WO1995005893A1 - Mixed phase fixed bed reactor distributor - Google Patents

Mixed phase fixed bed reactor distributor Download PDF

Info

Publication number
WO1995005893A1
WO1995005893A1 PCT/US1994/009287 US9409287W WO9505893A1 WO 1995005893 A1 WO1995005893 A1 WO 1995005893A1 US 9409287 W US9409287 W US 9409287W WO 9505893 A1 WO9505893 A1 WO 9505893A1
Authority
WO
WIPO (PCT)
Prior art keywords
chimneys
tray
spray
conical
vapor
Prior art date
Application number
PCT/US1994/009287
Other languages
French (fr)
Inventor
Robert M. Koros
Yiu W. Wong
John T. Wyatt
David C. Dankworth
Original Assignee
Exxon Research & Engineering Company
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 Exxon Research & Engineering Company filed Critical Exxon Research & Engineering Company
Priority to JP50765195A priority Critical patent/JP3708960B2/en
Priority to CA002170139A priority patent/CA2170139C/en
Priority to EP94926520A priority patent/EP0715544B1/en
Priority to DE69420851T priority patent/DE69420851T2/en
Publication of WO1995005893A1 publication Critical patent/WO1995005893A1/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B05—SPRAYING OR ATOMISING IN GENERAL; APPLYING FLUENT MATERIALS TO SURFACES, IN GENERAL
    • B05B—SPRAYING APPARATUS; ATOMISING APPARATUS; NOZZLES
    • B05B1/00—Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means
    • B05B1/26—Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means with means for mechanically breaking-up or deflecting the jet after discharge, e.g. with fixed deflectors; Breaking-up the discharged liquid or other fluent material by impinging jets
    • B05B1/262—Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means with means for mechanically breaking-up or deflecting the jet after discharge, e.g. with fixed deflectors; Breaking-up the discharged liquid or other fluent material by impinging jets with fixed deflectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00539—Pressure

Definitions

  • the present invention relates to a method and apparatus for uniformly distributing a mixed phase reactant stream on to the surface of a fixed bed of contact material.
  • Another object of the present invention is to provide an improved method and apparatus for distributing a mixed stream of liquid and vapor through a bed of solid catalyst material, which method and apparatus can be utilized both at high liquid mass velo ⁇ cities and low liquid mass velocities.
  • Another object of the present invention is to provide an improved mixed phase distributor means that substantially uniformly distributes mixed phase reactant stream across the top of a contact bed without the stream impinging on intermediate beams and other structures located within the reactor vessel.
  • the present invention provides for the uniform distribution of mixed phase fluid stream onto the top of a contact bed in a reactor chamber by providing a horizontal tray with a plurality of spaced-apart, vertically disposed chimneys extending through the tray. These chimneys have a first end to receive liquid and gas above the tray and a second end for distributing the liquid and gas down ⁇ wardly below the tray. Importantly, the second end is provided with means located below the tray for producing a conical downward spray of the liquid and gas onto the top surface of a bed of contact material positioned below the tray.
  • the means for producing the conical spray are located at positions whereby the spray of liquid and gas, as it impinges on the top surface of the fixed bed, will overlap.
  • the means for producing the conical spray comprises a metallic ribbon wound the form of an inverted conical helix extending from the first end of the chimney.
  • Figure 1 is a schematic longitudinal cross-section illustrat ⁇ ing a two bed reactor embodying a preferred form of the structure according to the invention
  • Figure 2 is an enlarged, partial view showing the structure illustrated in Figure 1;
  • FIGS 3 and 4 are partial views of alternate embodiments of the present invention.
  • the present invention will now be described with particular reference to a reactor having two fixed beds of contact material in which the liquid vapor distribution device of the present invention is positioned between the two beds. It should be readily appreciated, however, that the distribution device of the present invention can be used equally as well with a single bed of contact material reactor or with a reactor having more than two fixed beds of contact material.
  • reactor vessel 10 that has a top inlet 12 for the introduction of mixed phase reactants and a bottom outlet 14 for the removal of product stream.
  • Located in the vessel are two spaced-apart beds 16 and 18 of contact material, typically catalyst particles 1, supported on a horizontally disposed pervious plate 19 and 20, respectively.
  • the distribution device of the present invention is located between beds 16 and 18 and comprises a horizontally disposed tray 22 having a plurality of cylindrical chimneys 24 extending above the plate 22 for receipt of liquid and gaseous material for downward distribution below the plate 22.
  • Means 23 are provided for producing a conical spray of the mixed phases onto the top surface of the fixed bed 18.
  • Each of the chimneys 24 is provided with a cap 26.
  • the chimney 24 has a first end 25 that extends above plate 22 and has a plurality of openings 27 therein for receipt of the gaseous or vapor phase material.
  • the apertures 27 are shown as circular holes; however, any shape opening that is convenient may be employed.
  • the chimney 24 is also provided with a cap 26.
  • a plurality of liquid inlet aper ⁇ tures 28 and 29 are shown as generally vertically slots arranged around the circumference of the chimney 24 and located below the vapor inlets 27 and above the tray 22.
  • the length of slots 28 and 29 are not equal, with slots 28 extending downwardly closer to plate 22 than slots 29. Under high liquid loadings in the reactor vessels, both slots 28 and 29 will serve as inlets for liquid into chimney 24. Under sufficiently low liquid levels on the tray 22, only slot 28 will serve as a liquid inlet.
  • liquid inlet slots may be all of the same length.
  • chimney 24 is provided with a second end 30 for discharge of liquid and vapor downwardly onto the bed 18 located below tray 22.
  • the second end 30 includes means 23 for producing a conical spray, of a fluid and gas, which spray is shown by the dotted lines.
  • the means for producing the conical spray consists of a ribbon in the form of a conical helix having its base facing upward and its apex downwardly.
  • each of the conical helixes is designed to provide sufficient conical spray of liquid and vapor so that the mixed phase from one means 23 as it impinges on the top of the catalyst bed 18 overlaps the spray of mixed phase produced from the next adjacent means 23.
  • cap 26 may be spaced apart from the first end 25 of chimney 24 by any suitable spacing means.
  • a mandrel 33 is posi ⁇ tioned within the second end 30.
  • Mandrel 33 has an outer diameter less than the inner diameter of end 30, defining an annular space therebetween.
  • Mandrel 33 serves to drive the fluids to the inner wall of second end 30 which thereby increases the swirl imparted to the fluids.
  • a plurality of swirl vanes are positioned within chimney 24 for fluids before they enter end 30 for discharge a conical spray produced by means 23 injecting a swirling motion to the mixed phase.
  • each conical spray producing means 23 is designed to produce a spray pattern on the top of the contact bed immediately below the tray sufficient to overlap the spray pattern produced by at least one adjacent spray producing means.
  • the chimneys 24 and hence the spray means 23 are so positioned that substantially none of the spray produced impinges on beams and other structural reactor internals located below tray 22 and above the contact material of bed 18.
  • the maximum flow through the device at acceptable pressure drop and the angle of the spread of the conical spray pattern are controlled by the choice of ribbon pitch, diameter width and length.
  • the angle of the spray and overlap determines the appropriate distance between the tray carrying the spray device and the catalyst bed.
  • Another important feature of the invention is the self- adjusting control of uniform vapor flow through each distribution element. This control is provided by the uniform back pressure due to the pressure drop exerted by the flow of vapor and liquid through the conical spray producing zone in combination with the uniform flow of liquid provided by the chimney slots.
  • fine drop ⁇ lets ranging between 1 micron and 100 microns are produced. These extremely small drops are dispersed and suspended in the vapor flow providing the fixed bed below the tray with a uniform vapor/liquid flow mixture which via normal bed flow dynamics characteristics will be distributed uniformly within the top entrance region of the catalyst bed.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The uniform distribution of mixed phase fluid stream on to the top of a contact bed (18) in a reactor chamber (10) is provided by a horizontal tray (22) with a plurality of spaced-apart vertically disposed chimneys (24) extending through the tray (22). These chimneys (24) have a first end to receive liquid and gas above the tray and a second end (30) for distributing the liquid and gas downwardly below the tray. Importantly, the second end is provided with a spray generating device (23) located below the tray (12) for producing a conical downward spray of the mixed fluid phase onto the top surface of a bed of contact material positioned below the tray (22). The spray generating devices (23) for producing the conical spray are located at positions so that the spray of the mixed fluid stream from one spray generating device as it impinges on the top surface of the fixed bed (18), will overlap the spray from an adjacent spray generating device (23).

Description

MIXED PHASE FIXED BED REACTOR DISTRIBUTOR
FIELD OF THE INVENTION
The present invention relates to a method and apparatus for uniformly distributing a mixed phase reactant stream on to the surface of a fixed bed of contact material.
BACKGROUND OF THE INVENTION
There are numerous petroleum and chemical processes which require uniformly distributing a mixed phase reactant stream with a bed of contact materials, such as catalyst particles. Uniform distri¬ bution is important to assure maximum utilization of the contact material. Various devices have been developed in an attempt to affect more uniform distribution of mixed phase reactant streams. These devices have been employed above the contact bed in a single bed reactor and they have been employed above a plurality of beds in a multi-bed contact reactor.
It is an object of this invention to provide improved distri¬ bution of a mixed phase reactant stream to a fixed bed of contact material .
Another object of the present invention is to provide an improved method and apparatus for distributing a mixed stream of liquid and vapor through a bed of solid catalyst material, which method and apparatus can be utilized both at high liquid mass velo¬ cities and low liquid mass velocities.
Another object of the present invention is to provide an improved mixed phase distributor means that substantially uniformly distributes mixed phase reactant stream across the top of a contact bed without the stream impinging on intermediate beams and other structures located within the reactor vessel.
SUMMARY OF THE INVENTION
Accordingly, the present invention provides for the uniform distribution of mixed phase fluid stream onto the top of a contact bed in a reactor chamber by providing a horizontal tray with a plurality of spaced-apart, vertically disposed chimneys extending through the tray. These chimneys have a first end to receive liquid and gas above the tray and a second end for distributing the liquid and gas down¬ wardly below the tray. Importantly, the second end is provided with means located below the tray for producing a conical downward spray of the liquid and gas onto the top surface of a bed of contact material positioned below the tray. The means for producing the conical spray are located at positions whereby the spray of liquid and gas, as it impinges on the top surface of the fixed bed, will overlap.
In a preferred embodiment of the present invention, the means for producing the conical spray comprises a metallic ribbon wound the form of an inverted conical helix extending from the first end of the chimney.
BRIEF DESCRIPTION OF THE DRAWINGS
The foregoing and other objects and benefits of the invention will be more fully set forth below in connection with the "Detailed Description of the Invention" and in connection with the drawings, in which:
Figure 1 is a schematic longitudinal cross-section illustrat¬ ing a two bed reactor embodying a preferred form of the structure according to the invention;
Figure 2 is an enlarged, partial view showing the structure illustrated in Figure 1; and
Figures 3 and 4 are partial views of alternate embodiments of the present invention.
DETAILED DESCRIPTION OF THE DRAWINGS
The present invention will now be described with particular reference to a reactor having two fixed beds of contact material in which the liquid vapor distribution device of the present invention is positioned between the two beds. It should be readily appreciated, however, that the distribution device of the present invention can be used equally as well with a single bed of contact material reactor or with a reactor having more than two fixed beds of contact material.
Turning now to Figure 1, there is shown reactor vessel 10 that has a top inlet 12 for the introduction of mixed phase reactants and a bottom outlet 14 for the removal of product stream. Located in the vessel are two spaced-apart beds 16 and 18 of contact material, typically catalyst particles 1, supported on a horizontally disposed pervious plate 19 and 20, respectively. The distribution device of the present invention is located between beds 16 and 18 and comprises a horizontally disposed tray 22 having a plurality of cylindrical chimneys 24 extending above the plate 22 for receipt of liquid and gaseous material for downward distribution below the plate 22. Means 23 are provided for producing a conical spray of the mixed phases onto the top surface of the fixed bed 18. Each of the chimneys 24 is provided with a cap 26.
As is shown in Figure 2, the chimney 24 has a first end 25 that extends above plate 22 and has a plurality of openings 27 therein for receipt of the gaseous or vapor phase material. In this particu¬ lar embodiment, the apertures 27 are shown as circular holes; however, any shape opening that is convenient may be employed. The chimney 24 is also provided with a cap 26. Also shown in Figure 2 is a plurality of liquid inlet aper¬ tures 28 and 29. These are shown as generally vertically slots arranged around the circumference of the chimney 24 and located below the vapor inlets 27 and above the tray 22. As is shown in Figure 2, the length of slots 28 and 29 are not equal, with slots 28 extending downwardly closer to plate 22 than slots 29. Under high liquid loadings in the reactor vessels, both slots 28 and 29 will serve as inlets for liquid into chimney 24. Under sufficiently low liquid levels on the tray 22, only slot 28 will serve as a liquid inlet. Optionally, liquid inlet slots may be all of the same length.
As can be seen in Figure 1, chimney 24 is provided with a second end 30 for discharge of liquid and vapor downwardly onto the bed 18 located below tray 22. As shown in greater detail in Figure 2, the second end 30 includes means 23 for producing a conical spray, of a fluid and gas, which spray is shown by the dotted lines. In the embodiment shown in Figure 2, the means for producing the conical spray consists of a ribbon in the form of a conical helix having its base facing upward and its apex downwardly. Importantly, each of the conical helixes is designed to provide sufficient conical spray of liquid and vapor so that the mixed phase from one means 23 as it impinges on the top of the catalyst bed 18 overlaps the spray of mixed phase produced from the next adjacent means 23.
As will be readily appreciated, cap 26 may be spaced apart from the first end 25 of chimney 24 by any suitable spacing means. In the embodiment shown in Figure 3, a mandrel 33 is posi¬ tioned within the second end 30. Mandrel 33 has an outer diameter less than the inner diameter of end 30, defining an annular space therebetween. Mandrel 33 serves to drive the fluids to the inner wall of second end 30 which thereby increases the swirl imparted to the fluids.
In the embodiment shown in Figure 4, a plurality of swirl vanes are positioned within chimney 24 for fluids before they enter end 30 for discharge a conical spray produced by means 23 injecting a swirling motion to the mixed phase.
It is an important feature of the present invention that each conical spray producing means 23 is designed to produce a spray pattern on the top of the contact bed immediately below the tray sufficient to overlap the spray pattern produced by at least one adjacent spray producing means. Thus, the chimneys 24 and hence the spray means 23 are so positioned that substantially none of the spray produced impinges on beams and other structural reactor internals located below tray 22 and above the contact material of bed 18.
The maximum flow through the device at acceptable pressure drop and the angle of the spread of the conical spray pattern are controlled by the choice of ribbon pitch, diameter width and length. The angle of the spray and overlap determines the appropriate distance between the tray carrying the spray device and the catalyst bed. Another important feature of the invention is the self- adjusting control of uniform vapor flow through each distribution element. This control is provided by the uniform back pressure due to the pressure drop exerted by the flow of vapor and liquid through the conical spray producing zone in combination with the uniform flow of liquid provided by the chimney slots. A surprising discovery is that this apparatus operates over wide variations in liquid and vapor flow rates while providing excellent flow distribution performance.
In addition, when in a preferred operating mode, fine drop¬ lets ranging between 1 micron and 100 microns are produced. These extremely small drops are dispersed and suspended in the vapor flow providing the fixed bed below the tray with a uniform vapor/liquid flow mixture which via normal bed flow dynamics characteristics will be distributed uniformly within the top entrance region of the catalyst bed.

Claims

CLAIMS:
1. In a reactor having a flow distributing apparatus therein for distributing a mixed phase fluid stream on the top of a contact bed in the reactor, the improvement comprising:
a horizontally disposed tray located above the top of the contact bed within the reator;
a plurality of spaced-apart, vertically disposed chimneys extending through the tray, the chimneys having a first end to receive a mixed fluid phase above the tray and a second end for downward discharge of the mixed fluid phase below the tray;
means extending downwardly from the second end of the chimneys for producing a conical downward spray of mixed fluid phase onto the top of the contact bed.
2. The improvement of claim 1 wherein the chimneys are spaced-apart relative to each other that downward conical spray from the means for producing the spray of a chimney overlaps the conical spray from the means of at least one adjacent chimney on the top of the contact bed extending downwardly from the second end of the chimney.
3. The improvement of claim 1 wherein the means for producing a conical spray of vapor and liquid metallic ribbon in the comprises a form of an inverted conical helix.
4. The improvement of claim 1 including a mandrel centrally located within the second end of each of the chimneys, the mandrel having an outer diameter less than the inner diameter of the chimney thereby defining an annular space therebetween whereby a swirl is imparted to the vapor and liquid discharged from the chimneys.
5. The improvement of claim 2 including a plurality of swirl vanes located within the chimneys for imparting swirling motion to vapor and liquid therein.
6. A flow distributing apparatus comprising:
a horizontally disposed tray;
vertically disposed chimneys extending through the tray, the chimneys having a first end adapted to receive a vapor and fluid stream and a second end for downward discharge of the vapor and fluid stream below the tray;
means extending downwardly from the second end of the chimneys for producing a conical downward spray fluid.
7. The apparatus of Claim 6 wherein the means extending downwardly from the second end of the chimneys is a metallic ribbon in the form of an inverted conical helix.
PCT/US1994/009287 1993-08-27 1994-08-17 Mixed phase fixed bed reactor distributor WO1995005893A1 (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
JP50765195A JP3708960B2 (en) 1993-08-27 1994-08-17 Distributor for mixed phase fixed bed reactor and reactor having the same inside
CA002170139A CA2170139C (en) 1993-08-27 1994-08-17 Mixed phase fixed bed reactor distributor
EP94926520A EP0715544B1 (en) 1993-08-27 1994-08-17 Mixed phase fixed bed reactor distributor
DE69420851T DE69420851T2 (en) 1993-08-27 1994-08-17 DISTRIBUTOR FOR MIXED PHASES IN A FIXED BED REACTOR

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US08/113,163 US5403561A (en) 1993-08-27 1993-08-27 Mixed phase fixed bed reactor distributor
US08/113,163 1993-08-27

Publications (1)

Publication Number Publication Date
WO1995005893A1 true WO1995005893A1 (en) 1995-03-02

Family

ID=22347906

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1994/009287 WO1995005893A1 (en) 1993-08-27 1994-08-17 Mixed phase fixed bed reactor distributor

Country Status (7)

Country Link
US (1) US5403561A (en)
EP (1) EP0715544B1 (en)
JP (1) JP3708960B2 (en)
CA (1) CA2170139C (en)
DE (1) DE69420851T2 (en)
SG (1) SG49339A1 (en)
WO (1) WO1995005893A1 (en)

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FR2745201A1 (en) * 1996-02-27 1997-08-29 Inst Francais Du Petrole Apparatus to optimise distribution and homogenisation of liquid/gaseous mixture
FR2745202A1 (en) * 1996-02-27 1997-08-29 Inst Francais Du Petrole Distribution plate for homogenisation of gas/liquid polyphase mixture
US7452516B2 (en) 2003-08-18 2008-11-18 Shell Oil Company Distribution device
KR20170119563A (en) * 2016-04-19 2017-10-27 주식회사 엘지화학 Distributor and Down-flow catalytic reactor comprising the same

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US5799877A (en) * 1996-01-03 1998-09-01 Exxon Research And Engineering Company Fluid distribution across a particulate bed
KR100421130B1 (en) * 1996-11-27 2004-06-12 에스케이 주식회사 Chimney tray of reactor
DE50114107D1 (en) * 2000-05-08 2008-08-28 Sulzer Chemtech Ag Column with a bottom between Füllkörperabschnitten
CA2431271C (en) 2000-12-11 2010-11-09 Shell Internationale Research Maatschappij B.V. Multiple bed downflow reactor
US7112312B2 (en) * 2001-04-02 2006-09-26 Tai-Sheng Chou Quench box for a multi-bed, mixed-phase cocurrent downflow fixed-bed reactor
US7506861B2 (en) * 2005-01-21 2009-03-24 Morten Muller Ltd. Aps Distribution device for two-phase concurrent downflow vessels
FR2883200B1 (en) * 2005-03-17 2007-05-11 Inst Francais Du Petrole DEVICE FOR MIXING AND DISTRIBUTING A GAS AND A LIQUID BEFORE A GRANULAR BED
US7523923B2 (en) * 2006-04-18 2009-04-28 Shell Oil Company Fluid distribution tray and method for the distribution of a highly dispersed fluid across a bed of contact material
BRPI0704849B1 (en) * 2007-12-13 2016-03-22 Petróleo Brasileiro S A Petrobras biphasic load distributor nozzle for fixed bed reactors
US20100126621A1 (en) * 2008-11-25 2010-05-27 Mark Van Wees High Velocity Low Impact Liquid Feed Distributor
US8372354B2 (en) * 2010-07-19 2013-02-12 Chevron U.S.A. Inc. Multiphase contact and distribution apparatus for hydroprocessing
FR2978679B1 (en) 2011-08-03 2014-01-17 Total Raffinage Marketing DISPENSER PLATE OF A GAS AND A LIQUID, REACTOR EQUIPPED WITH SUCH A TRAY AND USE OF SAID PLATEAU.
KR101692379B1 (en) * 2014-01-02 2017-01-03 한화케미칼 주식회사 Fluid distributor and multi trickle-bed catalytic reactors with the same
FR3016533B1 (en) 2014-01-21 2016-01-15 IFP Energies Nouvelles DISPENSER PLATE FOR EXCHANGE COLUMN BETWEEN GAS AND LIQUID WITH LIQUID DEFLECTOR
SA118400251B1 (en) * 2018-02-23 2021-12-06 انديان اويل كوربوريشن ليمتد Improved Distribution of A Multi-Phase Fluid Mixture
KR102524372B1 (en) 2019-09-24 2023-04-21 주식회사 엘지화학 Soket type fluid distributing device
EP4200381A1 (en) 2020-08-21 2023-06-28 Shell Internationale Research Maatschappij B.V. Process for hydrotreatment of materials from renewable sources

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2745201A1 (en) * 1996-02-27 1997-08-29 Inst Francais Du Petrole Apparatus to optimise distribution and homogenisation of liquid/gaseous mixture
FR2745202A1 (en) * 1996-02-27 1997-08-29 Inst Francais Du Petrole Distribution plate for homogenisation of gas/liquid polyphase mixture
US5882610A (en) * 1996-02-27 1999-03-16 Institut Francais Du Petrole Device for distributing a multiphase mixture through a catalytic bed
ES2135320A1 (en) * 1996-02-27 1999-10-16 Inst Francais Du Petrole Device for distributing a multiphase mixture through a catalytic bed
ES2135321A1 (en) * 1996-02-27 1999-10-16 Inst Francais Du Petrole Plate for distributing a multiphase mixture through a catalytic bed
US6093373A (en) * 1996-02-27 2000-07-25 Institut Francais Du Petrole Plate for distributing a multiphase mixture through a catalytic bed
US7452516B2 (en) 2003-08-18 2008-11-18 Shell Oil Company Distribution device
KR20170119563A (en) * 2016-04-19 2017-10-27 주식회사 엘지화학 Distributor and Down-flow catalytic reactor comprising the same
KR102071903B1 (en) 2016-04-19 2020-01-31 주식회사 엘지화학 Distributor and Down-flow catalytic reactor comprising the same

Also Published As

Publication number Publication date
CA2170139C (en) 2003-07-01
DE69420851T2 (en) 2000-05-18
JPH09502389A (en) 1997-03-11
EP0715544A4 (en) 1997-07-30
SG49339A1 (en) 1998-05-18
EP0715544B1 (en) 1999-09-22
JP3708960B2 (en) 2005-10-19
DE69420851D1 (en) 1999-10-28
CA2170139A1 (en) 1995-03-02
US5403561A (en) 1995-04-04
EP0715544A1 (en) 1996-06-12

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