AU616800B2 - Swirl tube separator - Google Patents
Swirl tube separator Download PDFInfo
- Publication number
- AU616800B2 AU616800B2 AU41591/89A AU4159189A AU616800B2 AU 616800 B2 AU616800 B2 AU 616800B2 AU 41591/89 A AU41591/89 A AU 41591/89A AU 4159189 A AU4159189 A AU 4159189A AU 616800 B2 AU616800 B2 AU 616800B2
- Authority
- AU
- Australia
- Prior art keywords
- housing
- swirl
- section
- outlet conduit
- fluid outlet
- 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.)
- Ceased
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
- B04C5/08—Vortex chamber constructions
-
- 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
- B04C5/08—Vortex chamber constructions
- B04C5/103—Bodies or members, e.g. bulkheads, guides, in 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
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/08—Vortex chamber constructions
- B04C5/081—Shapes or dimensions
-
- 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
- B04C5/12—Construction of the overflow ducting, e.g. diffusing or spiral exits
- B04C5/13—Construction of the overflow ducting, e.g. diffusing or spiral exits formed as a vortex finder and extending into the vortex chamber; Discharge from vortex finder otherwise than at the top of the cyclone; Devices for controlling the overflow
Landscapes
- Physics & Mathematics (AREA)
- Geometry (AREA)
- Cyclones (AREA)
- Separating Particles In Gases By Inertia (AREA)
- Centrifugal Separators (AREA)
Description
II
S F Ref: 106073 FORM COMMONWEALTH OF AUSTRALIA PATENTS ACT 1952 COMPLETE SPECIFICATION 616800
(ORIGINAL)
FOR OFFICE USE: Class Int Class
S
S
a Complete Specification Lodged: Accepted: Published: Priority: Related Art: Name and Address of Applicant: Address for Service: Shell Internationale Research Maatschappij B.V.
Carel van Bylandtlaan 2596 HR The Hague THE NETHERLANDS Spruson Ferguson, Patent Attorneys Level 33 St Martins Tower, 31 Market Street Sydney, New South Wales, 2000, Australia Complete Specification for the invention entitled: Swirl Tube Separator The following statement is a full description of this invention, including the best method of performing it known to me/us 5845/5
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The present invention relates to a swirl tube separator for the separation of solids from a mixture of fluid and solids.
The separation of solids from a mixture of fluid and solid particles using a swirl tube separator is based on different centrifugal forces acting on the fluid and the solids of the swirling mixture.
USA patent specification No. 2 890 764 discloses a swirl tube separator for separating solids from a mixture of fluid and solids, the separator comprising: a housing having a cylindrical mid section; an inlet opening for the mixture arranged near a first end of the housing; a solids outlet opening arranged near a second end of the housing; a fluid outlet conduit being arranged concentrically within the housing, said outlet conduit comprising a small diameter section, a large diameter section and a frustoconical section ior interconnecting 20 the small diameter section and the large diameter section, the small diameter section having a free end which is in direct fluid communication with the interior of the housing and the large diameter section extending through said first end of the housing; and a swirl zone which extends, when the separator is being used, through the interior of the housing ftom near the inlet opening to a location near the solids outlet opening.
The lower end of the fluid outlet conduit coincides with the lower end of the swirl zone.
As can be seen in Figures 10 and 14 of the prior -2 art document the ratio o; the distance from said free end of the small diameter section of the fluid outlet conduit to the location to which the swirl zone extends and the inner diameter of the cylindrical mid section of the housing is much less than I.
Applicants have now found that the separation efficiency of a swirl tube separator can be improved by selecting a larger ratio between said dimensions.
There is disclosed herein a swirl tube separator for separating solids from a mixture of fluid and solids, the separator comprising: a housing having a cylindrical mid section; an inlet opening for the mixture arranged near a first end of the housing; a solids outlet opening arranged near a second end of the housing; swirl imparting means arranged in an inlet part of the housing, which inlet part is arranged near the first end of the housing; a fluid outlet conduit being arranged concentrically within the housing, said outlet conduit comprising a small diameter section, a large diameter section and a frutoconlcal section for interconnecting 20 the small diameter section and the large diameter section, said sections extending between the swirl imparting means and the solids outlet opening, the small diameter section having a free end which is in direct fluid communication with the interior of the housing and the large diameter section extending through said first end of the housing; and a swirl zone which extends in use of the separator through the interior of the housing from near the inlet opening to a location near the solids outlet opening; characterized in that the specific distance as hereinbefore described from said free end of the small diameter section of the fluid outlet conduit to said location near the solids outlet opening to which the swirl zone extends is between 1.0 and Here the specific distance is referred to as the ratio of the above-mentioned distance to the inner diameter of the cylindrical mid section of the housing.
Hereinafter in the specification and in the claims the expressions "specific distance", "specific length" and "specific inner diameter" are r r i 2A used to refer to the ratio of said distance, length and inner diameter to the inner diameter of the cylindrical mid section of the housing.
The invention will now be described by way of example in more I detail with reference to the accompanying drawings, wherein: I 5 Figure 1, shows schematically a cross-section of the swirl tube i| separator according to the invention; and Figure 2, shows schematically a cross-section of an alternative j swirl tube separator according to the invention.
I
,i ii i .28721 1'I 3 Reference is made to Figure 1. The swirl tube separator comprises a housing 1 having an inlet part 3 at its upper end and a solids outlet opening 5 at its lower end part. The inlet part 3 is in communication with an inlet opening 9.
An open-ended fluid outlet conduit 11 extends concentrically into the housing 1. The lower end of the fluid outlet conduit 11 is arranged between the inlet part 3 and the solids outlet opening 5. The fluid outlet conduit 11 comprises a large diameter section in the form of a primary section 13, a downwardly tapering frustoconical section 15 joined to the lower end of the primary section 13, and a small diameter section in the form of a secondary section 17 joined to the lower end 15 of the frustoconical section 15. The largest inner diameter of the frustoconical section 15 is equal to the inner diameter of the pri ary section 13 and the smallest inner diameter of the frustoconical section is equal to the inner diameter of the secondary section 17.
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ai *aaa* Swirl imparting means in the form of swirl vanes 19 are arranged in the inlet part 3 and between the inner wall of the housing 1 and the outer wall of the primary section 13 of the fluid outlet conduit 11.
A swirl zone 20 extends in the housing 1 between the swirl imparting means in the form of swirl vanes 19 and the solids outlet opening During normal operation a mixture of gas and solid particles is introduced into the inlet part 3 through 30 inlet opening 9. The mixture flows downwardly between the inner wall of the housing 1 and the outer wall of the primary section 13 of the fluid outlet conduit 11, and passes the swirl vanes 19, which swirl vanes 19 impart a swirl to the mixture. The swirling mixture forms a vortex in the swirl zone I_ I
-"II
I
-4- The swirling solid particles in the mixture are flung towards the inner wall of the housing 1 by the centrifugal forces acting on them. At the inner wall of the housing 1 the solid particles flow downwardly by gravitational forces. The solid particles are discharged from the swirl zone 20 through the solids outlet opening The gas in the vortex is withdrawn from the swirl zone 20 through the fluid outlet conduit 11.
The alternative swirl tube separator shown in Figure 2 is additionally provided with a vortex stabilizer 21 arranged at or near the solids outlet opening 5. The vortex stabilizer 21 comprises a vortex stabilizer plate 23 arranged perpendicular to the 15 central longitudinal axis of the housing 1, and a vortex finder rod 25 arranged parallel to the central longitudinal axis of the housing 1 and extending in the :"direction of the fluid outlet conduit 11.
ego•Normal operation of the alternative swirl tube separator is similar to normal operation of the swirl tube separator with reference to Figure i. The function K of the vortex stabilizer is to stabilize the vortex in the housing 1 and to delimit the lower end of the vortex.
S. 25 The inlet part 3 of the housing 1 may alternatively be provided with swirl imparting means in the form of a tangential inlet (not shown).
Normal operation of a swirl tube separator provided with a tangential inlet is similar to normal operation of the swirl tube separator provided with swirl vanes 19.
The swirl tube separator according to the invention is similarly operated when a mixture of liquid and solid particles is introduced into the inlet part 3.
I I i It has been found that the discharge of solid I particles through the fluid outlet conduit can be further reduced by choosing the dimensions of the swirl tube separator according to each of the following specifications: the specific length of the secondary i section 17 of the fluid outlet conduit 11 to be between 0.25 and 1.0, the specific length of the frustoconical section 15 of the fluid outlet conduit 11 to be between 0.20 and 0.30, the specific inner diameter of the secondary section 17 of the fluid outlet conduit 11 to be between 0.20 and 0.40, the specific inner diameter of the primary section 13 of the fluid outlet conduit 11 to be between 0.55 and 0.75, the specific length of *:ebb:the primary section 13 of the fluid outlet conduit 11 15 to be between 1.0 and 1.4, and the specific length of the inlet part 3 to be between 0.50 and 0.70.
The following experiments 1-3 have been carried out to illustrate the swirl tube separator according to o the invention.
The expression "swirl number" is used to refer to the ratio of the tangential component of the mixture velocity to the axial component of the mixture velocity.
SgExperiment 1 i 25 The swirl tube separator used in experiment 1 had the following characteristics: specific distance between lower ends of the fluid outlet conduit and the see* 0* swirl zone 2.18, specific length of the secondary 0 section of the fluid outlet conduit 0.57, specific length of the frustoconical section of the fluid outlet conduit 0.26, specific length of the primary section of the fluid outlet conduit 1.21, specific length of the inlet part 0.60, specific inner diameter of the secondary section of the fluid outlet conduit 0.38, 6 6 specific inner diameter of the primary section of the fluid outlet conduit 0.65.
A mixture of gas and solid particles was supplied to the inlet part of the cylindrical housing. The gas 3 had a density of 1.23 kg/m 3 and the pressure difference between the gas at the inlet part and in the fluid i outlet conduit was 1930 Pa. The swirl number of the mixture in the swirl zone near the swirl imparting 3 f! means was 1.73. The mixture contained 0.092 kg/m 3 solid particles having a mean diameter of 14 Am. As a result it was found that 99.63% of the solid particles was discharged through the solids outlet opening and 0.37%
S
.through the fluid outlet conduit.
Experiment 2 15 The swirl tube separator used in experiment 2 had the following characteristics: specific distance between lower ends of the fluid outlet conduit and the swirl zone 2.43, specific length of the secondary section of the fluid outlet conduit 0.31, specific length of the frustoconical section of the fluid outlet conduit 0.26, specific length of the primary section *of the fluid outlet conduit 1.21, specific length of the inlet part 0.60, specific inner diameter of the S c "secondary section of the fluid outlet conduit 0.38, 25 specific inner diameter of the primary section of the 5 fluid outlet conduit 0.65. A mixture of gas and solid particles was supplied to the inlet part of the cylindrical housing. The gas had a density of 1.23 3 j kg/m 3 and the pressure difference between the gas at 30 the inlet part and in the fluid outlet conduit was 2000 Pa. The swirl number of the mixture in the swirl zone near the swirl imparting means was 1.73. The mixture contained 0.092 kg/m 3 solid particles having a mean diameter of 14 m. As a result it was found that 99.47% of the solid particles was discharged through the 7 0 0 00 0** 0 0 0 4 000 S* S
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solids outlet opening and 0.53% through the fluid outlet conduit.
Experiment 3 The swirl tube separator used in experiment 3 had the following characteristics: specific distance between lower ends of the fluid outlet conduit and the swirl zone 1.96, specific length of the secondary section of the fluid outlet conduit 0.78, specific length of the frustoconical section of the fluid outlet conduit 0.26, specific length of the primary section of the fluid outlet conduit 1.21, specific length of the inlet part 0.60, specific inner diameter of the secondary section of the fluid outlet conduit 0.38, specific inner diameter of the primary section of the 15 fluid outlet conduit 0.65.
A mixture of gas and solid particles was supplied to the inlet part of the cylindrical housing. The gas had a density nf 1.23 kg/m 3 and the pressure difference between the gas at the inlet part and in the fluid outlet conduit was 1980 Pa. The swirl number of the mixture in the swirl zone near the swirl imparting means was 1.73. The mixture contained 0.093 kg/m 3 solid particles having a mean diameter of 14 m. As a result it was found that 99.57% of the solid particles was 25 discharged through the solids outlet opening and 0.43% through the fluid outlet conduit.
The following experiments 4-6 have been carried out as comparison.
Experiment 4 The swirl cube separator used in experiment 4 had the following characteristics: specific distance between lower ends of the fluid outlet conduit and the swirl zone 1.53, specific length of the secondary section of the fluid outlet conduit 1.21, specific length of the frustoconical section of the fluid outlet a /:3 t i 5555
S
55 5
S
.55 S S
S
5*S S S. S S S 1_ 1 8 *00000 0 000
S
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S*
0 0 0
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1 0S Fd 0
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0e conduit 0.26, specific length of the primary section of the fluid outlet conduit 1.21, specific length of the inlet part 0.60, specific inner diameter of the secondary section of the fluid outlet conduit 0.38, specific inner diameter of the primary section of the fluid outlet conduit 0.65.
A mixture of gas and solid particles was supplied to the inlet part of the cylindrical housing. The gas had a density of 1.23 kg/m 3 and the pressure difference between the gas at the inlet part and in the fluid outlet conduit was 1920 Pa. The swirl number of the mixture in the swirl zone near the swirl imparting means was 1.73. The mixture contained 0.095 kg/m 3 soliparticles having a mean diameter of 14 Am. As a result 15 it was found that 99.49% of the solid particles was discharged through the solids outlet opening and 0.51% through the fluid outlet conduit.
Experiment The swirl tube separator used in experiment 5 had 20 the following characteristics: specific distance between lower ends of the fluid outlet conduit and the swirl zone 1.86, specific length of the secondary section of the fluid outlet conduit 0.56, specific length of the frustoconical section of the fluid outlet 25 conduit 0.56, specific length of the primary section of the fluid outlet conduit 1.21, specific length of the inlet part 0.60, specific inner diameter of the secondary section of the fluid outlet conduit 0.38, specific inner diameter of the primary section of the fluid outlet conduit 0.65.
A mixture of gas and solid particles was supplied to the inlet part of the cylindrical housing. The gas had a density of 1.23 kg/m 3 and the pressure difference between the gas at the inlet part and in the fluid outlet conduit was 1830 Pa. The swirl number of the ii 1_ x 9 mixture in the swirl zone near the swirl imparting 3 means was 1.73. The mixture contained 0.093 kg/m 3 solid particles having a mean diameter of 14 Am. As a result it was found that 99.53% of the solid particles was Jischarged through the solids outlet opening and 0.47% I through the fluid outlet conduit.
1 Experiment 6 i The swirl tube separator used in experiment 6 had iithe following characteristics: specific distance swirl zone 1.74, specific length of the secondary section of the fluid outlet conduit 1.07, specific length of the frustoconical section of the fluid outlet i conduit 0.26, specific length of the primary section 44 15 of the fluid outlet conduit 1.21, specific length of S. the inlet part 0.60, specific inner diameter of the 4 secondary section of the fluid outlet conduit 0.46, specific inner diameter of the primary section of the c .fluid outlet conduit 0.65.
A mixture of gas and solid particles was supplied to the inlet part of the cylindrical housing. The gas 3 had a density of 1.23 kg/m 3 and the pressure difference 4 between the gas at the inlet part and at the fluid S outlet conduit was 1260 Pa. The swirl number of the mixture in the swirl zone near the swirl imparting means was 1.73. The mixture contained 0.093 kg/m 3 solid particles having a mean diameter of 14 Am. As a result it was found that 98.92% of the solid particles was discharged through the solids outlet opening and 1.08% 4' 30 through the fluid outlet conduit.
Claims (8)
1. A swirl tube separator for separating solids from a mixture of fluid and solids, the separator comprising: a housing having a cylindrical mid section; an inlet opening for the mixture arranged near a first end of the housing; a solids outlet opening arranged near a second end of the housing; swirl imparting means arranged in an inlet part of the housing, which inlet part is arranged near the first end of the housing; a fluid outlet conduit being arranged concentrically within the housing, said outlet conduit comprising a small diameter section, a large diameter section and a frustoconical section for interconnecting the small diameter section and the large diameter section, said sections extending between the swirl imparting means and the solids outlet opening, the small diameter section having a free end which is in direct fluid communication with the interior of the housing and the large diameter section extending through said first end of the housing; and a swirl zone which extends in use of the separator through the 20 interior of the housing from near the inlet opening to a location near the solids outlet opening; characterized in that the specific distance as hereinbefore described from said free end of the small diameter section of the fluid outlet conduit to said location near the solids outlet opening to which the swirl zone extends is between 1.0 and
2. The separator of claim 1 wherein said location near the solids outlet opening to which the swirl zone extends is defined by the location at which a vortex stai2. 1zer is mounted within the housing.
3. The separator of claim 1 wherein the solids outlet opening is formed by a tapered frustoconical end section of the housing and said location to which said swirl zone extends is formed by the downstream end of said t,ustoconical end section of the housing.
4. Swirl tube separator according to any one of claims 1 to 3, wherein the specific length as hereinbefore described of the small diameter section of the fluid outlet conduit is between 0.25 and Swirl tube separator according to any one of claims 1 to 4, /28721 11 wherein the specific length of the frustoconiral section of the fluid outlet conduit is between 0.20 and 0.30.
6. Swirl tube separator according to any one of claims 1 to wherein the specific inner diameter as hereinbefore described of the small diameter section of the fluid outlet conduit is between 0.20 and 0.40.
7. Swirl tube separator according to any one of claims 1 to 6, wherein the specific inner diameter of the large diameter section of the fluid outlet conduit is between 0.55 and 0.75.
8. Swirl tube separator according to any one of claims 1 to 7, wherein the specific length of the large diameter section of the fluid i outlet conduit is between 1.0 and 1.4.
9. Swirl tube separator according to any one of claims 4 to 8, wherein the specific length of the inlet part of the housing is between 0.50 and 0.70. Swirl tube separator according to any one of claims 1 to 9, wherein the largest inner diameter of the frustoconical section is equal to or smaller th n the inner diameter of the large diameter section of the fluid outlet conduit. 20 11. Swirl tube separator substantially as described in the specification with reference to Figures 1 and 2. DATED this TWENTIETH day of AUGUST 1991 SShell Internationale Research Maatschappij B.V. Patent Attorneys for the Applicant SPRUSON FERGUSON E -0 KE R 721 L
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB888822348A GB8822348D0 (en) | 1988-09-22 | 1988-09-22 | Swirl tube separator |
| GB8822348 | 1988-09-22 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU4159189A AU4159189A (en) | 1990-03-29 |
| AU616800B2 true AU616800B2 (en) | 1991-11-07 |
Family
ID=10644103
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU41591/89A Ceased AU616800B2 (en) | 1988-09-22 | 1989-09-20 | Swirl tube separator |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP0360360B1 (en) |
| JP (1) | JP2907458B2 (en) |
| KR (1) | KR0152963B1 (en) |
| AU (1) | AU616800B2 (en) |
| CA (1) | CA1336899C (en) |
| DE (1) | DE68913882T2 (en) |
| ES (1) | ES2050785T3 (en) |
| GB (1) | GB8822348D0 (en) |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0486560U (en) * | 1990-11-30 | 1992-07-28 | ||
| US5357816A (en) * | 1992-02-07 | 1994-10-25 | Aisin Seiki Kabushiki Kaisha | Shock detecting device |
| JPH05221284A (en) * | 1992-02-14 | 1993-08-31 | Aisin Seiki Co Ltd | Impact detecting device |
| US5483846A (en) * | 1992-11-02 | 1996-01-16 | Aisin Seiki Kabushiki Kaisha | Impact sensing apparatus |
| JP3625980B2 (en) * | 1997-03-12 | 2005-03-02 | 株式会社日立製作所 | Cyclone system for separating solid components in gas |
| US7648544B2 (en) | 2002-07-19 | 2010-01-19 | Shell Oil Company | Swirl tube separator |
| MXPA05000719A (en) * | 2002-07-19 | 2005-04-08 | Shell Int Research | Cyclone separator with a vortex extender pin. |
| WO2008020051A1 (en) | 2006-08-18 | 2008-02-21 | Shell Internationale Research Maatschappij B.V. | Process to separate particles from a particles-containing gas stream |
| CN101678370B (en) * | 2007-06-01 | 2012-12-26 | 国际壳牌研究有限公司 | Gas-solids separator |
| WO2016156947A1 (en) * | 2015-03-30 | 2016-10-06 | Reliance Industries Limited | A gas-solid separator and a process for gas-solid separation |
| CN112146087B (en) * | 2020-09-17 | 2023-02-17 | 北京盛赢节能技术有限公司 | Separator for circulating fluidized bed heat exchanger |
| WO2024047123A1 (en) * | 2022-08-30 | 2024-03-07 | Katholieke Universiteit Leuven | Swirl reactor |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3273320A (en) * | 1963-07-15 | 1966-09-20 | Exxon Research Engineering Co | Cyclone separator for high temperature operations |
| US3636682A (en) * | 1968-03-08 | 1972-01-25 | Phillips Petroleum Co | Cyclone separator |
| CA1221659A (en) * | 1982-05-07 | 1987-05-12 | Charles W. Bouchillon | Hydrocyclone featuring hydraulic jump in overflow passage |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2667944A (en) * | 1949-12-10 | 1954-02-02 | Combustion Eng | Cyclone separator |
| US2890764A (en) * | 1953-12-07 | 1959-06-16 | Gerald D Arnold | Method and apparatus for centrifugal separation with uni-directional flow at the point of separation |
| US4455220A (en) * | 1982-12-23 | 1984-06-19 | Shell Oil Company | Separation of fluid cracking catalyst particles from gaseous hydrocarbons |
-
1988
- 1988-09-22 GB GB888822348A patent/GB8822348D0/en active Pending
-
1989
- 1989-09-01 CA CA000610163A patent/CA1336899C/en not_active Expired - Fee Related
- 1989-09-19 KR KR1019890013472A patent/KR0152963B1/en not_active IP Right Cessation
- 1989-09-20 JP JP1244881A patent/JP2907458B2/en not_active Expired - Fee Related
- 1989-09-20 AU AU41591/89A patent/AU616800B2/en not_active Ceased
- 1989-09-21 DE DE68913882T patent/DE68913882T2/en not_active Expired - Fee Related
- 1989-09-21 EP EP89202391A patent/EP0360360B1/en not_active Expired - Lifetime
- 1989-09-21 ES ES89202391T patent/ES2050785T3/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3273320A (en) * | 1963-07-15 | 1966-09-20 | Exxon Research Engineering Co | Cyclone separator for high temperature operations |
| US3636682A (en) * | 1968-03-08 | 1972-01-25 | Phillips Petroleum Co | Cyclone separator |
| CA1221659A (en) * | 1982-05-07 | 1987-05-12 | Charles W. Bouchillon | Hydrocyclone featuring hydraulic jump in overflow passage |
Also Published As
| Publication number | Publication date |
|---|---|
| KR900004408A (en) | 1990-04-12 |
| KR0152963B1 (en) | 1998-10-15 |
| EP0360360A2 (en) | 1990-03-28 |
| AU4159189A (en) | 1990-03-29 |
| EP0360360A3 (en) | 1991-01-30 |
| JPH02115056A (en) | 1990-04-27 |
| DE68913882D1 (en) | 1994-04-21 |
| CA1336899C (en) | 1995-09-05 |
| ES2050785T3 (en) | 1994-06-01 |
| GB8822348D0 (en) | 1988-10-26 |
| JP2907458B2 (en) | 1999-06-21 |
| EP0360360B1 (en) | 1994-03-16 |
| DE68913882T2 (en) | 1994-06-30 |
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