WO2007086612A1 - Réacteur de synthèse d'hydrocarbures du type colonne à bulles - Google Patents

Réacteur de synthèse d'hydrocarbures du type colonne à bulles Download PDF

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Publication number
WO2007086612A1
WO2007086612A1 PCT/JP2007/051854 JP2007051854W WO2007086612A1 WO 2007086612 A1 WO2007086612 A1 WO 2007086612A1 JP 2007051854 W JP2007051854 W JP 2007051854W WO 2007086612 A1 WO2007086612 A1 WO 2007086612A1
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WIPO (PCT)
Prior art keywords
gas
slurry
main body
catalyst particles
barrier member
Prior art date
Application number
PCT/JP2007/051854
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English (en)
Inventor
Osamu Wakamura
Yuzuru Kato
Eiichi Yamada
Yasuhiro Onishi
Yasuyuki Osawa
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Nippon Steel Engineering Co., Ltd.
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Filing date
Publication date
Application filed by Nippon Steel Engineering Co., Ltd. filed Critical Nippon Steel Engineering Co., Ltd.
Publication of WO2007086612A1 publication Critical patent/WO2007086612A1/fr

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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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
    • B01J8/226—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement internally, i.e. the particles rotate within the vessel
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/44—Fluidisation grids
    • 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
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/34—Apparatus, reactors
    • C10G2/342—Apparatus, reactors with moving solid catalysts
    • 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
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • 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
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00141—Coils
    • 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
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates

Definitions

  • the present invention relates to a bubble column type hydrocarbon synthesis reactor, and in particular to a reactor that carries out a Fischer-Tropsch synthesis reaction by introducing a synthesis gas into a slurry having solid catalyst particles suspended in a liquid hydrocarbon.
  • FT reaction Fischer-Tropsch synthesis reaction
  • a bubble column type slurry phase FT reaction system that carries out a FT reaction by introducing a synthesis gas into a slurry in which solid catalyst particles are suspended in a liquid hydrocarbon is available.
  • a hydrocarbon compound synthesized by the FT reaction is mainly utilized as a raw material for fuel oil and lubricant oil.
  • a technology has been proposed as solving means of such a problem, which improves a dispersed state of catalyst particles by providing another gas introducing portion separately from the main introducing port on the upper part of the main introducing port (distributor) of a synthesis gas (For example, refer to US Patent No. 5,252,613).
  • the present invention was developed in view of such problems. It is therefore an object of the invention to evenly disperse catalyst particles in a liquid hydrocarbon in a reactor without providing another gas introducing port separately from the main introducing port of a synthesis gas in a bubble column type hydrocarbon synthesis reactor that carries out a Fischer-Tropsch synthesis reaction.
  • the inventor et al. found, based on earnest research and study to solve the above-described problems, that it is possible to disperse catalyst particles, which are about to be accumulated on a screen, by means of an agitation effect of gas ejected from a introducing port by installing the screen, the mesh of which is smaller than the catalyst particles, directly below the introducing port (distributor) of a synthesis gas, and completed the invention based on the findings.
  • a bubble column type hydrocarbon synthesis reactor synthesizes a hydrocarbons by a chemical reaction of a gas whose main components are hydrogen and carbon monoxide, and a slurry having solid catalyst particles suspended in a liquid, and includes: a reactor main body for accommodating the slurry; a reaction gas-feeding portion that is disposed at the lower part of the reactor main body and feeds the gas into the slurry by ejecting the same; and a barrier member that is disposed forward of the ejecting direction of the gas ejected from the reaction gas-feeding portion and restricts the flow of the slurry.
  • the barrier member may be installed in a range where the flow of the slurry, which is produced by the gas ejected from the reaction gas-feeding portion, is reached.
  • the barrier member may be disposed equidistantly from all the gas ejecting ports for ejecting the gas downward of the gas ejecting ports of the reaction gas-feeding portion.
  • the barrier member may include a filtering element that does not allow the catalyst particles in the slurry to pass therethrough.
  • the filtering element may be installed in a part of the barrier member.
  • catalyst particles accumulated on the barrier member are agitated by an agitation effect of gas ejected from the distributor, and thus the dispersion effect into the slurry can be improved.
  • the temperature inside the reactor can be maintained more uniformly, wherein the composition of the liquid hydrocarbon product can be stabilized.
  • the bubble column type hydrocarbon synthesis reactor of the invention since it is not necessary for another gas introducing port to be provided separately from the distributor, the structure inside the reactor and arrangement of the piping outside the reactor can be simplified. Further, it is not necessary to provide a mechanism for adjusting or regulating the flow rate of gas supplied into the slurry between the distributor and another gas introducing port.
  • FIG. 1 is a longitudinal sectional view showing the entire configuration of an FT reactor according to Embodiment 1 of the invention.
  • FIG. 2 is an enlarged longitudinal sectional view showing the major parts of the FT reactor according to Embodiment 1 of the invention, which is depicted in FIG. 1.
  • FIG. 3 is an enlarged longitudinal sectional view showing a synthesis gas feeding nozzle that composes the distributor depicted in FIG. 2.
  • FIG. 4 is a cross-sectional view showing the FT reactor depicted in FIG. 2, which is taken along the line III-III.
  • FIG. 5 is a top plan view showing a barrier member according to Embodiment 1 of the invention, which shows an example having a screen provided on the entire surface thereof.
  • FIG. 6 is a top plan view showing a barrier member according to Embodiment 1 of the invention, which shows an example having a screen provided on a part of the surface thereof.
  • FIG. 7 is a view showing a method for diffusing catalyst particles according to Embodiment 1 of the invention, which shows a state where the catalyst particles are accumulated on the screen.
  • FIG. 8 is a view showing a method for diffusing catalyst particles according to Embodiment 1 of the invention, which shows a state where the catalyst particles are agitated.
  • FIG. 9 is a view showing a state where catalyst particles are agitated by a distributor according to a modified version of Embodiment 1 of the invention.
  • an FT reactor a bubble column type slurry phase FT synthesis reactor
  • the FT reactor 1 is essentially provided with a reactor main body 10, a distributor 20, a barrier member 30 and a cooling tube 40.
  • the reactor main body 10 is a roughly cylindrical vessel made of metal, the diameter of which is 1 to 20 meters, preferably 2 to 10 meters, and the height of which is 10 to 50 meters, preferably 15 to 45 meters.
  • Slurry 12 having solid catalyst particles 124 suspended in a liquid hydrocarbon (product of the FT reaction) 122 is contained in the interior of the reactor main body 10.
  • the distributor 20 is one example of a reaction gas-feeding portion according to the present embodiment.
  • the distributor 20 is disposed at the lower part in the interior of the reaction main body 10, and ejects a synthesis gas, the main components of which are hydrogen and carbon monoxide, downward and feeds the same into the slurry 12.
  • the distributor 20 is provided with a synthesis gas feeding pipe 22, a nozzle header 24 attached to the distal end part of the synthesis gas feeding pipe 22, and a plurality of synthesis gas feeding nozzles 26 attached to the side part of the nozzle header 24. The details thereof are described later.
  • the barrier member 30 is installed forward of the ejecting direction of the synthesis gas ejected from the distributor 20, that is, downward of the distributor 20, and restricts the flow of the slurry 12.
  • the barrier member 30 may include a filtering element that does not allow the catalyst particles 124 in the slurry 12 to pass therethrough.
  • the liquid hydrocarbon 122 is separated from the catalyst particles 124 by the filtering element, and only the liquid hydrocarbon 122 can be discharged through the liquid hydrocarbon discharge port 14 secured at the bottom part of the reactor main body 10.
  • the filtering element may be provided in the barrier member 30. The details of the barrier member 30 will also be described later.
  • the cooling tube 40 is provided along the height direction of the reactor main body 10 in the interior of the reactor main body 10 and cools the slurry 12, the temperature of which is raised due to heat generated by the FT synthesis reaction.
  • the cooling tube 40 may be formed so as to reciprocate a plurality of times (for example, it reciprocates two times in FIG. 1) vertically in the perpendicular direction by bending a single tube as shown in, for example, FIG. 1.
  • the shape and number of cooling tubes are not limited to the above-described shape and number, but may be such that the cooling tubes are evenly disposed in the interior of the reactor main body 10 and contribute to uniform cooling of the slurry 12.
  • a plurality of cooling tubes having a double-tube structure of a so-called bayonet type may be installed in the interior of the reactor main body 10.
  • Cooling water (for example, the temperature of which is different by -50 through 0 0 C from the interior temperature of the reactor main body 10) introduced from the cooling tube inlet 42 is made to circulate in the cooling tube 40.
  • the cooling water By exchanging heat between the cooling water and the slurry 12 via the tubular wall of the cooling tube 40 in the process during which the cooling water circulates in the cooling tube 40, the slurry 12 in the interior of the reactor main body 10 is cooled down and reaction temperature is constant.
  • Some of the cooling water is discharged from the cooling tube outlet 44 as steam.
  • the medium for cooling the slurry 12 is not limited to cooling water as described above, but, for example, a straight chain, branched-chain and annular paraffin, olefin, low-molecular-weight silane, silyl ether, and silicone oil, etc., of C4 through ClO may be used as the medium.
  • the distributor 20 is provided with the synthesis gas feeding pipe 22, nozzle header 24 and a plurality of synthesis gas feeding nozzles 26.
  • the synthesis gas feeding pipe 22 passes through the side wall of the reactor main body 10 and is bent downward toward the perpendicular direction at the middle part of the interior of the reactor main body 10 and in the vicinity thereof.
  • the nozzle header 24 is attached to the distal end part of the bent synthesis gas feeding pipe 22, and the nozzle header 24 is made to extend in the diametrical direction of the reactor main body 10.
  • a plurality of synthesis gas feeding nozzles 26 are provided in a direction roughly orthogonal to the nozzle header 24 at both sides in the lengthwise direction of the nozzle header 24.
  • the respective synthesis gas feeding nozzles 26 are made longer and longer as they approach the middle part of the nozzle header 24 in compliance with a circular sectional shape of the reactor main body 10, and are made shorter and shorter as they approach both the ends thereof, so that the synthesis gas is evenly distributed in the slurry 12 in the interior of the reactor main body 10.
  • the shape and number of the nozzle header 24 and synthesis gas nozzles 26 are not specially restricted.
  • a plurality of synthesis gas-ejecting ports 26a, 26b and 26c are formed along the lengthwise direction in the synthesis gas feeding nozzle 26 (in FIG. 4, the synthesis gas-ejecting ports 26a and 26c are not illustrated for convenience). It is preferable that the synthesis gas-ejecting ports 26a, 26b and 26c be installed in the lower half area of the synthesis gas feeding nozzle 26 so that the synthesis gas is ejected downward (in the direction toward the bottom part of the reactor main body 10).
  • the synthesis gas-ejecting ports 26a, 26b and 26c are not necessarily formed in the lower half area of the synthesis gas feeding nozzle 26, wherein if such a structure is employed by which the synthesis gas is ejected downward, these ports may be formed at any optional position.
  • ports for ejecting the synthesis gas upward may be formed in the upper half area of the synthesis gas feeding nozzle 26 in addition to the ports for ejecting the synthesis gas downward.
  • the synthesis gas ejecting ports 26a, 26b and 26c according to the embodiment are formed so that the ejecting directions of the ejecting ports adjacent to each other are shifted by 45° in order that the synthesis gas can be evenly and efficiently ejected.
  • the arrangement of the synthesis gas-ejecting ports 26a, 26b and 26c is not limited to the above-described arrangement, and the number of ejecting ports is not limited to three ports.
  • the synthesis gas supplied from the exterior of the reactor main body 10 into the distributor 20 via the synthesis gas feeding pipe 22 passes through the interior of the nozzle header 24 and is ejected into the slurry 12 downward (that is, the direction shown by the arrow in the drawing) from the synthesis gas-ejecting ports 26a, 26b and 26c secured at the lower part (the bottom part side of the reactor main body 10) of the synthesis gas feeding nozzle 26.
  • the synthesis gas introduced from the distributor 20 into the slurry 12 is made into bubbles 28 and drifts from bottom to the top toward the height direction (the perpendicular direction) of the reactor main body 10 in the slurry 12.
  • the synthesis gas is dissolved in the liquid hydrocarbon 122 and is brought into contact with the catalyst particles 124, whereby a synthesis reaction of a liquid hydrocarbon (FT synthesis reaction) is carried out.
  • the synthesis gas is introduced from the distributor 20, which is disposed at the lower part of the interior of the reactor main body 10, into the slurry 12, and the synthesis gas thus introduced in is made into bubbles 28 and is passed upward in the interior of the reactor main body 10, whereby, in the interior of the reactor main body 10, as shown by thick arrows in FIG. 1, an ascending flow of the slurry 12 is generated in the middle part of the reactor main body 10 and in the vicinity thereof (that is, in the vicinity of the center axis of the reactor main body 10), and a descending flow thereof is generated near the inner wall of the reactor main body 10 (that is, near the inner-circumferential portion).
  • the barrier member 30 is composed of a screen 32 operating as one example of the filtering element according to the embodiment and a screen supporting member 34 for supporting the screen 32 from its downside, and the barrier member 30 is installed forward in the ejecting direction of the synthesis gas ejected from the distributor 20, that is, downward of the distributor 20.
  • the screen 32 may be, for example, a filter that includes a plurality of slits having a smaller slit width than the size of the catalyst particles 124, does not permit the catalyst particles 124 to pass through, and allows only the liquid hydrocarbon 122 and bubbles 28 to pass through. By installing such a screen 32 at the bottom part of the reactor main body 10, only the flow of the catalyst particles downward of the screen 32 is restricted.
  • the screen supporting member 34 is a member for supporting the screen 32 from its downside and is composed so as to permit at least the liquid hydrocarbon 122 and bubbles 28 to pass through so that it does not hinder the role of the screen 32 as a filter.
  • the screen 32 including a plurality of slits 32a having a smaller width d than the size of the catalyst particles 124 and wires 32b provided at both sides of the slit 32a is installed on the entire upper surface of the barrier member 30.
  • the slit width d of the screen 32 be sufficiently smaller than the mean particle size of the catalyst particles 124 so that the catalyst particles 124 are not permitted to pass through downward of the screen 32. That is, it is preferable that the slid width d be, for example, 50% or less of the mean particle size of the catalyst particles, preferably 10 through 30% thereof.
  • the screen 32 including a plurality of slits 32a having a sufficiently smaller slit width d than the mean particle size of the catalyst particles 124 is installed, the liquid hydrocarbon 122 and the catalyst particles 124 are separated from each other, and only the liquid hydrocarbon 122 can be discharged from the liquid hydrocarbon discharge port 14 installed at the bottom part of the reactor main body 10.
  • the catalyst particles 124 are not permitted to pass through the screen 32, they will be accumulated on the screen 32. However, the catalyst particles 124 that will be accumulated on the screen 32 are raised upward of the reactor main body 10 by ejecting the synthesis gas from the above-described distributor 20 onto the screen 32. Further details are described later.
  • the screen 32 is installed on a part of the barrier member 30, as shown in FIG. 6, for example, the screen 32 installed at the opening 33 formed at the middle part of a shield plate 36 is supported from its downside by the screen supporting member 34. Therefore, a barrier member having the screen 32 operating as a filtering element installed at the middle part and having the shield plate 36 installed at the peripheral portion (that is, the inner wall side of the reactor main body 10) is provided in the interior of the reactor main body 10.
  • Such a shield plate 36 as described above prevents the synthesis gas ejected from the distributor 20 from being permitted to pass through downward, differing from the screen 32 having the slits 32a formed therein. Therefore, the catalyst particles 124 can be more efficiently raised upward than by the screen 32, wherein it is possible to effectively disperse the catalyst particles 124 in the slurry 12 in the interior of the reactor main body 10.
  • the screen 32 at a part of the barrier member 30, the liquid-phase component (liquid hydrocarbon 122) in the interior of the reactor main body 10 can be discharged through the liquid hydrocarbon discharge port 14 at the bottom part of the reactor main body 10.
  • the range where the screen 32 is provided that is, the size of the opening 33 of the shield plate 36 is not especially limited. However, it is preferable that the range be determined by taking into consideration the balance between the discharge efficiency of the liquid hydrocarbon 122 and dispersion effect of the catalyst particles 124. Further, a steel plate, aluminum plate, or any optional material may be used as the shield plate 36 as long as the material has such a shape as described above, sufficient mechanical strength and heat-resisting temperature.
  • the catalyst particles 124 are likely to be accumulated at the peripheral portions of the barrier member 30. Therefore, as in the embodiment, if the screen 32 operating as one example of the filtering element is disposed at the middle part of the reactor main body 10, and the shield plate 36 having an excellent dispersion effect for the catalyst particles 124 is disposed at the peripheral portions in the interior of the reactor main body 10, it is possible to further effectively disperse the catalyst particles 124 in the slurry 12.
  • a metal plate such a steel plate may be used as the barrier member 30 without providing any filtering element in the barrier member 30. This case is not substantially different from a reactor of a flat bottom part being used.
  • the barrier member 30 be installed in the range accessible by the flow of the slurry, which is produced by a synthesis gas ejected from the distributor 20.
  • the barrier member 30 may be installed so that the distance between the barrier member 30 and the distributor 20 becomes 30 cm or less, preferably 10 cm or so.
  • the flow of the slurry 12 which is produced by the synthesis gas ejected from the distributor 20
  • the catalyst particles 124 can be sufficiently agitated, and the catalyst particles 124 can be effectively dispersed in the slurry 12.
  • the barrier member 30 is installed parallel to the distributor 20, that is, so as to become parallel to the horizontal plane perpendicular to the height direction of the reactor main body 10.
  • the bottom part of the reactor main body 10 is formed so as to form a curvature as shown in FIG. 2.
  • the synthesis gas ejected from the distributor 20 it becomes difficult for the synthesis gas ejected from the distributor 20 to reach the middle part of the bottom part of the reactor main body 10, wherein the catalyst particles 124 are likely to be accumulated at the bottom part thereof.
  • FIG. 7 through FIG. 9 a description is given of a method for dispersing the catalyst particles 124 according to the embodiment.
  • the configuration of the FT reactor 1 is described, after being simplified for convenience of description.
  • the catalyst particles 124 are accumulated on the barrier member 30 unless a gas introducing nozzle is separately provided and the gas is introduced from downward of the barrier meter 30.
  • the catalyst particles 124 are likely to be accumulated at the peripheral portions of the inner wall side of the reactor main body 10.
  • the distributor 20 is installed at a distance sufficiently close to the barrier member 30, and gas is ejected downward from the distributor 20 toward the barrier member 30, whereby, as shown by the thick arrows in FIG. 8, the catalyst particles 124 that will be accumulated on the barrier member 30 are raised upward, and the catalyst particles 124 are evenly dispersed in the slurry 12 in the interior of the reactor main body 10.
  • such a distributor 200 may be employed as a reaction gas-feeding portion for introducing a synthesis gas, which is provided with a two-stage gas introducing nozzle consisting of an upper-stage introducing nozzle 210 and a lower-stage introducing nozzle 220.
  • the synthesis gas is ejected upward from the upper-stage introducing nozzle 210, and the synthesis gas is ejected from the lower-stage introducing nozzle 220 to at least the barrier member 30 downward.
  • synthesis gas may be ejected upward from the lower-stage introducing nozzle 220 in addition to downward ejecting of the synthesis gas.
  • the catalyst particles 124 raised by the synthesis gas ejected from the lower-stage introducing nozzle 220 to the barrier member 30 can be raised further upward by an air-lift effect based on the synthesis gas ejected by the upper-stage introducing nozzle 210. Therefore, by employing the distributor 200 having two-stage gas introducing nozzles, the dispersion effect of catalyst particles 124 can be further improved compared to the case where a distributor 20 having a single-stage gas introducing nozzle as shown in FIG. 8 is employed, wherein the composition of the produced liquid hydrocarbon 122 can be further stabilized.
  • the FT reactor 1 since gas ejected from the distributor 20 or the lower-stage introducing nozzle 220 of the distributor 200 is introduced onto the barrier member 30, the catalyst particles 124 that will be accumulated on the barrier member 30 are agitated, and dispersion of the catalyst particles 124 in the slurry 12 can be promoted. Therefore, the temperature of the interior of the reactor main body 10 can be maintained more uniform, wherein the composition of the liquid hydrocarbon, which is a product synthesized by the FT reaction, can be stabilized.
  • the barrier member 30 is horizontally provided in the reactor main body 10, and gas is ejected onto the barrier member 30 from the distributor 20 or the lower-stage introducing nozzle 220 of the distributor 200, whereby the dispersion effect of catalyst particles can be increased. That is, since it is not necessary to provide another gas introducing port separately from the distributor as in the prior art in order to increase the effect of dispersing the catalyst particles 124 in the slurry 12, it is possible to simplify the interior structure of the reactor main body 10 and the arrangement of pipes outside the reactor main body 10. Further, since the distributor 20 or the distributor 200 alone is sufficient as a member for introducing gas, it is not necessary to employ a mechanism for adjusting or regulating the flow rate of gas between a plurality of gas introducing nozzles as in the prior art.
  • the shape of the reactor main body 10 is roughly cylindrical.
  • the shape of the reactor main body is not specifically limited as long as the shape is able to upwardly raise catalyst particles which will be accumulated on the barrier member or on the bottom part of the reactor main body and to evenly disperse the catalyst particles in the slurry.
  • the cooling tube 40 is formed so as to reciprocate a plurality of times vertically along the perpendicular direction by bending a single tube.
  • the shape and number of the cooling tubes are not specifically limited.
  • a plurality of a double-tube structure cooling tubes of a so-called "bayonet type" may be disposed in the interior of the reactor.
  • a screen having a plurality of slits formed therein is used as a filtering element included in the barrier member.
  • the filtering element may be, for example, a meshed filter having meshes whose apertures are sufficiently smaller than the size of the catalyst particles.
  • a porous sintered plate may be employed.
  • the present invention is applicable to a bubble column type hydrocarbon synthesis reactor, and particularly to a reactor for carrying out a Fischer-Tropsch synthesis reaction by introducing a synthesis gas into a slurry having solid catalyst particles suspended in a liquid hydrocarbon.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

L'invention concerne un réacteur de synthèse d'hydrocarbures du type colonne à bulles. Ledit réacteur synthétise des hydrocarbures par une réaction chimique d'un gaz dont les constituants principaux sont l'hydrogène et le monoxyde de carbone et d'une suspension épaisse présentant des particules solides de catalyseur en suspension dans un liquide. Ledit réacteur comprend: un corps principal de réacteur destiné à recevoir la suspension épaisse; une partie d'alimentation en gaz de réaction qui est disposée au niveau de la partie inférieure du corps principal de réacteur et alimente le gaz dans la suspension épaisse par éjection dudit gaz; et un élément de barrière qui est disposé à l'avant du sens d'éjection du gaz éjecté depuis la partie d'alimentation en gaz de réaction et limite le flux de la suspension épaisse.
PCT/JP2007/051854 2006-01-30 2007-01-30 Réacteur de synthèse d'hydrocarbures du type colonne à bulles WO2007086612A1 (fr)

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JP2006020659A JP4874660B2 (ja) 2006-01-30 2006-01-30 気泡塔型炭化水素合成反応器
JP2006-020659 2006-01-30

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EP2055375A1 (fr) * 2007-10-25 2009-05-06 Mitsubishi Materials Corporation Buse d'éjection de gaz chlorure d'hydrogène, appareil de réaction et procédé pour la production de trichlorosilane
WO2010058164A1 (fr) * 2008-11-18 2010-05-27 Gtl.F1 Ag, Réacteur à colonne à bulles pour suspension épaisse
CN102441360A (zh) * 2011-09-30 2012-05-09 常熟市申华化工贸易有限公司 一种化工反应器
WO2012080933A1 (fr) 2010-12-13 2012-06-21 Sasol Technology (Proprietary) Limited Appareil pour phase de suspension pâteuse
US8980201B2 (en) 2009-06-26 2015-03-17 Gtl.Fi Ag Apparatus and process for three-phase reaction
WO2015087211A1 (fr) 2013-12-11 2015-06-18 Sasol Technology Proprietary Limited Procédé permettant d'arrêter un réacteur à colonnes à bulles de boue liquide à trois phases de fonctionnement
WO2015099549A3 (fr) * 2013-12-23 2015-10-15 Instituto Superior Técnico Réacteur catalytique pour l'oligomérisation d'oléfines en c4-c7 et procédé d'oligomérisation catalytique faisant intervenir ledit réacteur
US9278891B2 (en) 2008-12-22 2016-03-08 Gtl.F1 Ag Apparatus and method for conducting a fischer-tropsch synthesis reaction

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KR100992835B1 (ko) * 2008-02-29 2010-11-08 한국화학연구원 피셔-트롭쉬 합성반응용 고체촉매와 생성물의 연속분리배출장치 및 방법
AU2009299339B2 (en) 2008-09-30 2013-05-09 Cosmo Oil Co., Ltd. Bubble column reactor and method of controlling bubble column reactor
KR101210397B1 (ko) * 2010-09-17 2012-12-10 한국화학연구원 합성가스로부터 탄화수소를 제조하기 위한 반응장치
JP6145348B2 (ja) 2013-07-30 2017-06-07 新日鉄住金エンジニアリング株式会社 炭化水素合成用の反応器
CN105056844B (zh) * 2015-08-07 2017-04-12 北京华福工程有限公司 一种乙炔加氢制乙烯浆态床的气体分布器及其应用

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Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2055375A1 (fr) * 2007-10-25 2009-05-06 Mitsubishi Materials Corporation Buse d'éjection de gaz chlorure d'hydrogène, appareil de réaction et procédé pour la production de trichlorosilane
US8486339B2 (en) 2007-10-25 2013-07-16 Mitsubishi Materials Corporation Hydrogen chloride gas ejecting nozzle, reaction apparatus for producing trichlorosilane and method for producing trichlorosilane
US8974760B2 (en) 2007-10-25 2015-03-10 Mitsubishi Materials Corporation Hydrogen chloride gas ejecting nozzle, reaction apparatus for producing trichlorosilane and method for producing trichlorosilane
WO2010058164A1 (fr) * 2008-11-18 2010-05-27 Gtl.F1 Ag, Réacteur à colonne à bulles pour suspension épaisse
US9039980B2 (en) 2008-11-18 2015-05-26 Gtl.Fi Ag Slurry bubble column reactor
US9278891B2 (en) 2008-12-22 2016-03-08 Gtl.F1 Ag Apparatus and method for conducting a fischer-tropsch synthesis reaction
US8980201B2 (en) 2009-06-26 2015-03-17 Gtl.Fi Ag Apparatus and process for three-phase reaction
AU2011342806A1 (en) * 2010-12-13 2013-06-27 Sasol Technology (Proprietary) Limited Slurry phase apparatus
WO2012080933A1 (fr) 2010-12-13 2012-06-21 Sasol Technology (Proprietary) Limited Appareil pour phase de suspension pâteuse
AP3958A (en) * 2010-12-13 2016-12-23 Sasol Tech Pty Ltd Slurry phase apparatus
US9937476B2 (en) 2010-12-13 2018-04-10 Sasol Technology (Proprietary) Limited Slurry phase apparatus
US10322393B2 (en) 2010-12-13 2019-06-18 Sasol Technology (Proprietary) Limited Slurry phase apparatus
CN102441360A (zh) * 2011-09-30 2012-05-09 常熟市申华化工贸易有限公司 一种化工反应器
WO2015087211A1 (fr) 2013-12-11 2015-06-18 Sasol Technology Proprietary Limited Procédé permettant d'arrêter un réacteur à colonnes à bulles de boue liquide à trois phases de fonctionnement
US10058838B2 (en) 2013-12-11 2018-08-28 Sasol Technology Proprietary Limited Method of shutting down an operating three-phase slurry bubble column reactor
WO2015099549A3 (fr) * 2013-12-23 2015-10-15 Instituto Superior Técnico Réacteur catalytique pour l'oligomérisation d'oléfines en c4-c7 et procédé d'oligomérisation catalytique faisant intervenir ledit réacteur

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