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WO2006114241A1 - Chargement de particules de catalyseur dans des tubes reactionnels - Google Patents

Chargement de particules de catalyseur dans des tubes reactionnels Download PDF

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Publication number
WO2006114241A1
WO2006114241A1 PCT/EP2006/003672 EP2006003672W WO2006114241A1 WO 2006114241 A1 WO2006114241 A1 WO 2006114241A1 EP 2006003672 W EP2006003672 W EP 2006003672W WO 2006114241 A1 WO2006114241 A1 WO 2006114241A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
tube
loading
height
hose
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2006/003672
Other languages
English (en)
Inventor
Frederik André DEMAND
Leif Storgaard
Jacob Marcher
Kim Hedegaard Andersen
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.)
Topsoe AS
Original Assignee
Haldor Topsoe AS
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 Haldor Topsoe AS filed Critical Haldor Topsoe AS
Publication of WO2006114241A1 publication Critical patent/WO2006114241A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • B01J8/0242—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 vertical
    • B01J8/0257—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 vertical 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
    • B01J8/02—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
    • B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • 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
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • 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
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding

Definitions

  • the present invention relates to the loading of catalyst particles in reactor tubes.
  • the invention relates to a method and apparatus for the uniform loading of catalyst particles in heat exchange reactors used for carrying out non-adiabatic catalytic reactions. More particularly, the invention relates to a method for the uniform loading of catalyst particles in catalyst tubes having annular spaces adapted to accommodate said particles, and especially for the uniform loading of catalyst particles in bayonet tubes of heat exchange reactors used for the reforming of hydrocarbon feedstocks.
  • Non-adiabatic catalytic reactions such as the endothermic steam reforming of hydrocarbons are often conducted in heat exchange reactors.
  • a particular type of heat exchange reactor is the bayonet tube reactor.
  • the bayonet tubes are tubes in which the catalyst is placed in the annular space between an outer and inner tube, and in which the hydrocarbon feed first passes through the catalyst-containing annular space in one direction, and then through the inner, empty (catalyst-free) tube in the opposite direction.
  • additional heat is supplied by the reformed gas flowing upwardly through the inner tube.
  • the outer diameter of the outer tube is about 125 mm, the wall thickness about 5 mm, while the outer diameter of the inner tube is about 50 mm with a wall thickness of about 5 mm.
  • the length of the outer and inner tubes is normally about 7 m, but can be higher for instance about 10 m.
  • the number of bayonet tubes in a heat exchange reactor for steam reforming processes varies from 1 to about 30.
  • One particular embodiment of a bayonet tube heat exchange reactor is for instance disclosed in EP-A-O, 535, 505.
  • a loading tube is introduced into the reactor tube to be loaded with catalyst.
  • the loading tube has a diameter smaller than that of the reactor tube and a tube length substantially corresponding to the length of the reactor tube.
  • the loading tube consists of separate tube sections provided with a spirally formed body on the inner wall so as to decelerate the catalyst particles.
  • the loading tube is then successively withdrawn from the bayonet tube in a length corresponding to the loaded height of catalyst particles. This provides normally an even and gentle loading of the catalyst particles in conventional straight reformer tubes and eliminates the risk of crushing particles as they fill the reactor tube.
  • the loading of catalyst by means of mechanical devices having fixed parts is often inexpedient.
  • a loading tube having a diameter lower than for example 70 mm and a tube length substantially corresponding to the length of the bayonet tube (about 10 m) is introduced into the annular space of the bayonet tubes.
  • the inner tube of the bayonet tube runs substantially coaxially with the outer tube, said inner tube is often not fully straight along its length so that its wall often bends slightly outwardly.
  • the loading tube is substantially straight along its whole length.
  • the introduction of the loading tube results in an undesired colli- sion with the inner wall of the bayonet tube at a certain height, normally in its middle region for instance in the region corresponding to 30% to 70% of the length of the bayonet tube.
  • This impedes further penetration of the loading tube and as a result there is higher propensity of crushing catalyst particles as they are forced to be loaded into the catalyst tube from a high dropping height.
  • the density of particles at the bottom of the tube is higher than at any other height, thus further increasing the risk of breakage of particles, particularly at the bottom of the catalyst tube.
  • Some bayonet tubes disposed in a heat exchange reactor may have inner tubes which are fully straight along their length, while others may have inner tubes that bend slightly outwardly.
  • the bending of the inner tube in some bayonet tubes conveys the attendant problem of uneven loading of catalysts across the different bayonet tubes. This in turn creates uneven flow conditions in the reactor so that non-uniform temperatures prevail. Poor control of the conversion of reactants and/or undesired side reactions may thus occur.
  • uniform loading is meant a loading in which the density of the catalyst particles along the whole length of the reactor tubes is substantially equal or within a narrow range of density values for instance within the range 800-820 kg/m 3 .
  • initial dropping height is meant the distance from the open end of the hose where the particles are first discharged to the surface of the underlying catalyst bed.
  • loaded height is meant the distance from the bottom of the catalyst tube to the catalyst surface at the top of the particle bed.
  • catalyst tube encompasses in its broadest scope tubes having an annular space adapted to receive solid catalyst particles, such as bayonet tubes as described above and also so-called double-tubes, as for instance de- scribed in EP-A-I, 106, 570.
  • the one or more catalyst tubes consist of an inner tube arranged substantially coaxially with an outer tube and in which the walls of the inner and outer tube define an annular space adapted to receive solid catalyst particles, the method comprising stages (a) and (b) :
  • the IDH may be adjusted at any stage to a value which may be higher or lower than the IDH of the previous stage.
  • the density of particles will decrease with the loaded height, i.e. with the highest density at the bottom of the catalyst tube and lowest density at the top.
  • the initial drop- ping height as the loading position in the catalyst tube increases, the density of particles is kept at substantially the same value as at the bottom of the catalyst tube or within a narrow range of density values. Further, the loading time of the catalyst tubes is significantly reduced with respect to known methods.
  • the loading position in the catalyst tube is governed by the position of the discharge end of the loading hose, and each stage corresponds to IDH being adjusted to the required level.
  • the flow of catalysts into the hose from a catalyst box lying above the reactor tube or reactor tube assembly may be slowed down or optionally completely stopped.
  • the flow of particles may then be resumed. This enables better control of the loading procedure.
  • the IDH may conveniently be set at about 0.8 m.
  • the IDH may then be adjusted to about 1.1 m.
  • the IDH may be adjusted to 1.6 m.
  • the IDH is adjusted to a lower level of 1.3 m. This enables the density to be kept within a narrow range along the length of the tube.
  • the initial drop height (IDH) should not be too small because the packing of the particles and thereby the density may be too low.
  • the IDH should not be too high since the catalyst particles may break. Accordingly, the IDH may be increased up to the maximum level IDH max , which provides the highest density at any given loaded height. Increase of IDH above IDH max will result in a decrease in density.
  • IDH is adjusted at any stage to a value which is higher than the IDH of the previous stage but not above IDH max .
  • the invention provides also a method for the uniform loading of one or more catalyst tubes as described above, wherein in stage (b) said subsequent initial drop height IDH is higher than the initial drop height of the previous stage but not above a threshold value IDH max .
  • the density of particles will decrease with the loaded height, i.e. with the highest density at the bottom of the catalyst tube and lowest density at the top.
  • IDH at the bottom of the catalyst tube for example at a loaded height between 0 and 1 m (first 10% of tube's length from the bottom in a 10 m long tube), is in the range 0.4 to 0.9 m; the subsequent IDH at a loaded height of up to 4 or 5 m is preferably in the range 1.0 to 1.2 m, while up to a loaded height of 10 m, i.e. up to the top of the tube, the initial drop height may correspond to IDH max having values of 1.3 to 1.5 m.
  • IDH of for example 0.8 m gives a low density value and is thus more convenient to apply near the bottom of a 10 m catalyst tube.
  • a lower value of IDH can be used at the bottom, for example 0.6 or 0.5 m or even lower, such as 0.4 m.
  • IDH In the upper part of the tube, for example from bottom to the middle of the catalyst tube, for example up to 4 or 5 m, a value of IDH of 1.0-1.2 m may be applied. From about 4 or 5 m up to the top of the catalyst tube an IDH of 1.3 to 1.4 m (IDH max ) may be used. Further increasing IDH above IDH max to for instance 1.6 m results in a decrease of density with loaded height, which normally is undesired.
  • the catalyst tubes in the heat exchange reactor are selected from the group of bayonet tubes and double tubes.
  • the catalyst tubes are bayonet tubes.
  • the catalyst tubes are bayonet tubes having a length about 10 m and the loading of the catalyst along the whole length of the tube is conducted in three stages, wherein the initial drop height up is about 0.8 m up to a loaded height of 0.5, the subsequent initial drop height is about 1.1 m up to a loaded height of 4 m and the subsequent initial drop height is 1.3, which corresponds to IDH max and is used up to a loaded height of 10 m.
  • the filling of catalyst is effected so that an amount of catalyst corresponding to 0.2 to 0.7 m, most preferably 0.5 m loaded height is introduced in each filling step once the IDH has been adjusted to the required level.
  • the annular space of the catalyst tube is filled after each filling step with particles up to a level of about 0.1 to 0.8 m below the level corresponding to the discharging end of the loading hose (i.e. distance between catalyst surface and discharging end of loading hose after each filling) . This enables a reasonable dropping height for all the particles while being loaded.
  • the distance between catalyst surface and discharging end of loading hose after each filling is about 0.1 m.
  • the distance between the catalyst surface and discharging end of loading hose after each filling is about 0.6 m.
  • the loading of the annular space of the catalyst tube may also be effected by simultaneously filling particles with additional loading hoses introduced at different positions along the annular space. This enables more even packing and thereby even density at any position in the annular space of the catalyst tube. Alternatively, a single loading hose can be shifted from one side to the opposite side in the annular region.
  • the invention provides also a loading apparatus for use in the loading method described above.
  • the loading apparatus comprises a flexible loading hose adapted to be introduced into the annular space of the tube, said loading hose having a first end which is connected to a catalyst box con- taining the solid particles to be charged into the annular space of the tube and a discharging end, said loading hose further having an internal coating so as to provide for inner friction of the solid catalyst particles as they fall within the hose.
  • the catalyst box is preferably a hopper having a conical end to which the first end of the loading hose is attached. It would also be understood that the discharging end of the hose is the open end of the loading hose from where cata- lyst particles travelling within the hose are discharged.
  • flexible hose is meant that the hose is bend- able and therefore it can easily be adapted within the annular space of the catalyst tubes. The flexible loading hose enables the operator to lower the hose easily and rap- idly into the catalyst tube and at any position without bothering about the hose colliding with the outer wall of the catalyst tube.
  • the inner side of the loading hose which is in contact with the solid particles has to comply with the requirements of having a sufficiently high friction so as to decrease the speed of the particles in order to prevent particle breakage. At the same time, the friction has to be sufficiently low so as to avoid blockage of particles.
  • the hose is therefore provided with an internal coating that provides for inner friction of the particles so these decelerate during their passage through the loading hose.
  • the hose is made of polyester with an internal coating of ethylenpropylenpolymer rubber. Particular benefits are ob- tained with this internal coating, since it enables the loading of the catalyst particles to occur gently.
  • the diameter of the hose is about 50 mm, depending naturally on the size of the annular space to be filled. Obviously, the diameter of the hose is such that it can be in- troduced easily in the annular space along the length of the catalyst tube.
  • the invention encompasses also a heat exchange reactor for carrying out non-adiabatic catalytic reactions comprising at least one catalyst tube filled with solid catalyst particles according to the method above.
  • the heat exchange reactor is a bayonet tube reactor comprising one or more catalyst tubes used for the reforming of hydrocarbon feedstocks.
  • a particularly preferred type of reactor is the so-called HTCR heat exchange reformer, as for instance disclosed in EP-O, 983, 963.
  • Figure 1 shows a simplified longitudinal section of a bayonet tube catalyst tube
  • Figure 2 shows the trendlines of density of the catalyst particles as a function of the loaded height and initial drop height (IDH) in a bayonet tube.
  • bayonet tube 1 consists of an outer tube 2 having an open inlet 3 for the passage of unconverted process gas and closed outlet 4.
  • an inner tube 5 open at both ends is arranged substantially coaxi- ally with said outer tube 2.
  • Converted process gas enters through perforated bottom of inner tube 5 and leaves at its top.
  • the perforated bottom of inner tube 5 is fixed at the closed outlet 4 of the outer tube 2.
  • the outer and inner tubes define an annular space 6 adapted to receive and accommodate the solid catalyst particles 7 so as to form a catalyst bed 8.
  • the bayonet tube is provided with a sleeve 9 which defines a space 10 for the passage of a heat con- ducting medium, such as flue gas.
  • a loading hose 11 is introduced into the annular space 6 in one side of the bayonet tube 1, said hose 11 has a discharge end 12 where solid catalyst particles eject onto catalyst surface 13.
  • the distance from the bottom of the bayonet tube 1 to the catalyst surface 13 represents the loaded height, while the distance from the discharge end of the hose 12 (where the particles are discharged for the first time once the loading hose has been positioned) to the catalyst surface represents the initial drop height (IDH) .
  • Figure 2 shows the trendlines of obtained densities of par- tides.
  • the densities are higher at the bottom of the catalyst tube than in the top. This indicates that the particles, despite the inner coating of the loading hose, still accelerate significantly.
  • the density of particles decreases with loaded height.
  • a maximum in density at a given loaded height is obtained with an IDH of 1.3 m; further increasing IDH to for instance 1.6 m may result in a decrease of density as illustrated by the density vs. loaded height trendline for IDH of 1.6 m of Figure 2.
  • Inner diameter of outer tube 125 mm
  • Outer diameter of inner tube 50 mm
  • Tube height 6 m
  • the catalyst material is a steam reforming catalyst with particles of size 16 x 11 mm, but which are not impregnated with nickel, which is the active catalyst component in steam reforming. It is expected that nickel increases the strength of the particles.
  • a catalyst box loader
  • a flexible hose was attached to the exit of the loader. Because the diameter of this standard hose was too big, a smaller hose was put inside. Since the diameter of this hose still was too big a slid was made to decrease the diameter. The loading hose was lowered into the catalyst tube.
  • Loading hoses of various lengths were made to vary the drop height.
  • the loading hoses were made varying the length with 0.5 m. During loading it was thus aimed at loading particles corresponding to 0.5 m of tube at a time.
  • the loading density may vary as a function of the loading speed. If the loading speed is too high then the density will decrease.
  • the loading speed was independent of the reformer tube diameter.
  • the minimum loading speed for loading 0.5 m in a 120 mm tube is thus the same as when loading a 72 mm tube. In regular reformer tubes the minimum loading speed was found to be 20 seconds for loading of 0.8 meter of tube. Assuming the principle also was valid for bayonet tubes then the minimum loading time for loading 0.5 m was expected to be 12.5 seconds. However, the area in a bayonet tube is distributed differently than in a regular tube and the particles will typically drop in one side of the tube and then roll to the other side. Therefore, the minimum loading speed required in a bayonet tube may be higher than in a regular reformer.
  • the loading of a 10 m bayonet tube according to the invention can be conducted as follows:
  • the catalyst surface After loading the annular space of the tube with catalyst particles from the bottom to 0.5 m, the catalyst surface reaches a level of about 0.1 below the level of the discharging end of the loading hose.
  • the loading hose is then raised 1 m to provide for a new IDH of 1.1 m.
  • the catalyst tube is further filled with catalyst particles corresponding to 0.5 m so that the loaded height is now 1 m and reaches a level of 0.6 m below the discharging end of the hose i.e. distance between catalyst surface and discharging end of loading hose after each filling.
  • the loading hose is raised 0.5 m to provide again for an IDH of 1.1 m. The procedure is repeated after reaching a loaded height of 4 m.
  • the IDH is constant at 1.1 m and the distance between the discharging end of the hose and the catalyst surface after each 0.5 m filling is kept at 0.6 m.
  • the hose is raised 0.7 m to provide for a new IDH of 1.3 m (IDH max ), which is kept for the rest of the loading.
  • the catalyst tube is filled with catalyst corresponding to 0.5 m loaded height, thus resulting in a distance between the discharging end of the hose and the catalyst surface after each 0.5 m filling of 0.8 m.
  • the procedure is repeated until the catalyst mate- rial reaches a loaded height of 10 m.
  • the IDH is constant at 1.3 m and the distance between the discharging end of the hose and the catalyst surface after each 0.5 m filling is kept at 0.8 m.
  • the loading according to the inventive method provides a loading time of 1 hour per tube, which is a significant reduction in loading time compared with the use of the loading apparatus described in EP-A-I, 283, 070, where the time required for conducting the loading of one bayonet tube is 6-7 hours per tube.
  • Reactors used for the reforming of hydrocarbons contain normally about 30 bayonet tubes.

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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)

Abstract

L'invention concerne une méthode de chargement uniforme d'au moins un tube de catalyseur dans un réacteur d'échange de chaleur, au moins un tube de catalyseur étant constitué d'un tube intérieur agencé de manière sensiblement coaxiale avec un tube extérieur, et les parois du tube intérieur et du tube extérieur définissant un espace annulaire conçu pour recevoir des particules de catalyseur solide. La méthode de l'invention comprend les étapes consistant à: (a) introduire un tuyau souple de chargement dans l'espace annulaire du tube à remplir à l'aide du catalyseur, de sorte que la distance entre l'extrémité d'évacuation du tube flexible de chargement et le fond de ce tube définisse une première hauteur de chute initiale, et remplir, en au moins une étape, l'espace annulaire du tube avec le catalyseur, jusqu'à une hauteur chargée, le niveau de la hauteur chargée correspondant à l'extrémité d'évacuation du tuyau souple de chargement ou à un niveau inférieur, tout en maintenant simultanément la première hauteur de chute initiale susmentionnée à une valeur constante par le relevage du tuyau souple de chargement après chaque étape de remplissage de catalyseur; (b) relever le tuyau souple de chargement de sorte que la distance entre l'extrémité d'évacuation du tuyau souple de chargement et la surface de catalyseur définisse une hauteur de chute initiale subséquente qui est supérieure ou inférieure à la hauteur de chute initiale de l'étape précédente, et remplir, en au moins une étape, l'espace annulaire du tube à l'aide du catalyseur, jusqu'à une hauteur chargée subséquente, la hauteur chargée subséquente susmentionnée présentant une valeur supérieure à la hauteur chargée de l'étape précédente, mais inférieure à la longueur totale du tube du catalyseur, le niveau de la hauteur chargée susmentionnée correspondant au niveau de l'extrémité d'évacuation du tuyau souple de chargement ou à un niveau inférieur, tout en maintenant simultanément ladite hauteur de chute initiale subséquente constante par le relevage du tuyau souple de chargement après chaque étape de remplissage; l'étape (b) étant effectuée au moins une fois.
PCT/EP2006/003672 2005-04-28 2006-04-21 Chargement de particules de catalyseur dans des tubes reactionnels Ceased WO2006114241A1 (fr)

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DKPA200500624 2005-04-28
DKPA200500624 2005-04-28

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2016500561A (ja) * 2012-10-17 2016-01-14 イエフペ エネルジ ヌヴェルＩｆｐ Ｅｎｅｒｇｉｅｓ Ｎｏｕｖｅｌｌｅｓ 水蒸気改質反応器−交換器のためのバヨネット管に触媒を濃密に装填するためのガスを供給する取り外し可能な管を有する気体システム
RU2635601C2 (ru) * 2012-10-17 2017-11-14 Ифп Энержи Нувелль Пневматическая система плотной загрузки катализатора в байонетные трубы для реактора-теплообменника конверсии с водяным паром
RU2641740C2 (ru) * 2012-10-17 2018-01-22 Ифп Энержи Нувелль Пневматическая система для плотной загрузки катализатора в байонетные трубы обменного реактора парового реформинга с использованием вспомогательной трубы для введения твердых частиц

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Publication number Priority date Publication date Assignee Title
US5585075A (en) * 1994-04-28 1996-12-17 Softard Industries Co., Ltd. Catalyst loading structure and a loading method for a reactor
EP0904831A1 (fr) * 1997-01-23 1999-03-31 Nippon Shokubai Co., Ltd. Procede d'acheminement de materiau granuleux et systeme d'alimentation
EP0938924A1 (fr) * 1998-02-10 1999-09-01 Hercules Incorporated Réacteur à lit fixe pour des réactions catalytiques
US5964259A (en) * 1997-07-15 1999-10-12 Praxair Technology, Inc. Multiple adsorbent loading method and apparatus for a radial flow vessel
US6467513B1 (en) * 1998-12-25 2002-10-22 Toyo Engineering Corporation Method for packing catalyst and device therefor
US20040191136A1 (en) * 2001-06-21 2004-09-30 Early Simon Robert Method of loading a particulate solid into a vessel

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5585075A (en) * 1994-04-28 1996-12-17 Softard Industries Co., Ltd. Catalyst loading structure and a loading method for a reactor
EP0904831A1 (fr) * 1997-01-23 1999-03-31 Nippon Shokubai Co., Ltd. Procede d'acheminement de materiau granuleux et systeme d'alimentation
US5964259A (en) * 1997-07-15 1999-10-12 Praxair Technology, Inc. Multiple adsorbent loading method and apparatus for a radial flow vessel
EP0938924A1 (fr) * 1998-02-10 1999-09-01 Hercules Incorporated Réacteur à lit fixe pour des réactions catalytiques
US6467513B1 (en) * 1998-12-25 2002-10-22 Toyo Engineering Corporation Method for packing catalyst and device therefor
US20040191136A1 (en) * 2001-06-21 2004-09-30 Early Simon Robert Method of loading a particulate solid into a vessel

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2016500561A (ja) * 2012-10-17 2016-01-14 イエフペ エネルジ ヌヴェルＩｆｐ Ｅｎｅｒｇｉｅｓ Ｎｏｕｖｅｌｌｅｓ 水蒸気改質反応器−交換器のためのバヨネット管に触媒を濃密に装填するためのガスを供給する取り外し可能な管を有する気体システム
RU2635601C2 (ru) * 2012-10-17 2017-11-14 Ифп Энержи Нувелль Пневматическая система плотной загрузки катализатора в байонетные трубы для реактора-теплообменника конверсии с водяным паром
RU2637338C2 (ru) * 2012-10-17 2017-12-04 Ифп Энержи Нувелль Пневматическая система плотной загрузки катализатора в байонетные трубы для реактора обменного типа конверсии с водяным паром со съемной трубой для подачи газа
RU2641740C2 (ru) * 2012-10-17 2018-01-22 Ифп Энержи Нувелль Пневматическая система для плотной загрузки катализатора в байонетные трубы обменного реактора парового реформинга с использованием вспомогательной трубы для введения твердых частиц

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