CA1117034A - Cyclone separator - Google Patents
Cyclone separatorInfo
- Publication number
- CA1117034A CA1117034A CA000314179A CA314179A CA1117034A CA 1117034 A CA1117034 A CA 1117034A CA 000314179 A CA000314179 A CA 000314179A CA 314179 A CA314179 A CA 314179A CA 1117034 A CA1117034 A CA 1117034A
- Authority
- CA
- Canada
- Prior art keywords
- solids
- cyclone separator
- gas outlet
- free
- feet per
- 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
Classifications
-
- 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
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/24—Multiple arrangement thereof
- B04C5/28—Multiple arrangement thereof for parallel flow
Abstract
CYCLONE SEPARATOR
(D#74,797-F) ABSTRACT OF THE DISCLOSURE
A cyclone separator for the removal of entrained solids from gases, the cyclone separator having a barrel portion and a conical portion which cooperatively define a separation chamber, a gas inlet in open communication with the portion of the separation chamber defined by the barrel portion, a gas outlet tube extending centrally, upwardly from the barrel portion, a solids discharge outlet located at the lower end of the conical section, a solids discharge dipleg conduit in open communication with the solids outlet, the geometric parameters of the separator providing high efficiency with minimal erosion.
(D#74,797-F) ABSTRACT OF THE DISCLOSURE
A cyclone separator for the removal of entrained solids from gases, the cyclone separator having a barrel portion and a conical portion which cooperatively define a separation chamber, a gas inlet in open communication with the portion of the separation chamber defined by the barrel portion, a gas outlet tube extending centrally, upwardly from the barrel portion, a solids discharge outlet located at the lower end of the conical section, a solids discharge dipleg conduit in open communication with the solids outlet, the geometric parameters of the separator providing high efficiency with minimal erosion.
Description
3~L 1 BACKGROUND OF THE INVENTION
The present invention relates to gas-solid separators.
More particularly, the present invention relates to cyclone separators of improved design and especially to cyclone separators ~useful in separating entrained solid catalyst from hydrocarbon vapors or flue gases encountered in the catalytic cracking of ~hydrocarbon.
Cyclone separatorsare widely used as dust collectors or gas-solid separators. For example, cyclones are widely used 'lin both the reactor and regenerator sections of Fluidized ,ICatalytic Cracking Units (FCCU) for the removal of entrained catalyst particles from hydrocarbon effluent vapors and flue gases used and/or produced in the cracking process. The con-Ilstruction and operation of cyclone separators is well known ~jto those skilled in the art. Briefly, a cyclone separator has ¦la cylindrical upper portion, commonly called a barrel, adjoined to a lower conic section, the lower, smaller diameter end of lthe conic section forming a solids outlet. Gas enters the B barrel portion, tangentially, at one or more ~r~nts, and !!lexits through a centrally disposed gas outlet extending through the top wall of the barrel. The dust, e.g. catalyst ¦particles, by virtue of their inertia, tend to move toward ¦Ithe outside walls of the separator and eventually leave through ¦lhe solids outlet. Essentially, a cyclone separator is a 111 ettling chamber in which gravitational acceleration is re-¦placed by centrifugal acceleration. Under common operating l -onditions, it is not unusual for the centrifugal separating I
The present invention relates to gas-solid separators.
More particularly, the present invention relates to cyclone separators of improved design and especially to cyclone separators ~useful in separating entrained solid catalyst from hydrocarbon vapors or flue gases encountered in the catalytic cracking of ~hydrocarbon.
Cyclone separatorsare widely used as dust collectors or gas-solid separators. For example, cyclones are widely used 'lin both the reactor and regenerator sections of Fluidized ,ICatalytic Cracking Units (FCCU) for the removal of entrained catalyst particles from hydrocarbon effluent vapors and flue gases used and/or produced in the cracking process. The con-Ilstruction and operation of cyclone separators is well known ~jto those skilled in the art. Briefly, a cyclone separator has ¦la cylindrical upper portion, commonly called a barrel, adjoined to a lower conic section, the lower, smaller diameter end of lthe conic section forming a solids outlet. Gas enters the B barrel portion, tangentially, at one or more ~r~nts, and !!lexits through a centrally disposed gas outlet extending through the top wall of the barrel. The dust, e.g. catalyst ¦particles, by virtue of their inertia, tend to move toward ¦Ithe outside walls of the separator and eventually leave through ¦lhe solids outlet. Essentially, a cyclone separator is a 111 ettling chamber in which gravitational acceleration is re-¦placed by centrifugal acceleration. Under common operating l -onditions, it is not unusual for the centrifugal separating I
-2-1.l ~1703~
force or acceleration to be several hundred times gravitational force. The high forces imparted to the dust or solid particles results in a highly erosive effect on the internal walls of the cyclone thereby resulting in rapid wearing.
Cyclone separators of the type under consideration are commonly used as last stage dust collectors, as for example, to remove remaining dust and solid particles from gases such as flue gases prior to atmospheric venting. Because of increasing concern for the environment, it is necessary that such cyclone separators, when they are used as last stage solids removing devices, be as efficient as possible in order that the gas vented to the atmosphere will be as pollution free as possible.
The invention provides for a cyclone separator com-prising an upper barrel portion having an inlet means and a solids-free-gas outlet means wherein said separator inlet means having a cross-sectional inlet area (I) sufficient to provide a gas inlet velocity in the range of 52 feet per second to 80 feet per second, said solids-free-gas outlet means having a cross-sectional outlet area (O) sufficient to provide a solids-free-gas outlet velocity in the range of 52 feet per second to 200 feet per second, the ratio of said solids-free-gas cross-sectional outlet area (O) to said separator cross-sectional in-let area (I) being in the range of substantially 0/I = 0.4/1 to 1.0/1.0, and the distance (L) between said gas outlet means and a solids outlet being related to the diameter (D) of the upper barrel portion of the cyclone separator in an amount such that L/D = 4.49-1.09 (O/I).
The invention also provides a method for removal of entrained solids from gases in an upright cyclone separator ~ - 3 -1~ ~7~)34 comprising an upper cylindrical barrel portion with a diameter (D) and having an inlet with a cross-sectional area (I), a solids-free-gas outlet with a cross-sectional area (O), with the ratio O/I in the range of 0.4/1 to 1/1, and a solids outlet at a vertical distance (L) below the solids-free-gas outlet D with the ratio L/0 about 4, said method comprising: injecting gases with entrained solids in the inlet at a speed in the range of substantially 52 feet per second to 80 feet per second;
spinning the injected gases with the entrained solids around and down the cyclone separator to the solids outlet; and ejecting resultant solids-free-gases through the gas outlet at a speed in the range of substantially 52 ~eet per second to 200 feet per second.
The present invention relies on the unexpected finding that by controlling certain geometrical parameters in the design and construction of cyclone separators, the latter can be made much more efficient and wearing of the internal surfaces due to erosion can be greatly reduced. A cyclone separator of one embodiment of the present invention comprises an upper, generally cylindrical barrel portion having a top wall, and a lower, generally conic portion having a solids outlet at the smaller diameter, lower end thereof. The lower, open end of the barrel portion and the conic portion, at its larger diameter end, are adjoined and together define a separation chamber. The barrel portion is provided with a gas inlet for introducing a gas stream tangentially into the separation chamber. A gas outlet tube, which in the preferred case is generally centrally, vertically disposed, extends through the top wall of the barrel portion and has a lower end terminating internally of the separation chamber. A generally cylindrical, solids discharge ~ - 4 -~7~34 dipleg conduit has an upper end in open communication with the solids outlet whereby disentrained solids can be removed from the separator. The usually rectangular, cross-sectional area, "I", of the gas inlet is sufficient to provide a gas inlet velocity of about 80 ft/sec or less whereas the cross-sectional area, "O", of the gas outlet tube is sufficient to provide a gas outlet velocity of about 178 ft/sec or less. The ratio O/I
is maintained in the range of from about 0.4/1 to about 1/1.
The ratio of the distance, "L", between the solids-free-gas out-let at the lower end of the gas outlet tube and the solidsoutlet at the upper end of the dipleg conduit, to the internal diameter, D - 4a -~ ~ 7 O 3 4 ~"D", of the barrel portion of the separator is such as to ~satisfy the equation:
j L/D = -1.09 (O/I) + 4.49.
IlMost preferably, the cyclone is designed such that the ratio I!L/D is about 4Ø
In a preferred embodiment, the cyclone is provided ¦with a dust bowl which provides communication between the upper ¦¦end of the dipleg conduit and the solids outlet formed in the ¦llower conic portion of the separator. It has been found that 'lla cyclone separator, designed in accordance with the above ! parameters, functions most effectively in removing solids, e.g. catalyst particulates from gas streams such as hydrocarbons or flue gases, particularly those used in FCCU.
.15 BRIEF DESCRIPTION OF THE DRAWINGS
Fig. 1 is an elevational view showing, schematically, a typical arrangement of a regenerator used in a FCCU and in-corporating the cyclone separators of the present invention.
Fig. 2 is a partial, elevational view, similar to Fig. 1, but showing in greater detail the unique construction ¦of the cyclone separators of the present invention.
¦ Fig. 3 is a view, partially reduced in size, taken long the lines 3-3 of Fig. 2.
¦ DESCRIPTION OF THE PREFERRED E~BODIMENTS
While the invention will be described with particular -eference to the use of the cyclone separators of the present vention in removing entrained catalyst particle~ from combustion _5_ ~ ~7~34 gases leaving a regenerator used in a FCCU, it is to be understood that the cyclones disclosed and claimed herein find utility in any system wherein a cyclone separator can be used to separate entrained solids from gaseous streams.
The use of a cyclone separator as a means of removing solids from entrained gases in a regeneration scheme is shown in United States Patent 3,394,076. The regenerator system shown in Figure 1 is substantially the same as that shown in the cited patent. Referring then to Figure 1, the regenerator~ shown gen-erally as 10, is provided with an inlet conduit 12 through which is fed spent catalyst from a suitable FCCU reactor (not shown).
A dense phase bed 14 having an upper level 16 is maintained in regenerator 10. An oxygen containing gas, for example, air, is - introduced into regenerator 10 through a suitable air ring 18.
Coke or other carbonaceous material coated on the catalyst par-ticles in regenerator 10 is burned away by the oxygen in the regeneration gases.
Regenerated catalyst is withdrawn from regenerator 10 through draw-off standpipe 20 and returned for further usage in the reactor section of the FCCU. Combustion gases leaving the dense phase bed at level 16 and entrained catalyst particles pass into the disengaging space 22 in the upper portion of the regenerator 10. The gases pass through a first stage cyclone separator 24 via inlet 26. Solids disengaged in separator 24 are returned to bed 14 in regenerator 10 via dipleg 28. The gases leave cyclone separator 24 via transfer line 30 and enter second or last stage separator 32. Solids disengaged in separator 32 are returned to the catalyst bed via dipleg 34 while the sub-stantially solid-free gas passes from separator 32 via gas ¦discharge conduit 35 into plenum 36 located in the upper portion ¦of regenerator lO. The gases in plenum 36 are vented or otherwise removed from regenerator lO via line 38.
I Turning now to Fig. 2, there is shown, in detail, ~the system depicted schematically in Fig. l. First and second stage cyclone separators 24 and 32, respectively, are disposed in regenerator lO by means of suita~le bracing and supports (not shown). First stage cyclone separator 24 has an upper l cylindrical barrel portion 40 having a top wall 52, the lower 1 end of barrel portion 40 being open. Adjoined to the lower, open end of barrel portion 40 is the upper open, greater diameter end of lower conic portion 42. Barrel portion 40 and conic portion 42 cooperatively define an internal separation chamber.
Adjoined to the lower end of conic portion 42 is a dust bowl, shown generally as 25, dust bowl 25 comprising an upper cy-lindrical barrel section 46 and a lower conic section 48.
Conic section 48 terminates at its lower end, in an outlet which is connected to the upper end of dipleg 28. A gas inlet 26, which is generally rectangular in cross-sectional shape, provides a means for introducing a gas stream tangentially into the barrel portion 40 of cyclone 24. A gas outlet tube 50 extends through the top wall 52 of cyclone 24.
Gas outlet tube 50 communicates with gas transfer conduit 30 which in turn is in open communication with a rectangular gas inlet 54 in second stage separator 32. Second stage separator 32 has an upper cylindrical barrel portion 56 with a top wall 72 and an open, lower end, and a lower conic portion 58 with an upper, open end. The lower end of barrel 7(~34 ;
:' .
portion 56 and the upper end of conic portion 58 are adjoined and together define a separation chamber 6 a . Conic section 58, at its lower end, defines a circular solids outlet 62 which lis in open communication with dust bowl 33. Dust bowl 33, ¦¦like dust bowl 25, is comprised basically of an upper cylindri-¦cal barrel section 64 and a lower conic section 66, the junction of barrel section 64 and conic section 66 lying in a plane which passes substantially through the apex, shown as 68, of the projection (shown in phantom lines) of the conic portion 58 ¦ of separator 32. The lower conic section 66 of dust bowl 33 is in open communication with the upper end 70 of cylindrical dipleg 34.
Gas outlet tube 35 extends through the top wall 72 of cylindrical barrel portion 56, gas outlet tube 35 having a lower end 74 terminating in separation chamber 60. Gas out-let tube 35 has an upper open end 76 in communication with the interior of plenum 36. Plenum 36 is defined by a portion of the upper interior wall of regenerator 10, a cylindrical wall 78 ffixed to the upper, inner wall of regenerator 10, and a domed shaped bottom wall 80, affixed at its periphery to the lower end of cylindrical wall 78.
In operation, gas from disengaging space 22 enters rectangular gas inlet 26 of separator 24 and is introduced tangentially into the barrel portion 40. Solid particles, because of their inertia, move toward the walls of separator ¦ 24 and generally spiral downwardly toward dust bowl 25, being ¦ultimately discharged through dipleg 28 into the dense phase : ¦in regenerator 10. The gas, at least partially free of solids, passes upwardly through the central gas outlet tube 50 into transfer conduit 30. The gas then enters second stage cyclone jl 32 via rectangular inlet 54, the gas being introduced tan-l gentially into the part of separation chamber 60 defined by the barrel portion 56 of separator 32~ Solids once again move to the walls of the separator 32, spiral downwardly into dust ¦bowl 33, and return to regenerator 10 via dipleg 34. The substantially solid-free gas passes upwardly through the lower lend 74 of gas outlet tub 35 and is discharged through the upper iend 76 into plenum 36.
¦ It has been unexpectedly found that, particularly ~in the case of the last stage cyclone separator 32, or if more than two stages are used, the last several stages, if certain parameters, with regard to the geometry of the cyclone separator are adhered to, enhanced efficiency and reduced wearing due to erosion result. Thus, for example, it is necessary that the gas inlet, as for example, inlet 54, have a cross-sectional area, "I", which is sufficient to provide a gas inlet velocity of about 80 ft/sec or less~ and preferably a gas inlet velocity ¦of from about 52 to about 80ft/sec. Additionally, it is nec-essary that the gas outlet tube 35 have a cross-sectional area, "O", sufficient to provide a gas outlet velocity of about 178 ft/sec or less. It is also necessary, to achieve optimum efficiency and maximum reduction in wear due to erosion! that ~ertain relationships between the cross-sectional areas "I" and 'O" be maintained. Thus it has been found that the ratio O/I
should be in the range of from about 0.4/1 to about 1/1, and ¦
?referably from about 0.6/1 to about 0.45/1. Lastly, it is _9_ necessary for the cyclone separator of the present invention be designed such that the ratio of the distance, shown as L, between the solids-free-gas outlet at the lower end of outlet tube 35 and the solids outlet at the upper end of dipleg conduit 34 to the internal diameter, shown as D, of the barrel portion 56 of cyclone separator 32 be such as to satisfy the equation:
L/D = -1.09 (O/I) + 4.49.
Most preferably, for minimizing erosion of the cyclone internals by impinging catalyst, the ratio L/D is about 4Ø Cyclone separators designed in accordance with the above critical para-meters exhibit maximum efficiency and minimum wear due to erosion.
In addition to the above parameters, it has also been found desirable that the diameter of the upper end of the dipleg conduit, i.e. conduit 34, be from about 0.05 D to about 0.2 D.
Additionally, and as pointed out above, in cases where a dust bowl such as 33 is employed it is desirable that the apex of the projection of the lower conic portion of the cyclone separator lie in a plane passing substantially through the junction of the barrel section and the conic section of the dust bowl. It is also possible that the diameter of the dust bowl and the diameter of the dipleg conduit be substantially the same.
It is further desirable that there be a solids entrance means 62 to a dust bowl 33 in said cyclone separator having a diameter D62 relative to the diameter (D) of the upper barrel portion D60 in the range of substantially 0.2D to 0.8D.
As used herein, the term "diameter(s)" refers to the internal diameter(s). It will be understood that, generally speaking, the cyclone separator of the present invention will be disposed in a generally vertical position. However, it is within the scope of the invention for the cyclone separators of the present invention to be disposed off-vertical.
The invention may be embodied in other specific forms without departing from the spirir or essential ,characteristics thereof. The present embodiments are S therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being in-. dicated by the appended claims rather than by the foregoing description, and all changes which would come within the meaning and range of the equivalence of the claims are ~therefore intended to be embraced therein.
force or acceleration to be several hundred times gravitational force. The high forces imparted to the dust or solid particles results in a highly erosive effect on the internal walls of the cyclone thereby resulting in rapid wearing.
Cyclone separators of the type under consideration are commonly used as last stage dust collectors, as for example, to remove remaining dust and solid particles from gases such as flue gases prior to atmospheric venting. Because of increasing concern for the environment, it is necessary that such cyclone separators, when they are used as last stage solids removing devices, be as efficient as possible in order that the gas vented to the atmosphere will be as pollution free as possible.
The invention provides for a cyclone separator com-prising an upper barrel portion having an inlet means and a solids-free-gas outlet means wherein said separator inlet means having a cross-sectional inlet area (I) sufficient to provide a gas inlet velocity in the range of 52 feet per second to 80 feet per second, said solids-free-gas outlet means having a cross-sectional outlet area (O) sufficient to provide a solids-free-gas outlet velocity in the range of 52 feet per second to 200 feet per second, the ratio of said solids-free-gas cross-sectional outlet area (O) to said separator cross-sectional in-let area (I) being in the range of substantially 0/I = 0.4/1 to 1.0/1.0, and the distance (L) between said gas outlet means and a solids outlet being related to the diameter (D) of the upper barrel portion of the cyclone separator in an amount such that L/D = 4.49-1.09 (O/I).
The invention also provides a method for removal of entrained solids from gases in an upright cyclone separator ~ - 3 -1~ ~7~)34 comprising an upper cylindrical barrel portion with a diameter (D) and having an inlet with a cross-sectional area (I), a solids-free-gas outlet with a cross-sectional area (O), with the ratio O/I in the range of 0.4/1 to 1/1, and a solids outlet at a vertical distance (L) below the solids-free-gas outlet D with the ratio L/0 about 4, said method comprising: injecting gases with entrained solids in the inlet at a speed in the range of substantially 52 feet per second to 80 feet per second;
spinning the injected gases with the entrained solids around and down the cyclone separator to the solids outlet; and ejecting resultant solids-free-gases through the gas outlet at a speed in the range of substantially 52 ~eet per second to 200 feet per second.
The present invention relies on the unexpected finding that by controlling certain geometrical parameters in the design and construction of cyclone separators, the latter can be made much more efficient and wearing of the internal surfaces due to erosion can be greatly reduced. A cyclone separator of one embodiment of the present invention comprises an upper, generally cylindrical barrel portion having a top wall, and a lower, generally conic portion having a solids outlet at the smaller diameter, lower end thereof. The lower, open end of the barrel portion and the conic portion, at its larger diameter end, are adjoined and together define a separation chamber. The barrel portion is provided with a gas inlet for introducing a gas stream tangentially into the separation chamber. A gas outlet tube, which in the preferred case is generally centrally, vertically disposed, extends through the top wall of the barrel portion and has a lower end terminating internally of the separation chamber. A generally cylindrical, solids discharge ~ - 4 -~7~34 dipleg conduit has an upper end in open communication with the solids outlet whereby disentrained solids can be removed from the separator. The usually rectangular, cross-sectional area, "I", of the gas inlet is sufficient to provide a gas inlet velocity of about 80 ft/sec or less whereas the cross-sectional area, "O", of the gas outlet tube is sufficient to provide a gas outlet velocity of about 178 ft/sec or less. The ratio O/I
is maintained in the range of from about 0.4/1 to about 1/1.
The ratio of the distance, "L", between the solids-free-gas out-let at the lower end of the gas outlet tube and the solidsoutlet at the upper end of the dipleg conduit, to the internal diameter, D - 4a -~ ~ 7 O 3 4 ~"D", of the barrel portion of the separator is such as to ~satisfy the equation:
j L/D = -1.09 (O/I) + 4.49.
IlMost preferably, the cyclone is designed such that the ratio I!L/D is about 4Ø
In a preferred embodiment, the cyclone is provided ¦with a dust bowl which provides communication between the upper ¦¦end of the dipleg conduit and the solids outlet formed in the ¦llower conic portion of the separator. It has been found that 'lla cyclone separator, designed in accordance with the above ! parameters, functions most effectively in removing solids, e.g. catalyst particulates from gas streams such as hydrocarbons or flue gases, particularly those used in FCCU.
.15 BRIEF DESCRIPTION OF THE DRAWINGS
Fig. 1 is an elevational view showing, schematically, a typical arrangement of a regenerator used in a FCCU and in-corporating the cyclone separators of the present invention.
Fig. 2 is a partial, elevational view, similar to Fig. 1, but showing in greater detail the unique construction ¦of the cyclone separators of the present invention.
¦ Fig. 3 is a view, partially reduced in size, taken long the lines 3-3 of Fig. 2.
¦ DESCRIPTION OF THE PREFERRED E~BODIMENTS
While the invention will be described with particular -eference to the use of the cyclone separators of the present vention in removing entrained catalyst particle~ from combustion _5_ ~ ~7~34 gases leaving a regenerator used in a FCCU, it is to be understood that the cyclones disclosed and claimed herein find utility in any system wherein a cyclone separator can be used to separate entrained solids from gaseous streams.
The use of a cyclone separator as a means of removing solids from entrained gases in a regeneration scheme is shown in United States Patent 3,394,076. The regenerator system shown in Figure 1 is substantially the same as that shown in the cited patent. Referring then to Figure 1, the regenerator~ shown gen-erally as 10, is provided with an inlet conduit 12 through which is fed spent catalyst from a suitable FCCU reactor (not shown).
A dense phase bed 14 having an upper level 16 is maintained in regenerator 10. An oxygen containing gas, for example, air, is - introduced into regenerator 10 through a suitable air ring 18.
Coke or other carbonaceous material coated on the catalyst par-ticles in regenerator 10 is burned away by the oxygen in the regeneration gases.
Regenerated catalyst is withdrawn from regenerator 10 through draw-off standpipe 20 and returned for further usage in the reactor section of the FCCU. Combustion gases leaving the dense phase bed at level 16 and entrained catalyst particles pass into the disengaging space 22 in the upper portion of the regenerator 10. The gases pass through a first stage cyclone separator 24 via inlet 26. Solids disengaged in separator 24 are returned to bed 14 in regenerator 10 via dipleg 28. The gases leave cyclone separator 24 via transfer line 30 and enter second or last stage separator 32. Solids disengaged in separator 32 are returned to the catalyst bed via dipleg 34 while the sub-stantially solid-free gas passes from separator 32 via gas ¦discharge conduit 35 into plenum 36 located in the upper portion ¦of regenerator lO. The gases in plenum 36 are vented or otherwise removed from regenerator lO via line 38.
I Turning now to Fig. 2, there is shown, in detail, ~the system depicted schematically in Fig. l. First and second stage cyclone separators 24 and 32, respectively, are disposed in regenerator lO by means of suita~le bracing and supports (not shown). First stage cyclone separator 24 has an upper l cylindrical barrel portion 40 having a top wall 52, the lower 1 end of barrel portion 40 being open. Adjoined to the lower, open end of barrel portion 40 is the upper open, greater diameter end of lower conic portion 42. Barrel portion 40 and conic portion 42 cooperatively define an internal separation chamber.
Adjoined to the lower end of conic portion 42 is a dust bowl, shown generally as 25, dust bowl 25 comprising an upper cy-lindrical barrel section 46 and a lower conic section 48.
Conic section 48 terminates at its lower end, in an outlet which is connected to the upper end of dipleg 28. A gas inlet 26, which is generally rectangular in cross-sectional shape, provides a means for introducing a gas stream tangentially into the barrel portion 40 of cyclone 24. A gas outlet tube 50 extends through the top wall 52 of cyclone 24.
Gas outlet tube 50 communicates with gas transfer conduit 30 which in turn is in open communication with a rectangular gas inlet 54 in second stage separator 32. Second stage separator 32 has an upper cylindrical barrel portion 56 with a top wall 72 and an open, lower end, and a lower conic portion 58 with an upper, open end. The lower end of barrel 7(~34 ;
:' .
portion 56 and the upper end of conic portion 58 are adjoined and together define a separation chamber 6 a . Conic section 58, at its lower end, defines a circular solids outlet 62 which lis in open communication with dust bowl 33. Dust bowl 33, ¦¦like dust bowl 25, is comprised basically of an upper cylindri-¦cal barrel section 64 and a lower conic section 66, the junction of barrel section 64 and conic section 66 lying in a plane which passes substantially through the apex, shown as 68, of the projection (shown in phantom lines) of the conic portion 58 ¦ of separator 32. The lower conic section 66 of dust bowl 33 is in open communication with the upper end 70 of cylindrical dipleg 34.
Gas outlet tube 35 extends through the top wall 72 of cylindrical barrel portion 56, gas outlet tube 35 having a lower end 74 terminating in separation chamber 60. Gas out-let tube 35 has an upper open end 76 in communication with the interior of plenum 36. Plenum 36 is defined by a portion of the upper interior wall of regenerator 10, a cylindrical wall 78 ffixed to the upper, inner wall of regenerator 10, and a domed shaped bottom wall 80, affixed at its periphery to the lower end of cylindrical wall 78.
In operation, gas from disengaging space 22 enters rectangular gas inlet 26 of separator 24 and is introduced tangentially into the barrel portion 40. Solid particles, because of their inertia, move toward the walls of separator ¦ 24 and generally spiral downwardly toward dust bowl 25, being ¦ultimately discharged through dipleg 28 into the dense phase : ¦in regenerator 10. The gas, at least partially free of solids, passes upwardly through the central gas outlet tube 50 into transfer conduit 30. The gas then enters second stage cyclone jl 32 via rectangular inlet 54, the gas being introduced tan-l gentially into the part of separation chamber 60 defined by the barrel portion 56 of separator 32~ Solids once again move to the walls of the separator 32, spiral downwardly into dust ¦bowl 33, and return to regenerator 10 via dipleg 34. The substantially solid-free gas passes upwardly through the lower lend 74 of gas outlet tub 35 and is discharged through the upper iend 76 into plenum 36.
¦ It has been unexpectedly found that, particularly ~in the case of the last stage cyclone separator 32, or if more than two stages are used, the last several stages, if certain parameters, with regard to the geometry of the cyclone separator are adhered to, enhanced efficiency and reduced wearing due to erosion result. Thus, for example, it is necessary that the gas inlet, as for example, inlet 54, have a cross-sectional area, "I", which is sufficient to provide a gas inlet velocity of about 80 ft/sec or less~ and preferably a gas inlet velocity ¦of from about 52 to about 80ft/sec. Additionally, it is nec-essary that the gas outlet tube 35 have a cross-sectional area, "O", sufficient to provide a gas outlet velocity of about 178 ft/sec or less. It is also necessary, to achieve optimum efficiency and maximum reduction in wear due to erosion! that ~ertain relationships between the cross-sectional areas "I" and 'O" be maintained. Thus it has been found that the ratio O/I
should be in the range of from about 0.4/1 to about 1/1, and ¦
?referably from about 0.6/1 to about 0.45/1. Lastly, it is _9_ necessary for the cyclone separator of the present invention be designed such that the ratio of the distance, shown as L, between the solids-free-gas outlet at the lower end of outlet tube 35 and the solids outlet at the upper end of dipleg conduit 34 to the internal diameter, shown as D, of the barrel portion 56 of cyclone separator 32 be such as to satisfy the equation:
L/D = -1.09 (O/I) + 4.49.
Most preferably, for minimizing erosion of the cyclone internals by impinging catalyst, the ratio L/D is about 4Ø Cyclone separators designed in accordance with the above critical para-meters exhibit maximum efficiency and minimum wear due to erosion.
In addition to the above parameters, it has also been found desirable that the diameter of the upper end of the dipleg conduit, i.e. conduit 34, be from about 0.05 D to about 0.2 D.
Additionally, and as pointed out above, in cases where a dust bowl such as 33 is employed it is desirable that the apex of the projection of the lower conic portion of the cyclone separator lie in a plane passing substantially through the junction of the barrel section and the conic section of the dust bowl. It is also possible that the diameter of the dust bowl and the diameter of the dipleg conduit be substantially the same.
It is further desirable that there be a solids entrance means 62 to a dust bowl 33 in said cyclone separator having a diameter D62 relative to the diameter (D) of the upper barrel portion D60 in the range of substantially 0.2D to 0.8D.
As used herein, the term "diameter(s)" refers to the internal diameter(s). It will be understood that, generally speaking, the cyclone separator of the present invention will be disposed in a generally vertical position. However, it is within the scope of the invention for the cyclone separators of the present invention to be disposed off-vertical.
The invention may be embodied in other specific forms without departing from the spirir or essential ,characteristics thereof. The present embodiments are S therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being in-. dicated by the appended claims rather than by the foregoing description, and all changes which would come within the meaning and range of the equivalence of the claims are ~therefore intended to be embraced therein.
Claims (12)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A cyclone separator comprising an upper barrel portion having an inlet means and a solids-free-gas outlet means wherein, (a) said separator inlet means having a cross-sectional inlet area (I) sufficient to provide a gas inlet velocity in the range of 52 feet per second to 80 feet per second, (b) said solids-free-gas outlet means having a cross-sectional outlet area (O) sufficient to provide a solids-free-gas outlet velocity in the range of 52 feet per second to 200 feet per second, (c) the ratio of said solids-free-gas cross-sectional outlet area (O) to said separator cross-sectional inlet area (I) being in the range of substantially O/I = 0.4/1 to 1.0/1.0, and (d) the distance (L) between said gas outlet means and a solids outlet being related to the diameter (D) of the upper barrel portion of the cyclone separator in an amount such that L/D = 4.49-1.09 (O/I).
2. A cyclone separator as recited in claim 1 wherein, (a) said separator inlet means is shaped for receiving gases with entrained solids therein at a velocity of substant-ially 80 feet per second and the solids-free-gas outlet means is shaped with a cross-sectional area (O) for ejecting solids-free-gases at a velocity of substantially 178 feet per second.
3. A cyclone separator as recited in claim l wherein, (a) said separator inlet means is rectangularly shaped for receiving the gases with entrained solids therein at a velocity of substantially 80 feet per second and the solids-free-gas outlet means has a cross-sectional outlet area (O) that is circularly shaped to provide a maximum velocity of 178 feet per second.
4. A cyclone separator as recited in claim 1 wherein, (a) said ratio of said gas outlet area (O) to said separator inlet area (I) being in the range of substantially O/I = 0.45/1 to 0.6/1.
5. A cyclone separator as recited in claim 1 wherein, (a) a solids entrance means to a dust bowl in said cyclone separator has a diameter relative to the diameter (D) of the upper barrel portion in the range of substantially 0.2D to 0.8D.
6. A cyclone separator as recited in claim 1 wherein, (a) said solids-free-gas outlet means has a diameter relative to the diameter (D) of the upper barrel portion in the range of substnatially 0.05D to 0.2D.
7. A cyclone separator as recited in claim 1 wherein, the ratio L/D = substantially 4.
8. A method for removal of entrained solids from gases in an upright cyclone separator comprising an upper cylindrical barrel portion with a diameter (D) and having an inlet with a cross-sectional area (I), a solids-free-gas outlet with a cross-sectional area (O), with the ratio O/I in the range of 0.4/1 to 1/1, and a solids outlet at a vertical distance (L) below the solids-free-gas outlet with the ratio L/D about 4, said method comprising:
(a) injecting gases with entrained solids in the inlet at a speed in the range of substantially 52 feet per second to 80 feet per second;
(b) spinning the injected gases with the entrained solids around and down the cyclone separator to the solids outlet; and (c) ejecting resultant solids-free-gases through the gas outlet at a speed in the range of substantially 52 feet per second to 200 feet per second.
(a) injecting gases with entrained solids in the inlet at a speed in the range of substantially 52 feet per second to 80 feet per second;
(b) spinning the injected gases with the entrained solids around and down the cyclone separator to the solids outlet; and (c) ejecting resultant solids-free-gases through the gas outlet at a speed in the range of substantially 52 feet per second to 200 feet per second.
9. A method as recited in claim 8 wherein the first method step comprises further, (a) injecting the gases with the entrained solids into the cyclone separator inlet at a speed of substantially 80 feet per second (24 m/s).
10. A method as recited in claim 8 wherein the third method step comprises further, (a) ejecting the solids-free-gases through the gas outlet at a speed of substantially 178 feet per second (54 m/s).
11. A method as recited in claim 8 wherein the third method step comprises further, (a) ejecting the solids-free-gases through the gas outlet wherein the cross-sectional area (O) of the gas outlet is related to the gas inlet cross-sectional area (I) such that the ratio O/I is in the range of substantially 0.45/1 to 0.6/1.
12. A method as recited in claim 8 wherein the second method step comprises further, (a) spinning the injected gases with the entrained solids around and down from the cyclone separator cylindrical upper barrel portion having a diameter D to the solids outlet having a diameter substantially in the range of 0.05D to 0.2D.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US86505177A | 1977-12-27 | 1977-12-27 | |
| US865,051 | 1977-12-27 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1117034A true CA1117034A (en) | 1982-01-26 |
Family
ID=25344609
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000314179A Expired CA1117034A (en) | 1977-12-27 | 1978-10-25 | Cyclone separator |
Country Status (4)
| Country | Link |
|---|---|
| CA (1) | CA1117034A (en) |
| DE (1) | DE2849201A1 (en) |
| GB (1) | GB2011285B (en) |
| ZA (1) | ZA786322B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL8720219A (en) * | 1986-04-23 | 1989-01-02 | Carroll Noel | CYCLONE SEPARATOR. |
| DE4136935C2 (en) * | 1991-11-11 | 1994-10-06 | Rheinische Braunkohlenw Ag | Cyclone separator |
-
1978
- 1978-10-25 CA CA000314179A patent/CA1117034A/en not_active Expired
- 1978-11-09 ZA ZA786322A patent/ZA786322B/en unknown
- 1978-11-10 GB GB7844067A patent/GB2011285B/en not_active Expired
- 1978-11-13 DE DE19782849201 patent/DE2849201A1/en not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| DE2849201A1 (en) | 1979-07-05 |
| GB2011285B (en) | 1982-04-15 |
| GB2011285A (en) | 1979-07-11 |
| ZA786322B (en) | 1980-03-26 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |