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WO2013062226A1 - Distributeur de gaz dynamique et réacteur à tour de fractionnement à calottes utilisant celui-ci - Google Patents

Distributeur de gaz dynamique et réacteur à tour de fractionnement à calottes utilisant celui-ci Download PDF

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Publication number
WO2013062226A1
WO2013062226A1 PCT/KR2012/006926 KR2012006926W WO2013062226A1 WO 2013062226 A1 WO2013062226 A1 WO 2013062226A1 KR 2012006926 W KR2012006926 W KR 2012006926W WO 2013062226 A1 WO2013062226 A1 WO 2013062226A1
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WIPO (PCT)
Prior art keywords
bubble
disk
rotating disk
gas distributor
dynamic gas
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/KR2012/006926
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English (en)
Korean (ko)
Inventor
양정훈
정헌
이호태
양정일
김학주
천동현
박지찬
김병권
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.)
Korea Institute of Energy Research KIER
Original Assignee
Korea Institute of Energy Research KIER
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
Priority claimed from KR1020120094731A external-priority patent/KR101399403B1/ko
Application filed by Korea Institute of Energy Research KIER filed Critical Korea Institute of Energy Research KIER
Publication of WO2013062226A1 publication Critical patent/WO2013062226A1/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
    • B01J8/18—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
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/006—Separating solid material from the gas/liquid stream by filtration
    • 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
    • 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
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B01J2208/0092—Perforated plates

Definitions

  • the present invention relates to a bubble column reactor, and more particularly, uniformly converts the bubble particles of the incoming synthesis gas, as well as generating a bubble column by the wake (wake: flow of disturbed air) generated after the bubble particles.
  • the present invention relates to a dynamic gas distributor and a bubble column reactor to which the catalyst is applied so as to increase the catalyst and the reaction efficiency in the reaction body by suppressing the phenomenon.
  • bubble column reactors have the advantages of high heat and mass transfer and are widely used in reactions such as biochemical reactions, wastewater treatment and coal liquefaction.
  • reaction takes place while the gaseous reactants (synthetic gas) pass through a continuous phase consisting of a catalyst and a product.
  • the mass transfer rate through uniform contact and dispersion between the reactant (synthetic gas) and the catalyst is very important as a variable for determining the reaction efficiency.
  • a method of increasing the fluidity in the reactor and a method of increasing the gas collection rate in the continuous phase are mainly utilized.
  • the fluid flow in a bubble column reactor is largely divided into two regions: a uniform flow region and a heterogeneous flow region.
  • the gas capture rate is defined as the volume fraction of the gas phase present in the continuous phase.
  • the ratio of gas capture rate to mass transfer rate of the reactant is constant at about 0.5. Therefore, increasing the gas capture rate is an important variable for increasing the mass transfer rate.
  • the gas collection rate is influenced by the linear velocity of the reactor body, the reactor diameter, the physical properties of the continuous phase, and the like.
  • the rate of bubble rise is closely related to the size and size distribution of the bubble particles.
  • the rate of bubble rise increases in proportion to 0.5 square of the size of the bubble particles.
  • An increase in bubble rise rate is negative in terms of gas capture rate because it leads to a decrease in the time of residence in the reactor for a unit time.
  • the technique of controlling the size of the bubble particles introduced into the reactor is very essential for improving the reactor efficiency.
  • a porous gas distribution plate As a representative example of this, a porous gas distribution plate, a porous gas distribution pipe, a metal foam, and the like can be considered.
  • the bubble column formed at this time is estimated to appear as the wake formed at the rear end of the bubble particle which rises earlier promotes the rate of rise of the bubble particle which follows.
  • the present invention has been made in view of the above problems, and the first object of the present invention is to uniformly convert the bubble particles of the synthesis gas reacting with the catalyst in the reaction body and the Fischer-Tropsch reaction.
  • a dynamic gas distributor and bubble tower reactor employing the same can be used to suppress the phenomenon in which a column of bubbles are generated by a wake generated at the rear of the bubble particles so that the catalyst and reaction efficiency in the reaction body can be enhanced. To provide.
  • the second object of the present invention is to prevent the slurry inside the reaction body from flowing back to the dynamic gas distributor when the reaction body is operated or stopped, as well as maintaining the rotation cycle of the rotating disk to prevent the settling of the slurry.
  • to provide a dynamic gas distributor and a bubble column reactor using the same to stop the backflow of the slurry by stopping the rotating disk at a fixed position to eliminate or minimize the opening ratio of the fixed dispersion disk at the end of the reactor have.
  • the present invention provides a bubble column reactor comprising a reaction base and a dynamic gas distributor.
  • the reactor body stores a slurry containing a catalyst, and reacts with the synthesis gas into which the slurry containing the catalyst is introduced to generate synthetic fuel.
  • the dynamic gas distributor is disposed in communication with the lower portion of the reaction base, dispersing the synthesis gas supplied through the inlet tube in rotation, and converts the dispersed synthesis gas into uniform bubble particles to be supplied into the reaction base body do.
  • the dynamic gas distributor includes a fixed dispersion disk, a mixing cylinder, and gas dispersing means.
  • the fixed dispersion disk is formed with a plurality of opening holes on the surface to convert the bubble particles of the synthesis gas supplied through the inlet pipe to a uniform size.
  • the compounding cylinder extends vertically downward to the edge of the fixed dispersion disk to guide the synthesis gas supplied through the inlet pipe, and mixes it with a constant composition and pressure.
  • the gas dispersing means disperses the synthesis gas introduced into the compounding cylinder in rotation to provide the fixed dispersion disk.
  • the gas dispersing means includes a rotating disk and a driving means.
  • the rotating disk is spaced apart from the lower portion of the fixed dispersion disk to control the opening and closing period of the opening hole.
  • the driving means is disposed outside the compounding barrel to rotate the rotating disk.
  • the rotating disk is a semi-circular disk, a plurality of arc-shaped disks are formed symmetrically with each other, a semi-circle disk with a plurality of opening holes, a plurality of openings are formed and a plurality of arc-shaped disks are formed symmetrically It may be any one selected from the circular disk in which the opening hole is formed.
  • the opening ratio of the rotating disk may range from 10 to 90% of the circular disk.
  • the material of the rotating disk is any one selected from iron, copper, nickel, nickel-chromium alloy and iron-chromium-aluminum alloy, which is a hydrophobic material having a contact angle with water of 80 ° or more. It can be one.
  • the driving means may be a magnetic mixer capable of operating at 50 atm or less.
  • the distance between the fixed dispersion disk and the rotating disks spaced apart from each other may be in the range of 0.01 mm to 10 mm.
  • the rotation speed of the rotating disk may be proportional to the linear velocity of the syngas gas.
  • At least one rotating disk may be installed in the mixing barrel.
  • At least one of the inlet pipes may be connected to a side surface of the mixing vessel below the portion where the rotating disk is installed.
  • the size of the aperture diameter of the fixed dispersion disk is in the range of 0.1 ⁇ 2mm, the opening ratio may be in the range of 0.05 ⁇ 2.0%.
  • the catalyst contained in the slurry in the reaction base is iron, cobalt, copper, potassium, cesium, sodium, molybdenum, tungsten, zinc, nickel, rubidium, having a particle size distribution of 0.1 ⁇ 200um, It may be configured by mixing one or more kinds selected from the group consisting of rhodium and palladium.
  • the bubble column reactor according to the present invention further includes filtering means which is disposed above the inside of the reaction base to filter the catalyst and to discharge only the synthetic fuel produced by the reaction to the outside of the reaction base.
  • the upper end of the reaction base may be connected to an outlet pipe for outflowing the unreacted synthesis gas and the chemical gas generated during the reaction to the outside of the reaction base.
  • the present invention also includes a mixing vessel, a gas dispersing means, and a fixed dispersing disk as a dynamic gas distributor installed in communication with the reaction base of the bubble column reactor.
  • the compounding vessel has an open portion formed at an upper portion thereof to be connected to the reaction base, and temporarily stores the synthesis gas introduced through the inlet pipe and mixes the same at a constant composition and pressure.
  • the gas dispersing means disperses the synthesis gas introduced into the mixing vessel by rotation.
  • the fixed dispersion disk is coupled to the opening of the mixing cylinder, and a plurality of opening holes are formed on the surface to convert the bubble particles of the synthesis gas dispersed by the gas dispersing means into a uniform size.
  • a wake generated at the rear end of the bubble particles as well as uniformly converting the bubble particles of the synthesis gas reacting with the catalyst in the reaction body and the Fischer-Tropsch reaction. (wake: disturbed flow of air) by suppressing the phenomenon that the bubble column is generated there is an effect that can increase the catalyst and the reaction efficiency in the reaction base.
  • FIG. 1 is a block diagram of a bubble column reactor to which a dynamic gas distributor according to the present invention
  • FIG 2 is a perspective view of the dynamic gas distributor extracted in Figure 1,
  • Figure 7 is a photograph showing the bubble particles discharged from the fixed dispersion disk of the bubble column reactor according to a comparative example
  • FIG. 8 is a conceptual diagram showing the bubble particles of the bubble column reactor to which the dynamic gas distributor according to the present invention
  • FIG. 9 is a photograph showing bubble particles discharged from the fixed dispersion disk of the bubble column reactor in FIG. 8.
  • FIG. 1 is a block diagram of a bubble column reactor to which a dynamic gas distributor according to the present invention is applied
  • FIG. 2 is a perspective view of a dynamic gas distributor extracted from FIG. 1
  • FIG. 3 is a diagram showing various embodiments of a rotating disk according to the present invention.
  • 5 is a diagram illustrating various embodiments of the inlet pipe connected to the mixing vessel according to the present invention
  • FIG. 6 is another embodiment of the gas dispersing means according to the present invention.
  • the present invention by controlling the bubble particles of the synthesis gas in Fischer-Tropsch reaction with the catalyst in the reaction body 10, the reaction body 10
  • the present invention relates to a bubble column reactor (100) employing a dynamic gas distributor (20) having a structure capable of improving mass transfer and reaction efficiency of a catalyst and synthesis gas.
  • the bubble column reactor 100 to which the dynamic gas distributor 20 is applied is merged with a wake (flow: disturbed air flow) generated at the rear end of the bubble particles uniformly converted through the dynamic gas distributor 20 to generate a bubble column. It is a configuration including a gas dispersing means 23 that rotates to prevent the phenomenon.
  • the bubble column reactor 100 to which the dynamic gas distributor 20 of the present invention is applied is largely composed of three parts, which is a reaction body 10 having a filtering means 30, an outlet pipe 11, and a reaction body ( 10 is disposed below the dynamic gas distributor 20 for converting the synthesis gas flowing through the inlet tube 24 into uniform particles.
  • the reaction base 10 has a structure in which a slurry (oil and wax) containing a catalyst for reacting with a synthesis gas and a Fischer-Tropsch reaction is stored.
  • the catalyst contained in the slurry stored in the reaction body 10 is active for the Fischer-Tropsch reaction and the water gas shift reaction, depending on the components of the synthetic fuel obtained, iron, cobalt, copper, potassium , Cesium, sodium, molybdenum, tungsten, zinc, nickel, rubidium, rhodium, palladium from the group consisting of one or two or more may be mixed.
  • the catalyst has a particle size distribution of 0.1um ⁇ 200um in order to spray evenly in the reaction base (10). If the particle size is smaller than 0.1 ⁇ m, this may cause the outflow of the catalyst because it is not filtered by the filtering means 30. If the particle size is larger than 200 ⁇ m, precipitation of the catalyst is strongly observed and the catalyst in the reaction body 10 is increased. It is not preferred because the even dispersion of the particles is difficult.
  • the filtering means 30 discharges the synthetic fuel produced by the Fischer-Tropsch reaction and the catalyst functions to filter.
  • the filtering means 30 is disposed above the inside of the reaction body 10 to filter the catalyst and to discharge only the synthetic fuel produced by the reaction to the outside.
  • the filtering means 30 may be made of a general stainless steel material, the pore size may be configured in the range of 0.1um ⁇ 10um, most preferably the pore size of 1um. When the filtering means 30 having a pore size of 1 ⁇ m is used, the catalyst particles in the reaction body 10 may be filtered and selectively only the synthetic fuel may be collected.
  • the outlet pipe 11 functions to discharge the unreacted syngas and the chemical gas (methane, propane, pentane, etc.) generated by the reaction in the reaction body (10).
  • the chemical gas and the synthetic fuel are similar in that they are all products of the Fischer-Tropsch reaction, but the chemical gas has a gaseous form under the reaction conditions, and the synthetic fuel has a liquid form. There is a difference.
  • the dynamic gas distributor 20 is connected to the lower portion of the reaction base 10 so that the bubble particles of the synthesis gas supplied through the inlet pipe 24 can be converted into uniform bubble particles and supplied into the reaction base 10.
  • the structure is arranged.
  • the dynamic gas distributor 20 includes a fixed dispersion disk 21, a mixing cylinder 22 and a gas dispersing means 23.
  • the mixing barrel 22 extends vertically downward to the edge of the fixed dispersion disk 21, and the inlet pipe 24 is connected.
  • the gas dispersing means 23 includes a rotating disk 231 embedded in the compounding barrel 22 and driving means 232 disposed outside the compounding barrel 22 to rotate the rotating disk 231. .
  • the fixed dispersion disk 21 has a plurality of opening holes (H) formed on the surface to function to convert the bubble particles of the synthesis gas supplied through the inlet pipe 24 to a uniform size.
  • the diameter of the aperture H of the fixed dispersion disk 21 is in the range of 0.1 mm to 2 mm, and the aperture ratio is preferably in the range of 0.05 to 2.0%.
  • the opening ratio of the opening hole H is 2.0% or more, even injection of the synthesis gas into the inside of the reaction body 10 becomes difficult, so that it is preferable to limit the opening ratio within the range of 0.05 to 2.0%.
  • the syngas having a uniform particle distribution provides sufficient fluidity in the continuous phase of the reaction body 10 to increase contact with the catalyst and slurry. Not only can the production yield of syngas be increased, but the heat of reaction by the Fischer-Tropsch exothermic reaction can be evenly released to the outside.
  • the compounding cylinder 22 is integrally coupled with the fixed dispersion disk 21, and more specifically, has a structure extending vertically downward to the edge of the fixed dispersion disk 21. That is, the compounding barrel 22 has an opening portion 221 formed at a portion connected to the reaction body 10, and the fixed dispersion disk 21 is coupled to the compounding cylinder 22 so as to cover the opening portion 211. do.
  • the compounding barrel 22 functions to temporarily store the synthesis gas introduced through the inlet pipe 24 to be mixed at a constant composition and pressure.
  • the inlet tube 24 is provided with a flow rate control unit 40 for adjusting the flow rate of the synthesis gas, and a flow meter 50 for checking the flow rate of the gas in real time to select the synthetic fuel obtained by the reaction with the catalyst Can improve the degree.
  • the inflow pipe 24 showed the example in which one was provided toward the center of the mixing barrel 22 like FIG. 2, it is not limited to this.
  • the inlet pipe 24 may be provided in plural in the mixing barrel 22.
  • the plurality of inflow pipes 24 are exposed inwardly of the compounding barrel 22 through the side surface of the compounding barrel 22 in a direction deviated at a predetermined angle from the center of the compounding barrel 22. Can be installed.
  • the plurality of inflow pipes 24 may be inserted into the mixing cylinder 22 to protrude, and the ends may be bent to one side.
  • the inlet pipe 24 to the mixing vessel 22
  • the synthesis gas flowing into the mixing vessel 22 can be more uniformly dispersed.
  • the gas dispersing means 23 is installed in the lower portion of the fixed dispersion disk 21 is a wake (wake) that is generated in the rear end of the bubble particles converted into uniform particles through the opening hole (H) of the fixed dispersion disk 21 Merged with the disturbed air flow) to prevent the occurrence of bubble columns.
  • the gas dispersing means 23 is disposed at the lower portion of the fixed dispersing disk 21 to be disposed outside of the mixing cylinder 22 and the rotating disk 231 for adjusting the opening / closing period of the opening hole H. And a driving means 232 for rotating the rotating disk 231.
  • the rotating disk 231 is a semicircular disk, a plurality of arc-shaped disks are formed symmetrically, a plurality, as shown in Figs. 3 and 4 (a) (b) (c) (d) (e) (f) (g) A semicircular disk formed with an opening hole of a plurality of opening holes are formed, a plurality of arc-shaped disks are formed symmetrically and a plurality of circular holes formed with a plurality of opening holes.
  • the opening ratio of the rotating disk 231 is preferably in the range of 10 to 90% of the total size of the rotating disk 231, which is compounded when the shape of the rotating disk 231 is irregular or the opening ratio is smaller than 10%.
  • Unstable fluctuations occur in the pressure inside the cylinder 22, and a drift appears in the flow of the synthesis gas flowing into the reaction body 10, and the occurrence of this drift is caused by a gas collection rate in the reaction body 10. It is not preferable because it leads to a result of lowering the reaction efficiency because it sharply lowers.
  • the opening ratio of the rotating disk 231 is larger than 90%, the effect of suppressing the occurrence of the bubble column by the rotating disk 231 is not so preferable.
  • the rotation speed of the rotating disk 231 is proportional to the linear velocity of the syngas gas. Therefore, if the linear velocity of the incoming syngas gas is high, the wake becomes large to speed up the rotational speed of the rotating disk, and if the linear velocity of the syngas gas is low, the wake is small and the rotational speed of the rotating disk 231 is preferable.
  • the material of the rotating disk 231 is preferably any one selected from iron, copper, nickel, nickel-chromium alloy, iron-chromium-aluminum alloy, which is a hydrophobic material having a contact angle with respect to water of 80 ° or more.
  • the rotational speed of the rotating disk 231 is preferably 10,000rpm or less, which means that when the rotational speed is 10,000rpm or more, the unit time through which the small bubbles can pass through the opening hole H is smaller than the opening and closing unit time of the pore. It is not preferable because the synthesis gas cannot pass through the opening hole H of the fixed dispersion disk 21, and as a result, the pressure inside the compounding barrel 22 rises.
  • the rotating disk (231) 10,000rpm If you adjust the rotation speed below It is possible to minimize the generation of the bubble column by the wake effect and to control the size of the generated bubble particles.
  • the driving means 232 may be composed of an electric motor, and more preferably, it is preferably composed of a magnetic mixer for rotating the rotating disk 231 at a constant speed.
  • This magnetic mixer is a device that operates at 50 atm or less, and can control the rotation speed constantly.
  • the magnetic mixer can stably rotate the rotating disk 231.
  • the rotating disk 231 blocks the opening hole H of the fixed dispersion disk 21 to drive or stop the reaction body 10 when the slurry inside the reaction body 10 flows back to the dynamic gas distributor 20.
  • the rotation period of the rotating disk 231 can be kept constant to prevent the settling of the slurry, and when the reactor 100 is terminated, the rotating disk 231 is stopped and fixed at a fixed position. The backflow of the slurry can be prevented by eliminating or minimizing the aperture ratio of the dispersion disk 21.
  • the rotating disk 231 is installed in close proximity to the fixed dispersion disk 21 so that the opening and closing period of the opening hole H of the fixed dispersion disk 21 can be stably adjusted.
  • the distance between the fixed dispersion disk 21 and the rotating disk 231 spaced apart from the lower portion is preferably in the range of 0.01mm ⁇ 10mm.
  • the distance between the fixed dispersion disk 21 and the rotating disk 231 is 0.01 mm or less because it prevents the gas of the synthesis gas flowing through the fixed dispersion disk 21, and in the case of 10 mm or more. It is not preferable because the wake occurs again on a spaced gap.
  • Inlet tube 24 is connected to the lower portion of the mixing barrel 22 than the position.
  • the rotating disk 231 has been disclosed an example in which one is provided in the mixing barrel 22, but is not limited thereto.
  • a plurality of rotating disks 231a and 231b may be installed in the compounding barrel 22.
  • the plurality of rotating disks 231a and 231b may be installed above the inlet pipe 24.
  • the bubble tower reactor 100 having the dynamic gas distributor 20 according to the present invention and the bubble tower reactor according to the comparative example in which only the fixed dispersion disc is simply installed in the mixing cylinder will be described as follows.
  • FIG. 7 is a photograph showing bubble particles discharged from the fixed dispersion disk 121 of the bubble column reactor according to the comparative example.
  • FIG. 8 is a conceptual diagram illustrating bubble particles of the bubble column reactor to which the dynamic gas distributor 20 is applied
  • FIG. 9 is a photograph showing bubble particles discharged from the fixed dispersion disc 21 of the bubble column reactor in FIG. 8.
  • the present comparative example does not have a separate gas dispersing means, it can be confirmed that the size of the formed bubbles is not uniform.
  • the inlet synthesis gas is not converted into uniform bubble particles through the opening of the fixed dispersion disc 121 and merges with a wake (wake: flow of disturbed air) generated at the rear end. It can be seen that rounds are generated.

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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)

Abstract

La présente invention concerne un distributeur de gaz dynamique et un réacteur à tour de fractionnement à calottes utilisant celui-ci, dans lequel un gaz synthétique est uniformément converti en particules de bulles uniformes, et un phénomène de génération d'une colonne de bulles par un sillage (flux d'air perturbé) généré aux extrémités arrière des particules de bulle est prévenu de manière à obtenir une efficacité de réaction améliorée dans un corps de réacteur. Le réacteur à tour de fractionnement à calottes selon la présente invention comprend un corps de réacteur et un distributeur de gaz dynamique. Le corps de réacteur stocke dans celui-ci une suspension concentrée contenant un catalyseur, et génère un combustible synthétique par l'intermédiaire de la réaction de la suspension concentrée contenant un catalyseur et un gaz synthétique. Le distributeur de gaz dynamique est configuré de manière à communiquer avec une partie inférieure du corps de réacteur, se disperse par une rotation du gaz synthétique s'écoulant à travers un tube d'entrée, convertit le gaz synthétique dispersé en particules de bulles uniformes et transfère les particules de bulles à l'intérieur du corps de réacteur.
PCT/KR2012/006926 2011-10-27 2012-08-30 Distributeur de gaz dynamique et réacteur à tour de fractionnement à calottes utilisant celui-ci Ceased WO2013062226A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
KR20110110225 2011-10-27
KR10-2011-0110225 2011-10-27
KR10-2012-0094731 2012-08-29
KR1020120094731A KR101399403B1 (ko) 2011-10-27 2012-08-29 동적 기체분배기 및 그를 적용한 기포탑 반응기

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* Cited by examiner, † Cited by third party
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CN103803712A (zh) * 2014-01-28 2014-05-21 辽宁工业大学 一种白腐真菌降解造纸废水的鼓泡塔反应器
CN108854859A (zh) * 2018-07-27 2018-11-23 中化蓝天霍尼韦尔新材料有限公司 一种悬浮液气液相反应装置及运行方法
CN112705060A (zh) * 2020-12-15 2021-04-27 燕山大学 旋转式多直径气泡发生装置
CN117954652A (zh) * 2023-12-21 2024-04-30 青岛理工大学 一种燃料电池测试台增湿系统
CN119869373A (zh) * 2023-10-25 2025-04-25 国家能源投资集团有限责任公司 一种具有均匀气含率分布的浆态床反应器

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JPH10216501A (ja) * 1997-01-31 1998-08-18 Nkk Corp スラリー床反応器
US5905094A (en) * 1997-10-21 1999-05-18 Exxon Research And Engineering Co. Slurry hydrocarbon synthesis with reduced catalyst attrition and deactivation
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KR20120033623A (ko) * 2010-09-30 2012-04-09 한국에너지기술연구원 복합 반응이 가능한 ｆ-ｔ 기포탑 반응기

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Publication number Priority date Publication date Assignee Title
JPH10216501A (ja) * 1997-01-31 1998-08-18 Nkk Corp スラリー床反応器
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CN103803712A (zh) * 2014-01-28 2014-05-21 辽宁工业大学 一种白腐真菌降解造纸废水的鼓泡塔反应器
CN108854859A (zh) * 2018-07-27 2018-11-23 中化蓝天霍尼韦尔新材料有限公司 一种悬浮液气液相反应装置及运行方法
CN108854859B (zh) * 2018-07-27 2023-08-18 中化蓝天霍尼韦尔新材料有限公司 一种悬浮液气液相反应装置及运行方法
CN112705060A (zh) * 2020-12-15 2021-04-27 燕山大学 旋转式多直径气泡发生装置
CN119869373A (zh) * 2023-10-25 2025-04-25 国家能源投资集团有限责任公司 一种具有均匀气含率分布的浆态床反应器
CN117954652A (zh) * 2023-12-21 2024-04-30 青岛理工大学 一种燃料电池测试台增湿系统
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