EP0000094A1 - Moving bed radial flow solids-fluid contacting apparatus - Google Patents

Moving bed radial flow solids-fluid contacting apparatus Download PDF

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Publication number
EP0000094A1
EP0000094A1 EP78300023A EP78300023A EP0000094A1 EP 0000094 A1 EP0000094 A1 EP 0000094A1 EP 78300023 A EP78300023 A EP 78300023A EP 78300023 A EP78300023 A EP 78300023A EP 0000094 A1 EP0000094 A1 EP 0000094A1
Authority
EP
European Patent Office
Prior art keywords
particle
screen
collection
retention
volume
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.)
Withdrawn
Application number
EP78300023A
Other languages
German (de)
English (en)
French (fr)
Inventor
Robert Fredrick Millar
Robert Hugh Jensen
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.)
Honeywell UOP LLC
Original Assignee
UOP LLC
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 UOP LLC filed Critical UOP LLC
Publication of EP0000094A1 publication Critical patent/EP0000094A1/en
Withdrawn legal-status Critical Current

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    • 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
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • 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
    • B01J8/0207—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 flow within the bed being predominantly horizontal
    • B01J8/0214—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 flow within the bed being predominantly horizontal in a cylindrical annular shaped bed
    • 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
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/04—Filters; Permeable or porous membranes or plates, e.g. dialysis

Definitions

  • Radial flow fluid-solids contacting apparatus may be used in a wide variety of industrial processes. Examples are the radial flow reactors used in a variety of hydrocarbon conversion processes. These processes include the isomerization of normal paraffins, the dehydrogenation of normal paraffins and the reforming of naphtha boiling range petroleum fractions.
  • a radial flow reactor the various reactants flow along radials extending from the major central axis'of the reactor to its periphery.
  • the present invention is concerned with those reactors in which the reactant flow is inwards. That is, the reactants flow inwards from an annular reactant distribution volume to a cylindrical reactant collection volume.
  • This central reactant collection volume is enclosed within an inner catalyst retention screen, which is commonly referred to as the central pipe (or centerpipe) of the reactor.
  • Radial flow may also be used in other contacting apparatus such as adsorbent chambers and treaters.
  • the invention also applies to a moving bed regenerator for the decarbonization, reduction or halogenation of used catalyst or adsorbents.
  • moving bed as it is used in this specification is. intended to refer to a particulate-containing system in which the particles rest upon one another in a dense bed and the inventory of the bed is gradually replaced through the removal of used particles at the bottom and the addition of fresh or regenerated particles at the top.
  • the present invention is therefore not directed to ebullated or fluidized bed contacting apparatus.
  • Apparatus in accordance with the invention may be used with either vapour or liquid-phase fluids.
  • the particles have been withdrawn from annular beds through a number of centrally located openings at the bottom of the vessel. Centrally located is used in this context to indicate the particle or catalyst withdrawal.conduits are located approximately midway between the two particle retention screens or within the middle 50% of the distance between the screens.
  • the or each outlet conduit was often covered by a cap or inverted cone such as shown in the specification of United States Patents 3,706,536; 3,785,963 and 3,854,887. The reason for utilizing these caps and the central placement of the withdrawal conduit ' s was to promote a uniform withdrawal of particles from all parts of the bed. That is, 'it was hoped this prior art structure would effect the withdrawal of bed particles, from zones adjacent to both the screens,at equal rates.
  • a second undesirable effect which has been observed using the prior art particle withdrawal systems is the accumulation of particle fines caused by the normal movement-induced attrition of the particulate material in a zone of stagnant particles. These fines are.moved into the stagnant zone by the inward vapour flow but are not removed from it, as would occur if this stagnant zone did not exist. Eventually this transport of fines seals a number of the small vapour passageways in the stagnant zone and causes a higher pressure drop across.the bottom of the particle bed than across the top. This in turn distorts the desired. equal flow rate through all parts of the annular particle bed. In a reactor, this results in the actual space velocity being higher at the top of the reactor than at the bottom.
  • This invention seeks to provide a moving bed radial flow solids-fluid contacting apparatus having a minimum of stagnant zones and which lessens the possibility of stagnant zones occurring against the surface of the central pipe of such apparatus during inward vapour flow.
  • a moving bed radial flow solids-fluid contacting apparatus comprises: a vertically oriented outer vessel, a first vertically oriented particle-retaining screen located within the outer vessel to define a fluid distribution volume between the first particle-retaining screen and the outer vessel; a second vertically oriented particle-retaining screen located within the first particle-retaining screen to define therebetween an annular particle retention volume having upper and lower ends, a cylindrical fluid. collection volume located within the second particle-retaining screen; a plurality of particle inlet conduits located in an upper section of the outer vessel and communicating with the upper end of the annular particle retention volume; a fluid inlet means communicating with the fluid distribution volume; a fluid outlet means communicating with the cylindrical fluid collection volume; and, a particle withdrawal means located between the.
  • the particle withdrawal means comprises: a plurality of tubular particle withdrawal conduits distributed in a pattern encircling the second particle retention screen, each particle withdrawal conduit having an unsealed upper end which communicates with the annular particle retention volume; and, a plurality of particle collection scoops, each scoop having an open upper first end which faces the second particle retention screen and a lower second end which is attached to the upper end of a respective one of each of the particle withdrawal conduits, and with each particle collection scoop having a greater cross-sectional area at the upper first end than at the lower second end and- reposing at an angle of from about 5 to 60° with respect to the horizontal.
  • the collection scoops substantially.completely surround the second particle-retaining screen and define an annular vertically-extending passageway for particles entering the scoops.
  • the angle of repose can be from 15 to 45° with respect to the horizontal.
  • FIGURE 1 there is shown a moving bed radial flow reactor.formed in part by an outer vessel 1 and which conforms to a preferred embodiment of the invention.
  • This vessel is a vertically oriented cylinder enclosed by. an upper end section 36 and a lower end section or cap 37.
  • a first or outer catalyst retention screen 2 is also cylindrical in shape, as is an inner or second catalyst retention screen 3. Both of these screens are concentric about the central vertical axis of the reactor.
  • the outer surface of the first screen 2 and the cylindrical inner surface of the outer vessel 1 define an annular fluid or reactant distribution volume 38, into which the reactants flow from an inlet conduit 6.
  • An annular shaped bed 4 of catalyst is retained between the two screens 2 and 3.
  • This catalyst bed is intermittently replenished with fresh catalyst which falls through catalyst inlet conduits 5 and 5'.
  • catalyst inlet conduits 5 and 5' For simplicity only two catalyst inlet conduits are shown; normally at least about eight are used.
  • the uppermost part of .the porous portion of each screen is preferably below the upper inner surface of the vessel, .and the top of the screen 2 is sealed off by an imperforate annular plate 10.
  • the reactants pass inward through the catalyst bed 4 and enter the cylindrical fluid or reactant collection volume within the screen 3.
  • the reactants and reaction products are then removed downwardly from the reactor .through the reactant outlet conduit'7.
  • the top of the reactant collection volume is sealed with a circular cover plate 9.
  • Used catalyst is withdrawn from the reactor through a plurality of catalyst collection scoops represented by scoops 8 and 8'.
  • Each scoop has an open upper end which faces the inner catalyst retention screen 3.
  • the catalyst enters through this upper end and is therefor withdrawn in an annular pattern much closer to the inner screen 3 than the outer screen 2.
  • Each scoop has a lower end connected to a catalyst withdrawal conduit such as 39 and 39'. These conduits encircle the inner screen 3 and pass through the lower end section 37.
  • the catalyst collection scoops and the upper portions of the catalyst withdrawal conduits are filled'with catalyst during operation of the reactor. This description of the preferred application of the invention is not intended to limit the apparatus to use as a reactor.
  • FIGURE 2 a side view of one catalyst collection scoop (here indicated by the numeral 13) is shown in-greater detail.
  • the lower end of the scoop 13 is attached to a catalyst withdrawal conduit 12.
  • This vertical con-. duit extends through an outer wall 11 of the reactor to a series of valves (not shown) or a catalyst collection hopper (not shown) as the case may be.
  • the conduit 12 may directly feed catalyst to another reactor in a "stacked" reactor design.
  • the scoop 13 is positioned such that an opening 41 at the upper end thereof faces the inner catalyst retention screen (here shown as 40) and is adjacent to this screen.
  • the opening 41 therefor faces radially inward of the catalyst bed.
  • the outer catalyst retention screen (here shown as 14) is closer to the lower end of the scoop 13.
  • the scoop 13 is preferably formed by parallel, planar upper and lower imperforate panels, these panels being inclined at an angle "a" to the horizontal as measured from the lower end of the scoop.
  • the sides of the scoop are enclosed by opposing planar side walls.
  • FIGURE 3 the view seen when looking downward at a catalyst collection scoop 13 is presented.
  • This scoop is similar to that shown in FIGURE 2.
  • the lower end of the scoop covers the open upper end of the catalyst withdrawal conduit 12.
  • the upper panel of the scoop has an upper edge 17 which is spaced further from the inner catalyst retention screen 40 than the upper edge 18 of the lower panel.
  • the triangular shaped panels result in the scoop.having a larger cross-sectional area at its upper end than at its lower end.
  • FIGURE 4 illustrates the preferred arcuate shave of the panel edges forming the upper end of a catalyst collection scoop (shown as 19 in this Figure). Again, the lower end of the scoop is positioned to direct catalyst into a withdrawal conduit 20.
  • the upper edges of the panels are once again horizontally staggered to collect catalyst, with an upper edge 21 being positioned further from an inner catalyst retention screen 35 than a lower panel edge 23.
  • the upper edge of the upper panel 22 and the upper edge of the lower panel are arcuate and have a radius of curvature which is related to that of the inner screen 35 such that the.distance measured radially between the inner screen 35 and either upper edge is uniform at all points along each edge (as shown in Figure 4).
  • Figure 4 also shows the use of a scalloped outer catalyst screen 44 adjacent to a cylindrical outer wall 43 of the reactor.
  • FIGURE 5 represents the view seen when looking towards the upper open end of a catalyst collection scoop 13 which is similar to that shown in Figures 2 and 3.
  • the lower end of the scoop 13 is attached to the catalyst withdrawal conduit 12.
  • the edge 17 of the upper panel is connected to the edge 18 of the lower panel by opposing, vertical, imperforate side walls 27 and 27'.
  • the open upper end of the scoop is therefore circumscribed by the elements 17, 18, 27 and 27'.
  • the particulate matter used in the apparatus is preferably a hydrocarbon conversion catalyst, but it may be an adsorbent including activated carbon, a zeolite or an alumina as may be used to treat gas streams for the removal of water, sulphur compounds or halogen- containing chemicals.
  • the particulate material may also be a solid acceptor used for the removal of sulphur oxides from a flue gas stream as disclosed in the specifications cf United States Patents 3,776,854 and 3,832,445.
  • the particulate matter is spherical and has a diameter within the range of 0.15 to 1.25 cm.
  • Catalyst used in the apparatus will preferably comprise an inorganic oxide support, such as alumina or silica, with a catalytically effective amount of a metal or metal oxide.
  • the metal may be one or more chosen from nickel, cobalt, iron, platinum, tin,' palladium, manganese or magnesium.
  • the outer vessel is preferably made of a suitable metal such as carbon or stainless steel, but it may be formed from other materials (including fiber reinforced- plastics) if the conditions, of, for example, temperature and pressure, allow their use.
  • the two particle or catalyst retention screens are preferably fabricated using wedge-shape wire having a cross-section which decreases in the direction that is away from the particle side of the screen. This results in a self cleaning surface such that as any particles, or pieces thereof, which pass from the bed through the openings between the screen wire fall free of the screen on the side remote from the bed.
  • the wedge- shaped wires are aligned vertically to minimize catalyst attrition as the catalyst moves downward during use against the screen.
  • the outer particle retention screen (2 in Figure 1) may be either cylindrical, to provide an annular fluid distribution volume.38, or it may be a scalloped screen as shown at 44 in FIGURE 4.
  • the contact apparatus will be provided with a plurality of particle inlet conduits (5 and 5')which pass through the upper section of the outer vessel and communicate with the top of the bed 4 in the annular particle retention volume formed between the screens.
  • About six to ten inlet conduits are normally adequate to give a proper distribution of the particulate catalyst material across the bed.
  • the retention screens preferably have an imperforate section at the top to provide a seal which prevents any portion of the fluid stream from passing over the particle bed through possible void spaces.
  • the screens may be capped as shown in FIGURE 1 or they may be extended upwards to the inner surface of the vessel.
  • the inlet conduits 5 and 5' will normally be connected to a valve for controlling the rate of particle addition or they may be connected directly to a hopper vessel used to distribute the particles. Alternatively the inlet conduits may be connected to the outlet conduits of vessels (reactors) located above (as in a stacked design).
  • the apparatus comprises a plurality of particle collection scoops which are arranged in a circular pattern around, and adjacent to, the bottom of a central screen pipe, such that the tips of the adjacent scoops are close together, or at least within 15 cm of each other, to form an annular catalyst collection zone which is uniformly disposed about the central pipe.
  • the radial width of this zone preferably is less than 30 centimeters.
  • the distance to the upper edge is less than 10 centimeters and is less than 5 centimeters for distance to the lower edge when arcuate scoops are used.
  • the straight edge scoops such as shown in FIGURE 3, will result in a zone of varying radial distance.
  • the upper and lower edges of the scoop panels are arcuate and conform closely to the curvature of the central pipe to present a uniform distance between the scoop and the central pipe.
  • Other edge shapes may also be employed if desired.
  • the individual scoops are of hollow form. That is, they are not solid but have a void interior space which conforms to their outer shape.
  • the upper and lower panels and side walls which define the scoops and enclose the interior void are imperforate.
  • These elements of the scoops may be relatively porous, however, so as to provide for drainage or vapour circulation. This may be desired in some cases to prevent coking or the entrapment of liquids in the particle withdrawal conduits.
  • the cross-sectional area of the interior of each scoop is larger at the upper end, which faces the central pipe, than at the lower end, which is attached to the particle withdrawal conduit.
  • the scoops are in this regard funnel-like particle collectors. To aid in the collection of the particles, the lower edge of the scoop (the upper horizontal edge of the lower panel) is located closer to the central pipe than the upper edge (see FIGURES 2, 3 and 4.)
  • the particle collection scoops, or catalyst.collection scoops if the apparatus is used as a reactor, are inclined at an angle of from about 5-60° above horizontal. This is indicated as the angle "a" in FIGURE 2. A preferred range for this angle "a” is from 15-45°, with 30° being particularly preferred. It is preferred that the upper and lower panels of the scoop are parallel and therefore have the same angle to the horizontal. This is not a necessity and the scoops may taper in the cross-section contained in a vertical plane also.
  • the scoops may be surrounded by the same particulate material which is moved through the apparatus, or inert spacers such as ceramic spheres may be placed in the bottom of the vessel. Several supports may be placed around and under the scoops to prevent their movement and distortion during the operation of the apparatus.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP78300023A 1977-06-09 1978-06-07 Moving bed radial flow solids-fluid contacting apparatus Withdrawn EP0000094A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US805062 1977-06-09
US05/805,062 US4110081A (en) 1977-06-09 1977-06-09 Moving-bed radial flow solids-fluid contacting apparatus

Publications (1)

Publication Number Publication Date
EP0000094A1 true EP0000094A1 (en) 1978-12-20

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP78300023A Withdrawn EP0000094A1 (en) 1977-06-09 1978-06-07 Moving bed radial flow solids-fluid contacting apparatus

Country Status (9)

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US (1) US4110081A (nl)
EP (1) EP0000094A1 (nl)
AR (1) AR231083A1 (nl)
BE (1) BE4T1 (nl)
CH (1) CH644032A5 (nl)
DE (1) DE2856949C2 (nl)
FR (1) FR2416726A1 (nl)
GB (1) GB2040718B (nl)
NL (1) NL190054C (nl)

Cited By (1)

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WO1995029228A1 (en) * 1994-04-21 1995-11-02 Genetic Therapy, Inc. Bioreactor

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FR2427378A1 (fr) * 1978-05-29 1979-12-28 Inst Francais Du Petrole Appareil pour la conversion d'hydrocarbures
CA1156439A (en) * 1980-07-30 1983-11-08 Abraham A. Pegels Moving catalyst bed reactor treating hydrocarbons
US4478793A (en) * 1982-09-22 1984-10-23 Uop Inc. Radial flow reactor with operating temperature profile
US4567023A (en) * 1984-02-27 1986-01-28 Uop Inc. Multiple-stage reactor system for a moving catalyst bed
DE3510671A1 (de) * 1985-03-23 1986-09-25 Kernforschungsanlage Jülich GmbH, 5170 Jülich Verfahren und vorrichtung zur durchfuehrung adsorptiver und/oder katalytischer reaktionen
US4976934A (en) * 1985-05-03 1990-12-11 Battelle Development Corporation Nested, recirculating-fiber filter
US4840731A (en) * 1985-06-18 1989-06-20 Morris Sheikh Apparaus for reduction of COD in water
GB8627897D0 (en) * 1986-11-21 1986-12-31 Shell Int Research Reactor
US5209908A (en) * 1989-09-25 1993-05-11 Uop Radial flow reactor with double perforated scallops
US5366704A (en) * 1989-09-25 1994-11-22 Uop Radial flow reactor with double perforated scallops
EP0484534A4 (en) * 1990-05-22 1993-01-07 Lev Zalmanovich Astanovsky Apparatus for carrying out a catalytic process in a fluidized bed
US5258563A (en) * 1992-06-11 1993-11-02 Uop Process for the production of benzene from light hydrocarbons
US5597489A (en) * 1995-03-02 1997-01-28 Sepragen Corporation Method for removing contaminants from water
US5525312A (en) * 1995-03-14 1996-06-11 Chevron U.S.A. Inc. Sleeve for preventing catalyst loss through a reactor ratcheted centerpipe
US6224838B1 (en) * 1999-06-07 2001-05-01 Uop Llc Scallop design for radial flow reactor internals
GB9922940D0 (en) * 1999-09-29 1999-12-01 Ici Plc Catalytic reactor
US6814857B1 (en) * 2002-01-31 2004-11-09 Uop Llc Method for passing a fluid through a moving bed of particles
US6907918B2 (en) * 2002-02-13 2005-06-21 Thermal Corp. Deformable end cap for heat pipe
US7169297B2 (en) * 2002-07-15 2007-01-30 Magnesium Elektron, Inc. pH adjuster-based system for treating liquids
US7442310B2 (en) * 2002-07-15 2008-10-28 Magnesium Elektron, Inc. Treating liquids with pH adjuster-based system
US20050077246A1 (en) * 2002-07-15 2005-04-14 Pardini James J. Treatment of liquid using porous polymer containment member
US7780928B2 (en) * 2007-10-29 2010-08-24 Leon Yuan Method and apparatus for improving radial flow moving bed regeneration/reaction system performance
US20150224464A1 (en) * 2014-02-13 2015-08-13 Uop Llc Radial flow reactor having a side inlet nozzle and methods for reacting hydrocarbons using the same
FR3033266B1 (fr) * 2015-03-05 2017-03-03 Ifp Energies Now Ensemble de collecte d'un fluide gazeux pour reacteur radial
CN107429171A (zh) 2015-03-31 2017-12-01 环球油品公司 用于集成异构化和铂重整工艺过程的方法和装置
CN110214048B (zh) 2017-02-16 2023-06-06 埃克森美孚技术与工程公司 用于轻质链烷烃转化的固定床径流式反应器
EP3622039A1 (en) * 2017-05-10 2020-03-18 SABIC Global Technologies B.V. Process for catalytic cracking of naphtha using radial flow moving bed reactor system
WO2020049372A1 (en) * 2018-09-06 2020-03-12 Sabic Global Technologies B.V. Process for catalytic cracking of naphtha using multi-stage radial flow moving bed reactor system
CN117225298B (zh) * 2023-11-09 2024-03-22 北京拓川科研设备股份有限公司 一种基于移动床反应器的固态原料投放系统

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US3785963A (en) * 1971-11-18 1974-01-15 Universal Oil Prod Co Uniform solids withdrawal system

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US3785963A (en) * 1971-11-18 1974-01-15 Universal Oil Prod Co Uniform solids withdrawal system

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1995029228A1 (en) * 1994-04-21 1995-11-02 Genetic Therapy, Inc. Bioreactor

Also Published As

Publication number Publication date
NL190054C (nl) 1993-10-18
GB2040718B (en) 1982-06-03
BE4T1 (fr) 1979-12-07
US4110081A (en) 1978-08-29
DE2856949A1 (de) 1980-01-03
CH644032A5 (de) 1984-07-13
AR231083A1 (es) 1984-09-28
FR2416726B1 (nl) 1983-03-11
NL7815001A (nl) 1979-07-31
DE2856949C2 (de) 1983-12-15
FR2416726A1 (fr) 1979-09-07
GB2040718A (en) 1980-09-03
NL190054B (nl) 1993-05-17

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