US3218249A - Vapor-liquid distribution method and apparatus for the conversion of hydrocarbons - Google Patents

Vapor-liquid distribution method and apparatus for the conversion of hydrocarbons Download PDF

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Publication number
US3218249A
US3218249A US355870A US35587064A US3218249A US 3218249 A US3218249 A US 3218249A US 355870 A US355870 A US 355870A US 35587064 A US35587064 A US 35587064A US 3218249 A US3218249 A US 3218249A
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Prior art keywords
liquid
vapor
tray
vessel
bed
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US355870A
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John H Ballard
Jr John E Hines
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Union Oil Company of California
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Union Oil Company of California
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Priority to US355870A priority Critical patent/US3218249A/en
Priority to FR9046A priority patent/FR1435218A/fr
Priority to NL656503278A priority patent/NL144836B/xx
Priority to DE1965U0011576 priority patent/DE1542513A1/de
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/30—Particle separators, e.g. dust precipitators, using loose filtering material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/16—Fractionating columns in which vapour bubbles through liquid
    • B01D3/18—Fractionating columns in which vapour bubbles through liquid with horizontal bubble plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/16—Fractionating columns in which vapour bubbles through liquid
    • B01D3/18—Fractionating columns in which vapour bubbles through liquid with horizontal bubble plates
    • B01D3/20—Bubble caps; Risers for vapour; Discharge pipes for liquid
    • B01D3/205—Bubble caps
    • 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
    • B01J8/0278—Feeding reactive fluids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/002—Apparatus for fixed bed hydrotreatment processes

Definitions

  • This invention relates generally to means and methods for distributing a vapor-liquid mixed phase feed to a contacting zone in a reactor or cont-actor, and to means and methods for effecting heat exchange between vapor and liquid phase in a contacting vessel. More particularly, the invention relates to a new and improved method and apparatus for uniform-1y distributing mixed phases to a granular solids contacting zone in a downfiow catalytic contactor such as a hydrodesulfurization, hydrocracking, or other catalytic reactor.
  • a downfiow catalytic contactor such as a hydrodesulfurization, hydrocracking, or other catalytic reactor.
  • One embodiment of the feed distribution means of this invention comprises a substantially horizontal distribution tray mounted above a contacting Zone in a reactor or equivalent contacting vessel, said tray having cap and downcomer or conduit means through which the vapor and liquid feed materials are distributed onto a bed of contact material or to a subsequent contacting zone below.
  • the cap and downcomer conduit means may resemble, in size and arrangement, bubble caps of the type commonly used in distillation columns, but they serve a far different function in our invention that do distillation bubble caps.
  • a vapor-liquid mixed phase feed is introduced to the distribution tray by means of a sparger, perforated tray or other device whereupon the distribution tray, in turn, causes distribution of the mixed phase feed uniformly over the contacting zone.
  • outlet nipples are V-notched to facilitate more even overfiow of the liquid, the use of such V-notches (or serrations, slits, etc) being quite common in the art.
  • the vapor constituent of the feed mixture is forced through the outlet nipples and then through the bed of contact material by the operating pressure drops within the reactor.
  • our vapor-liquid distribution method is an effective heat transfer device.
  • a quench gas is fed to the inlet of a contacting Zone together with hot material entering the zone
  • an interchange of heat between the cold quench gas and hot feed is required so that the vapor and liquid portions of the feed approach the same temperature on entering the granular solids contacting Zone. Similar heat exchange would be necessitated if the gas portion was at substantially higher temperatures than the liquid portion of the feed.
  • This heat interchange can be effectively achieved by direct contact of the liquid and the vapor in our distribution device.
  • FIGURE 1 is an elevation view, partly in section, of a reactor incorporating the feed distribution means of this invention
  • FIGURE 2 is an enlarged elevation view, mostly in section, of a cap and downcomer feed conduit according to this invention, taken along line 22 of FIGURE 1;
  • FIGURE 3 is a cross-sectional plan view of the cap and downcomer assembly taken along line 33 of FIG- URE 2;
  • FIGURE 4 is an enlarged partial cross-section of the reactor of FIGURE 1, showing a plan view of one quadrant of the distribution tray with cap and downcomer fittings, taken along line 44 of FIGURE 1;
  • FIGURES 5, 6, and 7 show several cap designs suitable for use in our invention
  • FIGURE 8 is a graph of data showing the levelling effect of our cap and downcomer distribution means on liquid flow rates through individual distribution tray outlets;
  • FIGURE 9 is a graph of data showing the damping effect of our cap and downcomer distribution means on liquid flow rate variations caused by vapor flow fluctuations through downcomers of different heights and the effect of vapor rate on liquid distribution;
  • FIGURE 10 is an elevation view of a portion of a reactor, in cross-section, incorporating another embodiment of a distribution means according to this invention which is particularly adaptable to the inter-mixing of a quench gas with liquid-vapor entering an intermediate contacting zone;
  • FIGURE 11 is a cross-sectional plan view of the quench deck installed above the distribution tray in the embodiment of FIGURE 10 taken along the line 1111 thereof;
  • FIGURE 12 is a plan view of the perforated tray installed above the distribution tray in the embodiment of FIGURE 10 taken along the line 1212 thereof;
  • FIGURE 13 shows the detail of another embodiment of a riser found to give superior distribution of the liquid portion of the feed.
  • the mixed phase feed distribution method and apparatus of this invention are broadly applicable to any contacting system, and thus to any reactant downflow contacting system, they are particularly useful in catalytic reaction systems.
  • the method and apparatus are specifically applicable for use in catalytic hydrodesulfurization and hydrocracking reactors, but they can also be used to conduct any contacting or treatment in which a portion of the feed is in liquid phase and the balance in vapor phase, such as in catalytic polymerization, isomerization, etc., of petroleum hydrocarbons, catalytic hydrogenation of liquid coal extracts, catalytic hydrogenation of aromatic compounds such as the conversion of benzene to cyclohexane, catalytic oxidation, catalytic chlorination, and the like.
  • the apparatus there shown consists essentially of a reactant downflow catalytic reactor with its various internal parts.
  • Cylindrical vessel 2 having a top 4 and a bottom 6, is usually constructed of corrosion resistant metal or an equivalent material, such as stainless steel, ceramic, or the like, and is normally insulated internally or externally for operation at elevated temperatures. While the outer shell of the reactor is substantially cylindrical in the preferred form of our apparatus, it can also be of a non-cylindrical shape if desired.
  • Outlet conduit 8 is provided in bottom 6.
  • Vessel top 4 is provided with access conduit 10 for convenience in filling vessel 2 with catalyst, and for routine maintenance.
  • a foraminate, cone-shaped cylindrical grating 12, located immediately above outlet conduit 8, is provided as a barrier to prevent escape of the solids within vessel 2 through outlet 8 while at the same time permitting fluid product to discharge therethrough.
  • Feed inlet conduit 14 communicates with a sparger 16 which comprises a closed-end pipe with two identical radial slits 17 in its upper portion, of which only one shows on the drawing, the other being hidden from view.
  • the vapor-liquid feed is introduced into the top of vessel 2 through the slits in the sparger which are so positioned that an end view of the sparger in operation would reveal the feed issuing therefrom in two sheet-like jets, first diverging in a roughly V-shaped pattern and then rapidly disintegrating so that the liquid is somewhat distributed within the vessel. Additional vapor can be introduced into vessel 2 through access conduit 10 if desired.
  • the improvement of our invention comprises a novel feed distribution system which takes the form of a transverse partition, or distribution tray, 18, fitted with caps and downcomers such as shown at 7, 7a, and 7b on the drawing.
  • caps and downcomers such as shown at 7, 7a, and 7b on the drawing.
  • 10 downcomers the number in the center row, as evident from FIGURE 4
  • only 9 are shown, a representative three of which are symbolized as 7, 7a, and 7b on the drawing.
  • Distribution tray 18 is securely mounted substantially horizontally within vessel 2 by a circumferential angle 19 firmly attached to the walls of vessel 2, or by other conventional supports such as angle sections, channels, brackets, welding or the like. Tray 18 is substantially vapor and liquid-tight, except for the downcomer conduit openings.
  • the contacting zone of the reactor in which is disposed a bed of granular catalyst material 102, .under a layer of chemically inert spherical pellets 100.
  • the inert pellets are preferably ceramic balls made of fused alumina or equivalent material interposed between the distributor tray and the catalyst bed, forming a layer, preferably from about 3 to about 6 inches in depth.
  • the chemically inert pellets act to improve the uniformity of distribution of the feed from distribution tray 18 and tend to prevent disruption of the upper surface of the catalyst bed.
  • the character of the material in catalyst bed 102 will depend upon the nature of the reaction taking place in the reactor.
  • a typical catalyst will consist of Ax-inch pelleted cobalt-molybdate hydrodesulfurization catalyst.
  • bed 106 Disposed below catalyst bed 102 is bed 106, which is another bed of inert ceramic spheres, or the like, surrounding and abutting against grating 12.
  • the layer of inert spheres is optional and may be eliminated completely or replaced by an equivalent, or other, volume of catalyst material if desired.
  • reactors suitable for our purpose can differ substantially in non-critical aspects from the FIGURE 1 embodiment.
  • Such reactors can, for example contain two or more distribution tray-catalyst bed combinations, or units, which can be arranged in series or parallel relationship.
  • the catalyst beds in the reactors of this invention have adjacent layers of inert materials such as inert spheres 100 and 106 of FIGURE 1.
  • the catalyst beds, whether or not covered by a layer of inert spheres or the like, may, if desired, have a plurality of foraminate baskets embedded therein in the manner shown in copending US. patent application Serial No. 1,505 to Young et al., which has matured into US. Patent No.
  • the baskets may be filled with inert ceramic particle-form material or not and they serve the purpose of providing more uniform distribution of the mixed phase reaction feeds throughout the catalyst bed while, at the same time, removing foreign matter from the feed materials which might otherwise plug the bed.
  • FIGURES 2 and 3 it will be noted that the downcomer 26 and cap 23 are fastened together by means of a bolt 20, a nut 22, a spacer 23, and a strap 24.
  • Bolt 20 passes through a hole in the center of the end closure 30 of cap 23 and a hole in strap 24 aligned therewith in such fashion as to affix cap 23 in proper spaced relation to downcomer 26.
  • Nut 22 fastens the whole assembly together.
  • Strap 24 is a relatively narrow strip of metal, or other suitable material, fastened diametrically across the upper opening of downcomer 26 by welding or other means.
  • the illustrated arrangement is merely one of the possible ways of fastening the caps and downcomers of this invention together.
  • Downcomer 26 projects through tray 13 and is fastened thereto by welding as indicated at 32, by suitably forming the riser to secure it in position on the tray as shown in FIGURE 13, or by other suitable means.
  • the materials from which all of the parts here involved are made should, for best results, be substantially non-corrosive with respect to the feed and other materials present in the reactor. Preferable materials from which to fabricate such parts are steel, ceramics, plastics, etc.
  • cap 28 can also be left unslotted.
  • the depth of the slots should preferably be from about A; to about A2 of the depth of the cap itself and the width of the slots from about 4 to about /5 of the cap crosssectional diameter.
  • Another even more suitbale operating range of slot widths is from about to about A; of the cap cross-section diameter.
  • All slots are preferably, but not necessarily, of the same size and shape. Other types of slots or notches besides those shown, such as V-notches, can be used if desired. Some typical slots are illustrated in FIGURES 5, 6 and 7.
  • the top of the slot should be maintained below the bottom of the upper rim of the downcomer. Although not essential, good practice would be to maintain a clearance of at least A-inch between the top of the slot and the top of the riser.
  • the top of downcomer 26 can be slotted in the manner shown at 36, or left unslotted, as desired. Any feasible number of such slots can be employed. For example, we have successfully employed two diametrically opposed slots.
  • the downcomer slots can be of any design, it is not necessary that they be more than about /2-inch in depth as their function is merely to restrict the flow of liquid over the rim of the downcomer in order to achieve a balancing of liquid flow.
  • the bottom of the downcomer slots should be maintained above the top of the cap slot.
  • the number of downcomers required for our purpose is variable, and can be the same as, greater than, or fewer than the number of corresponding outlet conduits in distribution trays heretofore known to the art.
  • the liquid discharge from our downcomers is not in discrete thin stream form, but is entrained in the vapor discharge to form a mixture of vapor and liquid which issues from each downcomer in an exit pattern substantially co-extensive in circumference with the downcomer cross-section thereby, with appropriately located downcomers, achieving substantially uniform distribution over a cross-section of the vessel.
  • Another advantage of our invention is the ability by its use to obtain better feed distribution over the surface of the catalyst bed with fewer downcomer conduits than has previously been possible.
  • the optimum number of downcomers for any given purpose will depend on many factors, the most obvious of which is the size of the reactor. Other contributing factors are the feed rate to the reactor and the proportion of the feed remaining in the liquid phase.
  • the design of the distribution tray will provide the proper number of downcomer outlets to assure optimum liquid level on the tray, and concomitant optimization of gas flow through each outlet for a given feed rate and reactor size.
  • the downcomer will be from about 3 to about 6 inches in cross-sectional diameter, although downcomers as small as 1% inches, or less, or larger than 6 inches may be employed.
  • the downcomers It is not necessary that the downcomers extend through the tray and project into the catalyst chamber below as shown in FIGURE 2, but there is no objection to this and in fact such projection is preferable in most instances. Where the downcomers do project in such fashion, however, they should preferably extend only a short distance below the distribution tray. Too great a distance mitigates against good dispersion of the feed onto the catalyst bed surface and too short a distance creates the possibility of liquid migration via the outer peripheries of the downcomer extensions to the under surface of the distribution tray and even to other downcomers before dropping onto the catalyst bed.
  • FIGURE 13 A preferred cap and riser design is shown in FIGURE 13, wherein is seen cap 300 mounted on riser 362.
  • Riser 302, corresponding to riser 26 in FIGURE 2, is formed to provide protruding section 304.
  • Riser 302 is inserted through downcomer hole 306 in tray 18 so that protruding section 304 rests on the tray.
  • Riser 302 is then rolled to form flared section 308 which firmly secures the riser to the tray without welding or other means.
  • the liquid tends to flow down the riser wall, particularly at lower vapor rates, and that flared section 3th; causes the liquid to be disengaged from the riser in a conical pattern thereby achieving greater distribution of the liquid over the cross-section of the vessel.
  • riser 302 The extent to which riser 302 is flared in part determines the flow pattern of the liquid eflluent discharged from the riser.
  • the riser tip may be flared approximately degrees from the axis of the riser so that the riser is rolled against the bottom of tray 18 without loss of effectiveness as a fastening device.
  • optimum flow patterns may not be achieved with such a wide flare. Satisfactory flow patterns can be obtained at flare angles between about 10 degrees and about 70 degrees from the axis of the riser, with a preferred range being between about 20 degrees and about 60 degrees.
  • Angle clips 310 usually three in number, are attached to riser 302 by welding, or other convenient means, and serve as a mounting for cap 300.
  • Holddown clamp 312 is attached to support means 314, which in turn is fastened to angle clips 310.
  • Cap 300 is positioned on riser 302 with holddown clamp 312 being inserted through a slot in the top of cap 300 out therein for that purpose.
  • Cap 300 is fastened in position by a wedge, not shown, which is inserted through slot 316 in holddown clamp 312. Centering lugs 318, more fully described hereafter, maintain cap 300 centered over riser 302.
  • Feed should be introduced to the distribution tray in a more or less uniform manner and without excessive velocity head or impingement on the bubble caps.
  • different types of devices can be installed above the distribution tray to pre-mix the feed and quench gas and to achieve more or less even distribution of the feed and gas to the distribution tray.
  • Such devices which can be used include, but are not limited to, solid staggered partial bafi'les, perforated trays and partially perforated trays.
  • FIGURES 10, 11, and 12 One effective device for pre-mixing and distributing a liquid-vapor influent to a contacting zone and a quench gas is shown in FIGURES 10, 11, and 12.
  • This device is particularly suitable where the liquid-vapor influent is the etfiuent of a contacting zone immediately above passing to a lower contacting zone.
  • the device described herein may thus be installed in the top of a vessel for pre-mixing a quench gas and a vapor-liquid feed to an upper contacting zone, or it may be installed intermediate to two contacting zones within the vessel.
  • a liquid-vapor influent passes downwardly through vessel 200 to contacting zone 102.
  • this material may be either a liquid-vapor feed to vessel 200 or a liquidvapor effluent from a contacting zone above.
  • Quench gas is introduced into an intermediate zone between two adjacent contacting zones at a point in the center of vessel 200 by means of nozzle 202 and internal pipe 204.
  • Quench deck 206 comprises a solid tray across the crosssection of Vessel 200, removably attached to the vessel wall around the periphery of deck 206 by means capable of a substantially leak-free seal.
  • Quench box 210 is positioned immediately below deck 206 and is fixedly attached thereto by welding, or other means.
  • Quench box 210 is usually located concentric to deck 206 and comprises bottom and side members, quench deck 206 serving as a top member to enclose the box.
  • the inlet to box 210 is through conduits 208 and the only outlet is through conduits 212 located in the bottom of box 210 approximately 90 degrees removed from conduits 208.
  • Liquid-vapor influent and quench gas entering the upper section of vessel 200 divide into two streams of more or less similar compositions and flow quanities. Each of these streams passes downwardly through one of conduits 208 into quench box 210.
  • each of the two streams flowing through conduits 208 divide into two streams of approximately equal composition and flow quantities which are combined with a similar portion of the stream passing through opposite conduit 208.
  • FIGURE 11 is a plan view of quench deck 206 showing conduits 208 and, in outline, the location of quench box 210 and conduits 212.
  • FIGURE 11 is a plan view of quench deck 206 showing conduits 208 and, in outline, the location of quench box 210 and conduits 212.
  • the illustrated embodiment employs two quench box inlet openings and two outlet openings, our invention is not so limited. Any number of quench deck openings may be employed, usually located sub-' stantially equidistant from the center axis of the vessel, and spaced substantially equidistant from the center axis.
  • any number of outlet openings may be employed, these openings also being usually located substantially equidistant about the center axis of the vessel and substantially uniformly offset about the center axis from the openings in the quench deck.
  • the purpose of offsetting the outlet openings is so liquid will not pass directly through both the inlet openings and the outlet openings without impinging on the bottom member of the quench box thereby causing a change in flow direction.
  • the embodiment employing two quench deck openings and two quench box outlet openings is preferred because superior distribution is achieved. Should channeling occur above the quench deck, downflowing liquid from any portion of the vessel cross-section is effectively redistributed over the vessel cross-section by passage through the apparatus described above and illustrated in FIGURES 10 and 11.
  • perforated tray 214 extends across the cross-section of vessel 200 below quench deck 206 and quench box 210, and is removably attached to vessel 200 around the periphery of the tray.
  • One orientation of perforations 216 is shown in FIGURE 12, a plan view of tray 214.
  • Tray 214 has perforations 216 uniformly distributed thereover, except in the area im mediately beneath conduits 212 indicated at 230. It should be noted that any convenient orientation, size, shape, and number of perforations may be employed, the particular design to be based on established chemical engineering practices.
  • Tray 214 functions to prevent localized impingement of the downflowing material on distributor tray 18.
  • Distributor tray 18 containing bubble cap and riser assemblies such as those typically illustrated at 7, 7a, and 7b, is located below perforated tray 21.4. Tray 18 is constructed and operated in accordance With the foregoing method and as shown in FIGURES 1, 2, 3, 4, 5, 6, 7, and 13. Other modifications of apparatus can be used to reduce the velocity head of the entering fluid and such devices are within the scope of our invention.
  • the downcomer elevations be as nearly identical as possible to achieve optimum equality of liquid flow therethrough, but considerable variation in elevation is permissible as will presently be shown.
  • the caps over the downcomers i.e., the distribution caps, can vary widely in size and design. However, for most practical purposes the caps should be of cylindrical design with an outside cross-sectional diameter of from about 4 /2 to about 9 inches and a vertical dimension roughly equivalent thereto. It is preferable in some applications to use caps of smaller size, down to about 2 inches or less. It is not necessary, however, that either the downcomers or caps be of cylindrical shape, and they may be of square, rectangular, triangular, or other cross-sectional configuration if desired.
  • the lower rims of the distribution caps can be adjusted to any level above the distribution tray so long as the flow of gas through the downcomers is not sealed off; a reasonable range being from a level corresponding to practically no distance above the tray to a distance of about one foot ther eabove.
  • the liquid on the distribution tray provides a settling zone for the accumulation of sludges, particles of scale and other solid materials present in the system.
  • these sludges be spread as uniformly as possible over the surface of the distribution tray and for this reason it is normally preferable to avoid close tolerances between the tray and the distribution cap rims.
  • FIGURE 4 is a plan view of one quadrant of distribution tray 18 showing the disposition of caps and downcomers thereon.
  • the downcomers are uniformly distributed over the surface of the tray.
  • the illustrated plan is merely representative and there are, of course, many alternative downcomer arrangements.
  • One of the design considerations for tray 18 is that there be sufiicient downcomer conduit area to assure a relatively small pressure drop across the tray.
  • the usual commercial practice is to construct the quench deck, perforated trays and distribution tray with removable sections to permit access to the vessel for catalyst loading and maintenance. The joints thus created, if properly installed, have no effect on the operation of these trays.
  • a mixed phase vapor-liquid feed is introduced into the upper portion thereof through inlet conduit 14 and sparger 16, which distributes the liquid onto tray 18 with a minimum of splashing and erosion.
  • the liquid phase disengaged from the vapor phase by gravity, fills up on tray 18 to a level below the slot depth in the downcomer caps, such level being determined primarily by the gas flow rate per cap. It is, of course, necessary that some of the slot openings be exposed above the liquid surface to permit the passage of vapor therethrough. Where the caps have no slots, the liquid level on the tray will be below the bottom rims of the caps for the same reason. Where unslotted caps are used, clearance between the bottom rim and the tray must be maintained to accommodate the passage of gas and liquid thereunder.
  • the pressure drop through the distribution tray in the reactor which is normally quite small (although operating pressures themselves can vary substantially so long as the vapor phase of the feed remains unliquifled), forces the feed vapor under the downcomer caps, either through the slots are around the bottom rims thereof as indicated above, from whence it flows upwardly through the annulus between the downcomer cap and the downcomer, reverses direction and thence flows downwardly through the downcomers into the contacting zone.
  • the vapor because of the forces acting on it as a result of being fed to the reactor under pressure and then forced into the contacting zone through the tortuous cap and downcomer paths, is in constant turbulence as it contacts the liquid in the reservoir on the distribution tray in the vicinity of the downcomers.
  • the vapor entrains liquid with it as it passes through the cap slots or under the downcomer cap and transports it through the downcomers from whence it is discharged into the contacting zone in the manner hereinbefore described.
  • the liquid on the distribution tray seeks its own equilibrium level, as dictated by the design of the apparatus, and it is thus not necessary for operability to achieve optimum design efficiency of the distribution tray.
  • the reactor will be operative so long as the liquid level on the tray does not seal off all openings in the downcomer caps. As mentioned above, all of the joints on the tray should be sealed so that all of the liquid and vapor passes through the downcomer conduits, except any small controlled quantity of liquid which might flow through weepholes in the tray for the purpose of emptying the tray on shutdown.
  • the feed temperature to a catalytic reactor or other solids contacting zone is frequently cooled by admixture of a cold quench gas with the reactor feed.
  • a cold quench gas In a twophase reactor, the introduction of the cold quench gas results in a tendency for super cooling of the gaseous or vaporous phase and only limited cooling of the liquid.
  • the liquid portion may be substantially higher in temperature than the gaseous portion.
  • our vapor-liquid distribution tray promotes the interchange of heat between the vapor and liquid portions of the feed to the extent that the temperature difference between phases is reduced to at least about 15 percent of its initial value. Further, heat transfer may be elfected in the sparger, in the quench box, on the perforated tray or other feed distribution device, and in the Alundum ball section of the reactor. Thus, overall heat transfer is greater than that obtained by means of the distribution tray alone.
  • Example I This example demonstrates the inequality of liquid flow through outlet nipples of the conventional type, even when special efforts of a kind not incident to the normal fabrication and installation of commercial units are made to avoid nipple irregularities.
  • a 30-inch diameter mockup of a catalytic reactor equipped with a high capacity blower for gas feeding purposes, a pump for liquid circulation, and orifices for flow measurements was employed in carrying out the work of this example.
  • the blower gave a head of 2 psi. at low flow rates, and flow rates as high as 1,300 s.c.f./ min. at zero head.
  • the pump also had a high head and capacity; suitably sized orifice plates were used where necessary in the system. Flow was set by hand using a metering valve.
  • a 30-inch diameter distribution tray having 19 identical distributing risers was constructed and positioned horizontally within the aforesaid mockup.
  • the risers were approximately 6-inch lengths cut from a 3-inch pipe. They were set into the tray, projecting upward, at a spacing of about 6 inches and on an approximate hexagonal layout.
  • the risers each had two As-inch by l-inch sawcuts in the upper rim.
  • the mockup apparatus was set up with the tray level and with the 19 risers carefully adjusted to a uniform elevation. The overall deviation of the risers from level did not exceed -inch, the deviation being even less on adjacent risers. As indicated previously, such an exact installation could not be expected commercially.
  • the two As-inch slots were cut in the risers to aid in giving even more uniform flow rates than would otherwise be possible. At the flow rates tested, which approximated the rates in commercial units, the liquid flowed only through the bottom portions of the slots.
  • the vapor-liquid system tested in this example was an air-water system.
  • the water was introduced onto the distribution tray through a sparger consisting of a 24-inch length of l /z-inch Schedule 40 pipe with many -inch holes tapped through its walls. The water squirted out through the holes and rained down upon the risers at random.
  • each riser was provided with a covering plate, or hat. In operation, the risers were surrounded by a reservoir of water which overflowed through the slots in their upper ends. The air feed was pumped into the top of the mockup enclosure behind a bafile to prevent impingement upon the tray, risers, liquid reservoir, etc.
  • the mockup unit was operated at a water flow rate of 1.52 g.p.m. and an air feed rate of 350 s.c.f./rn.
  • the water after building to the etfective weir level on the tray, passed down through the risers along with the accompanying air.
  • the water from each riser was disengaged from the air, collected and weighed separately.
  • the risers were provided with an inner sleeve whereby the water entered the annulus between the riser and sleeve and passed to an external weighing receiver. Most of the air passed through the sleeve and was vented to the atmosphere.
  • Example 11 This example was similar to Example I and was performed with the same apparatus except that here the risers in the distribution tray were fitted with metal caps, roughly 4 /2 by 4 /z-inches in size, in accordance with the teachings of this invention. Each cap was slotted around its lower rim with 14 slots of l /z-inch by fit-inch dimensions.
  • Example III This example illustrates the ability of the cap and downcomer distribution tray outlets of our invention to compensate for differences in elevation between downcomers during gas flow rate fluctuations and thus reduce flow rate unbalance between misaligned downcomers.
  • FIGURE 9 of the accompanying drawings Data from this example are plotted in FIGURE 9 of the accompanying drawings which graphically illustrates the minimal effect of the air flow changes on the water flow rates through the two risers.
  • the fraction of water passing through the lower riser varied only from about 0.4 to about 0.6 of the total flow, between air flow rates of about 1,800 and about 3,600 s.c.f./h.
  • the flow of water through the lower riser varied only from about 0.43 to about 0.55 of the total flow between air flow rates of 1,200 and 3,600 s.c.f./h.
  • the data indicate that one was apparently at a very slightly lower elevation than the other and the liquid flow rate data for that particular riser are plotted on FIGURE 9.
  • Example IV The tests of this example, demonstrating the heat transfer ability of our liquid-vapor distribution tray, were conducted in a closed vertical vessel resembling a typical catalytic downfiow reactor.
  • a horizontal distribution tray containing two bubble cap and riser assemblies was located below the feed points.
  • Risers were constructed of As-inch steel tubing, 9% inches tall and 3% inches outside diameter. Risers of this particular length were selected to permit viewing through an available window in the test device.
  • the caps were 4%inch inside diameter standard bubble caps, each having seven slots A-inch wide by 2 /2 inches long, equidistantly spaced around the periphery of the cap.
  • the tray effectively isolated the upper vessel section from the lower vessel section except for the fiow communication through the two bubble cap and riser assemblies.
  • Hot kerosene and cold carbon dioxide were used to simulate liquid and vapor feeds to the reactor.
  • the carbon dioxide entered at the top of the vessel at a rate of 1,470 actual cubic feet per hour.
  • Hot kerosene entered through the side wall just above the distributor tray at a point adjacent the east distributor assembly.
  • the kerosene feed entered at a rate of 32.8 lb./min.
  • System pressure was maintained at 200 p.s.i.g. On achieving steady state conditions, the following temperatures were read:
  • a process for contacting a liquid and a vapor in a substantially concurrent downflow manner comprising:
  • a process for contacting a feed mixture of liquid and vapor with a bed of particle-form solids which comprises:
  • an apparatus for contacting and uniformly distributing a substantially downfiowing liquid-vapor mixture over the cross-section of said vessel comprising:
  • a distribution tray substantially horizontally mounted Within said vessel below the source of said liquidvapor mixture, said distribution tray extending across the cross-section of said vessel to separate an upper section of said vessel from a lower section thereof;
  • downcomer conduit means through said distribution tray, said downcomer conduit means being the only fluid communication between said upper section and said lower section through which said liquid-vapor mixture passes, .said downcomer conduit means having their upper edges substantially level;
  • each of said caps surmounting each of said downcomer conduit means and fixedly secured thereto, each of said caps having a peripheral skirt extending downwardly to a level below that of the upper periphery of said downcomer conduit means and to a level above said distribution tray thereby forming an annulus between said peripheral skirt and said downcomer conduit means, said cap and downcomer conduit means serving as the sole conduits defining the flow path of liquid-vapor mixture from said upper section of said vessel to said lower section thereof.
  • each cap is substantially uniformly slotted around its skirt.
  • said contacting vessel contains a plurality of said substantially horizontal distribution trays mounted one above the other in said vessel and spaced apart therein.
  • the apparatus of claim 8 including:
  • a substantially horizontal quench deck mounted in said vessel above said distribution tray and spaced apart therefrom, said quench deck extending across the cross-section of said vessel and having at least two openings therethrough located substantially equidistant from a center axis of said vessel and spaced substantially equidistant about said center axis;
  • quench box attached to the under side of said quench deck and supported therefrom, said quench box having side and bottom members and said quench deck servingas a top member of said box, said openings in said quench deck opening into said quench box, and said bottom member of said quench box having at least two openings therethrough located substantially equidistant aboutsaid center axis of said vessel and substantially uniformly offset about said center axis from said openings in said quench deck;
  • perforated tray mounted within said vessel below said quench deck to which said quench box is attached and above said distribution tray, said perforated tray being spaced apart therefrom and extending substantially across a cross-section'of said vessel, said perforated tray having a plurality of relatively small diameter holes located therethrough and substantial ly uniformly disposed over the surface of said perforated tray except for an area immediately beneath said quench box outlet openings.
  • An apparatus for contacting in a substantially downflow manner a liquid-vapor mixture with a bed of particle-form solids comprising in combination:
  • an inlet means in said vessel located above said upper level of said solids bed to permit introduction of said liquid-vapor mixture into said vessel above said bed of particle-form solids;
  • a substantially horizontal distribution tray mounted in 16' said vessel between said inlet means and said upper level of said solids bed and extending across the cross-section of said vessel in such manner that said inlet means of said vessel is separated from said particle-form solids bed;
  • downcomer conduit means through said distribution tray, said downcomer conduit means being the only fluid communication between said inlef means and said particle-form solids bed, through which said liquid-vapor mixture passes downwardly onto said solids bed, said downcomer conduit means having their upper edges substantially level;
  • each of said caps surmounting each of said downcomer conduit means and fixedly secured thereto, each of said caps having a peripheral skirt extending downwardly to a level below that of the upper periphery of said downcomer conduit means, but above the level of said distribution tray, thereby forming an annulus between said peripheral skirt and said downcomer conduit means, said cap and downcomer conduit means serving as the sole conduits defining the flow path of liquid-vapor mixture through said distribution tray to said particle-form solids bed.
  • each cap is substantially uniformly slotted around its skirt.
  • a contacting vessel containing a plurality of contacting zones disposed one above the other and spaced apart within said vessel;
  • At least one intermediate feed means communicating from the exterior of said vessel to at least one of said intermediate zones for adding intermediate liquid or gaseous feeds to a liquid-vapor mixture flowing through said contacting vessel in a substantially downflow manner;
  • a substantially horizontal quench deck mounted in said intermediate zone of said vessel immediately below said intermediate feed means, said quench deck extending across the cross-section of said vessel and having at least two openings therethrough located substantially equidistant from a center axis of said vessel and spaced substantially equidistant about said center axis;
  • quench box attached to the under side of said quench deck and supported therefrom, said quench box hava perforated tray located in said intermediate zone of said vessel below said quench box, said perforated tray extending substantially across a cross-section of said vessel, said perforated tray having a plurality of relatively small diameter holes located therethrough and substantially uniformly disposed over the surface of said perforated tray except for an area immediately beneath said quench box outlet open ings;
  • a substantially horizontal distribution tray mounted in said intermediate zone of said vessel immediately below and spaced apart from said quench box, and
  • downcomer conduit means through said distribution tray, said downcomer means being the only fluid communication for said downwardly flowing liquid-vapor and intermediate feed mixtures, said downcomer conduit means having their upper edges substantially level;
  • each of said caps surmounting each of said downcomer conduit means and fixedly secured thereto, each of said caps having a peripheral skirt extending downwardly to a level below that of the upper periphery of said downcomer conduit means and to a level above said distribution tray, thereby forming an annulus between said peripheral skirt and said downcomer conduit means, said cap and downcomer conduit means serving as the sole conduits defining the flow path of liquid-vapor mixture from said upper section of said vessel to said lower section thereof.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US355870A 1964-03-30 1964-03-30 Vapor-liquid distribution method and apparatus for the conversion of hydrocarbons Expired - Lifetime US3218249A (en)

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US355870A US3218249A (en) 1964-03-30 1964-03-30 Vapor-liquid distribution method and apparatus for the conversion of hydrocarbons
FR9046A FR1435218A (fr) 1964-03-30 1965-03-12 Procédé de répartition d'une phase vapeur et d'une phase liquide
NL656503278A NL144836B (nl) 1964-03-30 1965-03-15 Inrichting voor het verdelen van een vloeistofgasmengsel over een horizontaal katalysatorbed in een reactor.
DE1965U0011576 DE1542513A1 (de) 1964-03-30 1965-03-30 Verfahren zum gleichmaessigen Verteilen einer aus Dampf und Fluessigkeit bestehenden Mischphase

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Cited By (28)

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Publication number Priority date Publication date Assignee Title
US3502445A (en) * 1966-11-02 1970-03-24 Union Oil Co Apparatus for mixing fluids in concurrent downflow relationship
US3791795A (en) * 1971-11-19 1974-02-12 Monsanto Co Interbed seal for multibed reactors
US3915847A (en) * 1974-02-22 1975-10-28 Universal Oil Prod Co Distribution of liquid-vapor feeds in packed chambers
US3977834A (en) * 1973-12-07 1976-08-31 The British Petroleum Company Limited Multi-bed, mixed-phase, down-flow reactor
US4481105A (en) * 1982-08-25 1984-11-06 Mobil Oil Corporation Processing of hydrocarbons in fixed catalyst bed with redistribution means
US4579647A (en) * 1982-10-15 1986-04-01 Mobil Oil Corporation Multiphase catalytic process with improved liquid distribution
US4743433A (en) * 1982-10-15 1988-05-10 Mobil Oil Corporation Catalytic reactor system
US5232283A (en) * 1992-10-13 1993-08-03 The M. W. Kellogg Company Apparatus for mixing concurrently, downwardly flowing fluids
EP0848974A2 (de) * 1996-12-19 1998-06-24 Haldor Topsoe A/S Flüssigkeitsverteiler für Abwärtsströmung zweier Phasen
EP0907399A1 (de) * 1996-06-04 1999-04-14 Fluor Corporation Verteilungsvorrichtung für einen reaktor und mischvorrichtung für die kühlzone
WO2000024505A1 (en) * 1998-10-23 2000-05-04 Fluor Corporation Reactor distribution apparatus and quench zone mixing apparatus
FR2807676A1 (fr) * 2000-04-17 2001-10-19 Inst Francais Du Petrole Sous-ensemble polyfonctionnel assurant la mise en contact, la distribution de matiere et l'echange de chaleur et/ou de matiere d'au moins une phase gazeuse et d'au moins une phase liquide
US20020172632A1 (en) * 2001-04-02 2002-11-21 Tai-Sheng Chou Quench box for a multi-bed, mixed-phase cocurrent downflow fixed-bed reactor
US20030146525A1 (en) * 2000-12-21 2003-08-07 Jacobs Garry E. Methods and apparatus for mixing fluids
US20040183216A1 (en) * 2003-03-18 2004-09-23 Alan Cross Gas - liquid contactor
EP1490166A1 (de) * 2002-03-14 2004-12-29 Fluor Corporation Verfahren und vorrichtung zum mischen von fluiden
US6881387B1 (en) 1996-06-04 2005-04-19 Fluor Corporation Reactor distribution apparatus and quench zone mixing apparatus
US20060257302A1 (en) * 2003-04-04 2006-11-16 Texaco Inc. Anode tailgas oxidizer
US20070145610A1 (en) * 2004-01-15 2007-06-28 Rasmus Breivik Vapour-liquid distribution tray
CN100434132C (zh) * 2006-11-01 2008-11-19 褚雅志 泡罩立体筛板
EP2047901A1 (de) 2007-10-10 2009-04-15 Petroleo Brasileiro S.A. Petrobras Vorrichtung und Verfahren zur Verteilung von gemischten Chargen auf Katalysator Festbetten bei Abwärtsflussreaktoren
US20090255872A1 (en) * 2006-05-23 2009-10-15 Otv Sa Aerating device for a water filtering system with immersed membranes, including a floor provided with means for injecting a gas and at least one pressure balancing system
US7803334B1 (en) * 2006-07-11 2010-09-28 Uop Llc Apparatus for hydrocracking a hydrocarbon feedstock
CN105363236A (zh) * 2015-12-10 2016-03-02 南通山剑防腐科技有限公司 一种高效节能泡罩塔
CN105498642A (zh) * 2015-12-31 2016-04-20 兰州兰石集团有限公司 抽吸溢流组合型气液分配器
JP2018521854A (ja) * 2015-08-28 2018-08-09 エルジー・ケム・リミテッド 分配器及びこれを含む下降流触媒反応器
JP2018523571A (ja) * 2015-08-28 2018-08-23 エルジー・ケム・リミテッド 分配器及びこれを含む下降流触媒反応器
US20190176119A1 (en) * 2017-12-11 2019-06-13 Axens System for distributing a liquid and/or gas phase into a reaction vessel

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US5158714A (en) * 1991-05-30 1992-10-27 Union Oil Company Of California Vapor-liquid distribution method and apparatus
RU2752351C1 (ru) * 2020-10-12 2021-07-26 Акционерное общество "НАУЧНО-ПРОИЗВОДСТВЕННАЯ КОМПАНИЯ МЕДИАНА-ФИЛЬТР" Опорно-распределительная тарелка

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Cited By (48)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3502445A (en) * 1966-11-02 1970-03-24 Union Oil Co Apparatus for mixing fluids in concurrent downflow relationship
US3791795A (en) * 1971-11-19 1974-02-12 Monsanto Co Interbed seal for multibed reactors
US3977834A (en) * 1973-12-07 1976-08-31 The British Petroleum Company Limited Multi-bed, mixed-phase, down-flow reactor
US3915847A (en) * 1974-02-22 1975-10-28 Universal Oil Prod Co Distribution of liquid-vapor feeds in packed chambers
US4481105A (en) * 1982-08-25 1984-11-06 Mobil Oil Corporation Processing of hydrocarbons in fixed catalyst bed with redistribution means
US4743433A (en) * 1982-10-15 1988-05-10 Mobil Oil Corporation Catalytic reactor system
US4579647A (en) * 1982-10-15 1986-04-01 Mobil Oil Corporation Multiphase catalytic process with improved liquid distribution
US5232283A (en) * 1992-10-13 1993-08-03 The M. W. Kellogg Company Apparatus for mixing concurrently, downwardly flowing fluids
US6508459B1 (en) * 1996-06-04 2003-01-21 Fluor Corporation Distribution apparatus having bubble caps with riser vanes
EP0907399A1 (de) * 1996-06-04 1999-04-14 Fluor Corporation Verteilungsvorrichtung für einen reaktor und mischvorrichtung für die kühlzone
US5989502A (en) * 1996-06-04 1999-11-23 Fluor Corporation Reactor distribution apparatus and quench zone mixing apparatus
EP0907399A4 (de) * 1996-06-04 2000-03-22 Fluor Corp Verteilungsvorrichtung für einen reaktor und mischvorrichtung für die kühlzone
US6881387B1 (en) 1996-06-04 2005-04-19 Fluor Corporation Reactor distribution apparatus and quench zone mixing apparatus
EP0848974A2 (de) * 1996-12-19 1998-06-24 Haldor Topsoe A/S Flüssigkeitsverteiler für Abwärtsströmung zweier Phasen
EP0848974B1 (de) * 1996-12-19 2005-10-12 Haldor Topsoe A/S Flüssigkeitsverteiler für Abwärtsströmung zweier Phasen
WO2000024505A1 (en) * 1998-10-23 2000-05-04 Fluor Corporation Reactor distribution apparatus and quench zone mixing apparatus
KR100810976B1 (ko) * 2000-04-17 2008-03-10 아이에프피 1종 이상의 기체 상 및 1종 이상의 액체 상의 접촉, 물질분배, 그리고 열 및/또는 물질 교환을 위한 다기능성 서브어셈블리
US7060232B2 (en) 2000-04-17 2006-06-13 Institut Francais Du Petrole Polyfunctional sub-assembly for contact, material distribution and heat and/or material exchange of at least one gas phase and at least one liquid phase
US20020127160A1 (en) * 2000-04-17 2002-09-12 Institut Francais Du Petrole Polyfunctional sub-assembly for contact, material distribution and heat and/or material exchange of at least one gas phase and at least one liquid phase
EP1147808A1 (de) * 2000-04-17 2001-10-24 Institut Francais Du Petrole Mehrzweckige Teilmontage, die den Kontakt, die Verteilung und den Wärme- und/oder Materialaustausch in mindestens eine Gasphase sowie eine Flüssigphase sicherstellt
FR2807676A1 (fr) * 2000-04-17 2001-10-19 Inst Francais Du Petrole Sous-ensemble polyfonctionnel assurant la mise en contact, la distribution de matiere et l'echange de chaleur et/ou de matiere d'au moins une phase gazeuse et d'au moins une phase liquide
US20030146525A1 (en) * 2000-12-21 2003-08-07 Jacobs Garry E. Methods and apparatus for mixing fluids
US7125006B2 (en) * 2000-12-21 2006-10-24 Fluor Technologies Corporation Methods and apparatus for mixing fluids
US20020172632A1 (en) * 2001-04-02 2002-11-21 Tai-Sheng Chou Quench box for a multi-bed, mixed-phase cocurrent downflow fixed-bed 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
EP1490166A4 (de) * 2002-03-14 2006-01-18 Fluor Corp Verfahren und vorrichtung zum mischen von fluiden
US20050082696A1 (en) * 2002-03-14 2005-04-21 Jacobs Garry E. Methods and apparatus for mixing fluids
EP1490166A1 (de) * 2002-03-14 2004-12-29 Fluor Corporation Verfahren und vorrichtung zum mischen von fluiden
US7172179B2 (en) * 2002-03-14 2007-02-06 Fluor Technologies Corporation Methods and apparatus for mixing fluids
US6832754B2 (en) * 2003-03-18 2004-12-21 Alan Cross Gas-liquid contactor
US20040183216A1 (en) * 2003-03-18 2004-09-23 Alan Cross Gas - liquid contactor
US20060257302A1 (en) * 2003-04-04 2006-11-16 Texaco Inc. Anode tailgas oxidizer
US8211387B2 (en) * 2003-04-04 2012-07-03 Texaco Inc. Anode tailgas oxidizer
US7600742B2 (en) * 2004-01-15 2009-10-13 Haldor Topsoe A/S Vapour-liquid distribution tray
US20070145610A1 (en) * 2004-01-15 2007-06-28 Rasmus Breivik Vapour-liquid distribution tray
US20090255872A1 (en) * 2006-05-23 2009-10-15 Otv Sa Aerating device for a water filtering system with immersed membranes, including a floor provided with means for injecting a gas and at least one pressure balancing system
US7803334B1 (en) * 2006-07-11 2010-09-28 Uop Llc Apparatus for hydrocracking a hydrocarbon feedstock
CN100434132C (zh) * 2006-11-01 2008-11-19 褚雅志 泡罩立体筛板
US20090134063A1 (en) * 2007-10-10 2009-05-28 Petroleo Brasileiro S.A. Device and process for distribution of mixed charges onto fixed beds of catalyst in descending-flow reactors
EP2047901A1 (de) 2007-10-10 2009-04-15 Petroleo Brasileiro S.A. Petrobras Vorrichtung und Verfahren zur Verteilung von gemischten Chargen auf Katalysator Festbetten bei Abwärtsflussreaktoren
US7988924B2 (en) 2007-10-10 2011-08-02 Petróleo Brasileiro S.A. - Petrobras Device and process for distribution of mixed charges onto fixed beds of catalyst in descending-flow reactors
JP2018521854A (ja) * 2015-08-28 2018-08-09 エルジー・ケム・リミテッド 分配器及びこれを含む下降流触媒反応器
JP2018523571A (ja) * 2015-08-28 2018-08-23 エルジー・ケム・リミテッド 分配器及びこれを含む下降流触媒反応器
US10792635B2 (en) 2015-08-28 2020-10-06 Lg Chem, Ltd. Distributor and down flow catalytic reactor comprising same
CN105363236A (zh) * 2015-12-10 2016-03-02 南通山剑防腐科技有限公司 一种高效节能泡罩塔
CN105498642A (zh) * 2015-12-31 2016-04-20 兰州兰石集团有限公司 抽吸溢流组合型气液分配器
US20190176119A1 (en) * 2017-12-11 2019-06-13 Axens System for distributing a liquid and/or gas phase into a reaction vessel
CN109894054A (zh) * 2017-12-11 2019-06-18 阿克森斯公司 用于在反应室中分布气相和/或液相的***

Also Published As

Publication number Publication date
NL144836B (nl) 1975-02-17
FR1435218A (fr) 1966-04-15
NL6503278A (de) 1965-10-01
DE1542513A1 (de) 1970-03-26

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