[go: up one dir, main page]

EP0360360A2 - Tube séparateur à vortex - Google Patents

Tube séparateur à vortex Download PDF

Info

Publication number
EP0360360A2
EP0360360A2 EP89202391A EP89202391A EP0360360A2 EP 0360360 A2 EP0360360 A2 EP 0360360A2 EP 89202391 A EP89202391 A EP 89202391A EP 89202391 A EP89202391 A EP 89202391A EP 0360360 A2 EP0360360 A2 EP 0360360A2
Authority
EP
European Patent Office
Prior art keywords
swirl
housing
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.)
Granted
Application number
EP89202391A
Other languages
German (de)
English (en)
Other versions
EP0360360A3 (fr
EP0360360B1 (fr
Inventor
Hendrikus Egidius Antonia Van Den Akker
Cornelius Josephus Maria De Kort
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0360360A2 publication Critical patent/EP0360360A2/fr
Publication of EP0360360A3 publication Critical patent/EP0360360A3/fr
Application granted granted Critical
Publication of EP0360360B1 publication Critical patent/EP0360360B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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

Definitions

  • 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 for interconnecting 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 from 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.
  • the ratio of 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 1.
  • the swirl tube separator according to the invention is characterized in that the specific distance 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 3.0.
  • 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.
  • 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 of the frustoconical section 15.
  • the largest inner diameter of the frustoconical section 15 is equal to the inner diameter of the primary section 13 and the smallest inner diameter of the frustoconical section 15 is equal to the inner diameter of the secondary section 17.
  • 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 5.
  • a mixture of gas and solid particles is introduced into the inlet part 3 through 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 20.
  • 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 5.
  • 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 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.
  • Normal operation of the alternative swirl tube separator is similar to normal operation of the swirl tube separator with reference to Figure 1.
  • the function of the vortex stabilizer is to stabilize the vortex in the housing 1 and to delimit the lower end of the vortex.
  • 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.
  • the discharge of solid 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 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 the primary section 13 of the fluid outlet conduit 11 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.
  • statin number is used to refer to the ratio of the tangential component of the mixture velocity to the axial component of the mixture velocity.
  • 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/m3 and the pressure difference between the gas at the inlet part and in the fluid outlet conduit was 1930 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/m3 solid particles having a mean diameter of 14 ⁇ m. As a result it was found that 99.63% of the solid particles was discharged through the solids outlet opening and 0.37% through the fluid outlet conduit.
  • 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/m3 and the pressure difference between the gas at 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/m3 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 solids outlet opening and 0.53% through the fluid outlet conduit.
  • 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/m3 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/m3 solid particles having a mean diameter of 14 ⁇ m. As a result it was found that 99.57% of the solid particles was discharged through the solids outlet opening and 0.43% through the fluid outlet conduit.
  • 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/m3 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/m3 solid particles having a mean diameter of 14 ⁇ m. As a result 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.
  • 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/m3 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 mixture in the swirl zone near the swirl imparting means was 1.73.
  • the mixture contained 0.093 kg/m3 solid particles having a mean diameter of 14 ⁇ m. As a result it was found that 99.53% of the solid particles was discharged through the solids outlet opening and 0.47% through the fluid outlet conduit.
  • 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/m3 and the pressure difference between the gas at the inlet part and at the fluid 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/m3 solid particles having a mean diameter of 14 ⁇ m. As a result it was found that 98.92% of the solid particles was discharged through the solids outlet opening and 1.08% through the fluid outlet conduit.

Landscapes

  • Physics & Mathematics (AREA)
  • Geometry (AREA)
  • Cyclones (AREA)
  • Separating Particles In Gases By Inertia (AREA)
  • Centrifugal Separators (AREA)
EP89202391A 1988-09-22 1989-09-21 Tube séparateur à vortex Expired - Lifetime EP0360360B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8822348 1988-09-22
GB888822348A GB8822348D0 (en) 1988-09-22 1988-09-22 Swirl tube separator

Publications (3)

Publication Number Publication Date
EP0360360A2 true EP0360360A2 (fr) 1990-03-28
EP0360360A3 EP0360360A3 (fr) 1991-01-30
EP0360360B1 EP0360360B1 (fr) 1994-03-16

Family

ID=10644103

Family Applications (1)

Application Number Title Priority Date Filing Date
EP89202391A Expired - Lifetime EP0360360B1 (fr) 1988-09-22 1989-09-21 Tube séparateur à vortex

Country Status (8)

Country Link
EP (1) EP0360360B1 (fr)
JP (1) JP2907458B2 (fr)
KR (1) KR0152963B1 (fr)
AU (1) AU616800B2 (fr)
CA (1) CA1336899C (fr)
DE (1) DE68913882T2 (fr)
ES (1) ES2050785T3 (fr)
GB (1) GB8822348D0 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2326717C2 (ru) * 2002-07-19 2008-06-20 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Сепаратор с вихревой трубой
WO2008145657A1 (fr) * 2007-06-01 2008-12-04 Shell Internationale Research Maatschappij B.V. Séparateur gaz-matières solides
US7648544B2 (en) 2002-07-19 2010-01-19 Shell Oil Company Swirl tube separator
US8025717B2 (en) 2006-08-18 2011-09-27 Shell Oil Company Process to separate particles from a particles-containing gas stream
WO2016156947A1 (fr) * 2015-03-30 2016-10-06 Reliance Industries Limited Séparateur gaz-solide et procédé de séparation gaz-solide
CN112146087A (zh) * 2020-09-17 2020-12-29 北京盛赢节能技术有限公司 一种用于循环流化床换热器的分离器
WO2024047123A1 (fr) * 2022-08-30 2024-03-07 Katholieke Universiteit Leuven Réacteur à effet tourbillonnaire

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0486560U (fr) * 1990-11-30 1992-07-28
US5357816A (en) * 1992-02-07 1994-10-25 Aisin Seiki Kabushiki Kaisha Shock detecting device
JPH05221284A (ja) * 1992-02-14 1993-08-31 Aisin Seiki Co Ltd 衝撃感知装置
US5483846A (en) * 1992-11-02 1996-01-16 Aisin Seiki Kabushiki Kaisha Impact sensing apparatus
JP3625980B2 (ja) * 1997-03-12 2005-03-02 株式会社日立製作所 ガス中の固体成分を分離するサイクロンシステム

Family Cites Families (6)

* Cited by examiner, † Cited by third party
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
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
FI834886L (fi) * 1982-05-07 1983-12-30 Bauer Bros Co Hydrocyklon med vattentroeskel i oeverstroemningskanalen.
US4455220A (en) * 1982-12-23 1984-06-19 Shell Oil Company Separation of fluid cracking catalyst particles from gaseous hydrocarbons

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2326717C2 (ru) * 2002-07-19 2008-06-20 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Сепаратор с вихревой трубой
US7648544B2 (en) 2002-07-19 2010-01-19 Shell Oil Company Swirl tube separator
US8025717B2 (en) 2006-08-18 2011-09-27 Shell Oil Company Process to separate particles from a particles-containing gas stream
WO2008145657A1 (fr) * 2007-06-01 2008-12-04 Shell Internationale Research Maatschappij B.V. Séparateur gaz-matières solides
US8287613B2 (en) 2007-06-01 2012-10-16 Shell Oil Company Gas-solids separator
CN101678370B (zh) * 2007-06-01 2012-12-26 国际壳牌研究有限公司 气固分离器
WO2016156947A1 (fr) * 2015-03-30 2016-10-06 Reliance Industries Limited Séparateur gaz-solide et procédé de séparation gaz-solide
CN112146087A (zh) * 2020-09-17 2020-12-29 北京盛赢节能技术有限公司 一种用于循环流化床换热器的分离器
CN112146087B (zh) * 2020-09-17 2023-02-17 北京盛赢节能技术有限公司 一种用于循环流化床换热器的分离器
WO2024047123A1 (fr) * 2022-08-30 2024-03-07 Katholieke Universiteit Leuven Réacteur à effet tourbillonnaire

Also Published As

Publication number Publication date
EP0360360A3 (fr) 1991-01-30
DE68913882D1 (de) 1994-04-21
ES2050785T3 (es) 1994-06-01
JPH02115056A (ja) 1990-04-27
KR0152963B1 (ko) 1998-10-15
CA1336899C (fr) 1995-09-05
JP2907458B2 (ja) 1999-06-21
KR900004408A (ko) 1990-04-12
AU616800B2 (en) 1991-11-07
EP0360360B1 (fr) 1994-03-16
DE68913882T2 (de) 1994-06-30
AU4159189A (en) 1990-03-29
GB8822348D0 (en) 1988-10-26

Similar Documents

Publication Publication Date Title
EP1385631B1 (fr) Ameliorations apportees a des hydrocyclones
US4711720A (en) Tangentially staged hydrocyclones
US7381235B2 (en) Cyclone separator, liquid collecting box and pressure vessel
US5771844A (en) Cyclone separator having increased gas flow capacity
EP0360360B1 (fr) Tube séparateur à vortex
US6596170B2 (en) Long free vortex cylindrical telescopic separation chamber cyclone apparatus
EP0243044A2 (fr) Hydrocyclone
EP0368849B1 (fr) Separateur cyclone
EP0360357A2 (fr) Appareil pour séparer des particules solides d'un fluide
US5858237A (en) Hydrocyclone for separating immiscible fluids and removing suspended solids
CA1197478A (fr) Cyclones separateurs
CA2215040A1 (fr) Separateur centrifuge et methode de separation des particules et des gaz chauds
US5100552A (en) Cyclone separator with enlarged underflow section
GB2263652A (en) Hydrocyclone
CA2120436A1 (fr) Systeme de flottation
EP0346328B1 (fr) Hydrocyclones
US20040069705A1 (en) Long free vortex, multi-compartment separation chamber cyclone apparatus
US5133861A (en) Hydricyclone separator with turbulence shield
CZ285066B6 (cs) Způsob a zařízení k oddělování alespoň jedné látky z kapalného nebo plynného média
WO1997028903A1 (fr) Separateur a hydrocyclone
CA2235011C (fr) Separateur hydrocyclone
WO1988002280A1 (fr) Separateur cyclonique
EP2571622B1 (fr) Séparateur à cyclone pourvu de deux sorties de gaz et procédé de séparation
WO1997005956A1 (fr) Hydrocyclone
WO1989009653A1 (fr) Separateur cyclone

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): BE DE ES FR GB IT NL

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Kind code of ref document: A3

Designated state(s): BE DE ES FR GB IT NL

17P Request for examination filed

Effective date: 19910611

17Q First examination report despatched

Effective date: 19921204

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE ES FR GB IT NL

REF Corresponds to:

Ref document number: 68913882

Country of ref document: DE

Date of ref document: 19940421

ITF It: translation for a ep patent filed
REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2050785

Country of ref document: ES

Kind code of ref document: T3

ET Fr: translation filed
PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19990830

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19990927

Year of fee payment: 11

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20000930

BERE Be: lapsed

Owner name: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.

Effective date: 20000930

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010401

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee

Effective date: 20010401

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20070926

Year of fee payment: 19

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20070927

Year of fee payment: 19

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20070817

Year of fee payment: 19

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20070814

Year of fee payment: 19

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20070723

Year of fee payment: 19

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20080921

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20090529

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20080921

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20090401

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20080930

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20080922

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20080921

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20080922