8 | ????5.7 |
| ????3 | ????3 | ????40.5 | ????82.1 | ????93.9 | ????6.2 |
| ????4 | ????3 | ????40.3 | ????83.7 | ????93.3 | ????5.5 |
| ????5 | ????3 | ????24.1 | ????80.7 | ????76.8 | ????6.7 |
| ????6 | ????3 | ????38.9 | ????84.9 | ????87.5 | ????5.5 |
| ????7 | ????3 | ????39.5 | ????85.0 | ????87.4 | ????5.4 |
Example 8-12
Test by cyclone separator of the present invention is arranged in the cyclone, cyclone wherein has a horizontal base that is used to seal the cyclone body bottom.According to description of the invention, in the case, solid granulates is to discharge from the air inlet of eddy flow through the aperture on the cyclone cylinder sidewall.Realize design of the present invention by making two rectangular slot that 90mm is long, 10mm is wide.The length direction of slit is parallel to the axis of whirlwind cylinder body, and the width dimensions of bottom part is near near the horizontal base the cyclone body bottom.Parameter conditions such as induction air flow ratio, granularity and average particulate diameter are maintained in the scope that sets in the comparison example.In addition, utilizing volume is that 1% to 3% underflow value is studied.Same performance indications are also calculated and are listed in the table 2.
Table 2
| Comparison example | Underflow gasses (percent by volume) | Blade exit air velocity (m/s) | Separative efficiency (%) | Particulate percentages (%) less than 10m | D50 value (m) |
| ????8 | ????1 | ????39.7 | ????88.7 | ????91.6 | ????5.1 |
| ????9 | ????1 | ????24.1 | ????85.0 | ????89.5 | ????6.2 |
| ????10 | ????3 | ????40.2 | ????89.9 | ????71.5 | ????4.4 |
| ????11 | ????3 | ????40.2 | ????90.1 | ????87.7 | ????5.0 |
| ????12 | ????3 | ????24.6 | ????87.7 | ????87.8 | ????5.7 |
Can be clear that from experimental result above: " leading directly to " type cyclone of bottom opening than the prior art, under 1% and 3% underflow condition, cyclone of the present invention all has higher removal efficient to solid granulates.This result is indicated on the figure line among Fig. 5.In addition, cyclone separator of the present invention has advantage aspect the particle that diameter is the 4-5 micron removing, and the overall performance of this and FCC third level separator designs is corresponding.Can find out that according to the d50 performance parameter cyclone separator of the present invention has improved short grained separating power, Fig. 6 has expressed this characteristic.At last, opposite with the experimental result of cyclone separator comparison example in the prior art, cyclone separator of the present invention can obtain solids content and be lower than 50mg/Nm
3Cleaning (overflow) gas, this result will meet environmental regulation existing even in the future.
Claims (13)
1. cyclone separator that is used between upper perforated plate and the lower perforated plate, this cyclone comprises:
A) cyclone body of a perpendicular, it has the bottom and a top of a sealing, the top is fixed with respect to upper perforated plate, cyclone body defines an air inlet at its top end, and air inlet extends to the top of upper perforated plate, is used for receiving from here the air-flow by particle contamination, cyclone body also defines the sidewall of cyclone body, be limited with a plurality of delivery ports on the sidewall, these apertures are used to discharge particle and a small amount of underflow air-flow between upper perforated plate and lower perforated plate;
B) one or more volution blades near described air inlet are used to make by the air-flow of particle contamination produce centripetal acceleration; And
C) blast pipe, it limits a clean gas inlet end, this entrance point is positioned at the center of cyclone body, be used to admit the air-flow after the purification, this blast pipe also defines clean air outlet, and the below that it is positioned at lower perforated plate is used to discharge the air-flow after the purification, blast pipe extends through the bottom of cyclone body sealing, and further extends through lower perforated plate.
2. cyclone separator according to claim 1 is characterized in that: total aperture area of described delivery port is 0.05% to 5% of a cyclone body surface area.
3. cyclone separator according to claim 1 is characterized in that: the shape of cyclone body is cylindric substantially.
4. cyclone separator according to claim 1 is characterized in that: the bottom of sealing is essentially the plane of level.
5. cyclone separator according to claim 1 is characterized in that: clean gas inlet is positioned at the top of delivery port.
6. cyclone separator according to claim 1, it is characterized in that: delivery port tilts with respect to radial direction, thereby gas can be discharged, and its tangential direction in cyclone body does not change substantially.
7. cyclone separator according to claim 1, it is characterized in that: it is the slit of rectangle substantially that delivery port defines some, the length direction of these slits is arranged essentially parallel to the axis of cyclone body, and slit is evenly spaced apart round the girth of cyclone body.
8. cyclone separator according to claim 7 is characterized in that: the slit vertical length is 5% to 25% of a cyclone body length.
9. cyclone separator according to claim 7 is characterized in that: the lower end of rectangular slot is near the closed bottom of cyclone body.
10. cyclone separator according to claim 7 is characterized in that: the lower end of rectangular slot extends to the closed bottom of cyclone body.
11. one kind is utilized the method for the described cyclone separator of claim 1 to being purified by the air-flow of solid pollution.
12. method according to claim 11 is characterized in that: purify and to have 5 microns or greater than the concentration of 5 micron particles in the air-flow of back, this concentration is less than by 50% of the granule density more than 5 microns or 5 microns in the flue gas stream of particle contamination.
13. method according to claim 11 is characterized in that: a spot of underflow air-flow is less than by 10% of the air-flow of particle contamination.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/US2002/002232 WO2003066225A1 (en) | 2002-01-24 | 2002-01-24 | Separating fine solid particulates from a gas stream |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1622860A true CN1622860A (en) | 2005-06-01 |
| CN1287902C CN1287902C (en) | 2006-12-06 |
Family
ID=27732062
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN02828591.3A Expired - Fee Related CN1287902C (en) | 2002-01-24 | 2002-01-24 | Technique of separating fine particulates from gas steam |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP1472004A1 (en) |
| CN (1) | CN1287902C (en) |
| AU (1) | AU2002309484A1 (en) |
| CA (1) | CA2477482A1 (en) |
| WO (1) | WO2003066225A1 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102343188A (en) * | 2011-10-27 | 2012-02-08 | 北京德天御投资管理有限责任公司 | Dust removing device applied to pipeline |
| CN101457688B (en) * | 2007-12-14 | 2013-01-02 | 现代自动车株式会社 | Intake duct system for an engine |
| CN108499750A (en) * | 2017-02-27 | 2018-09-07 | 松下知识产权经营株式会社 | Separator |
| CN109174478A (en) * | 2018-08-28 | 2019-01-11 | 中石化（洛阳）科技有限公司 | A kind of Combined vertical flow separation single tube and cyclone separator |
| CN111315491A (en) * | 2017-09-30 | 2020-06-19 | 环球油品有限责任公司 | Apparatus and method for gas-solid separation |
| CN111495040A (en) * | 2020-04-30 | 2020-08-07 | 西安交通大学 | Horizontal pipeline type gas-liquid separation device and method |
| CN113041759A (en) * | 2019-12-27 | 2021-06-29 | 中国石油大学(北京) | Multi-pipe cyclone separator underflow gas-solid separation method and separation device |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8419835B2 (en) | 2010-08-10 | 2013-04-16 | Uop Llc | Apparatuses and methods for gas-solid separations using cyclones |
| US8709115B2 (en) * | 2011-12-16 | 2014-04-29 | Uop Llc | Cyclone separators and separator apparatuses including the cyclone separators |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2063781T3 (en) * | 1988-06-02 | 1995-01-16 | Cyclofil Pty Ltd | SEPARATOR DEVICE WITH VORTICIAL TUBE. |
| US5514271A (en) * | 1994-04-28 | 1996-05-07 | Mobil Oil Corporation | Underflow cyclone with perforated barrel |
| US5538696A (en) * | 1994-05-02 | 1996-07-23 | Mobil Oil Corporation | FCC process and apparatus with contained vortex third stage separator |
| AUPN474095A0 (en) * | 1995-08-09 | 1995-08-31 | Barnes, Peter Haddon | Improved dust separator for process flue gas |
-
2002
- 2002-01-24 EP EP02736482A patent/EP1472004A1/en not_active Withdrawn
- 2002-01-24 WO PCT/US2002/002232 patent/WO2003066225A1/en not_active Application Discontinuation
- 2002-01-24 CN CN02828591.3A patent/CN1287902C/en not_active Expired - Fee Related
- 2002-01-24 CA CA002477482A patent/CA2477482A1/en not_active Abandoned
- 2002-01-24 AU AU2002309484A patent/AU2002309484A1/en not_active Abandoned
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101457688B (en) * | 2007-12-14 | 2013-01-02 | 现代自动车株式会社 | Intake duct system for an engine |
| CN102343188A (en) * | 2011-10-27 | 2012-02-08 | 北京德天御投资管理有限责任公司 | Dust removing device applied to pipeline |
| CN108499750A (en) * | 2017-02-27 | 2018-09-07 | 松下知识产权经营株式会社 | Separator |
| CN108499750B (en) * | 2017-02-27 | 2019-12-20 | 松下知识产权经营株式会社 | Separating device |
| CN111315491A (en) * | 2017-09-30 | 2020-06-19 | 环球油品有限责任公司 | Apparatus and method for gas-solid separation |
| CN111315491B (en) * | 2017-09-30 | 2022-08-16 | 环球油品有限责任公司 | Apparatus and method for gas-solid separation |
| CN109174478A (en) * | 2018-08-28 | 2019-01-11 | 中石化（洛阳）科技有限公司 | A kind of Combined vertical flow separation single tube and cyclone separator |
| CN113041759A (en) * | 2019-12-27 | 2021-06-29 | 中国石油大学(北京) | Multi-pipe cyclone separator underflow gas-solid separation method and separation device |
| CN113041759B (en) * | 2019-12-27 | 2024-05-28 | 中国石油大学(北京) | Bottom flow gas-solid separation method and device for multitube cyclone separator |
| CN111495040A (en) * | 2020-04-30 | 2020-08-07 | 西安交通大学 | Horizontal pipeline type gas-liquid separation device and method |
| CN111495040B (en) * | 2020-04-30 | 2021-03-16 | 西安交通大学 | Horizontal pipeline type gas-liquid separation device and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2477482A1 (en) | 2003-08-14 |
| CN1287902C (en) | 2006-12-06 |
| AU2002309484A1 (en) | 2003-09-02 |
| EP1472004A1 (en) | 2004-11-03 |
| WO2003066225A1 (en) | 2003-08-14 |
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