WO2020230348A1 - Réacteur - Google Patents

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Publication number
WO2020230348A1
WO2020230348A1 PCT/JP2019/042825 JP2019042825W WO2020230348A1 WO 2020230348 A1 WO2020230348 A1 WO 2020230348A1 JP 2019042825 W JP2019042825 W JP 2019042825W WO 2020230348 A1 WO2020230348 A1 WO 2020230348A1
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Prior art keywords
reaction
raw material
material liquid
gas
oxidation
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Application number
PCT/JP2019/042825
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English (en)
Japanese (ja)
Inventor
小黒　秀一
海野　洋
Original Assignee
日揮株式会社
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Publication of WO2020230348A1 publication Critical patent/WO2020230348A1/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
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • 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
    • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
    • B01J31/04—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing carboxylic acids or their salts
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/20—Catalysts, in general, characterised by their form or physical properties characterised by their non-solid state
    • B01J35/27—Catalysts, in general, characterised by their form or physical properties characterised by their non-solid state in a liquid or molten state
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
    • C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C53/00—Saturated compounds having only one carboxyl group bound to an acyclic carbon atom or hydrogen
    • C07C53/08—Acetic acid

Definitions

  • the present invention relates to a technique for advancing an oxidation reaction by bringing a raw material and an oxidizing agent into contact with each other.
  • a bubble tower reactor is known as a gas-liquid two-phase reactor in which a gas and a liquid are brought into contact with each other to proceed with a reaction.
  • the more increases the gas-liquid contact area (a) can be expected to improve the reaction rate by increasing the mass transfer capacity coefficient (k L a) (k L is Ekisakaimaku transfer coefficient ).
  • Patent Document 1 pressurized water supplied from a pressurized water pump and dissolved gas supplied from a gas compressor are mixed in a pressurized dissolution tank and then discharged from a releaser provided in a bubble tower reactor to form micro-nano bubbles.
  • the technology to generate the gas is described.
  • Patent Document 1 does not describe a technique for improving the reaction rate of the reaction while solving the problem of carrying out the oxidation reaction in the bubble column reactor.
  • the present invention has been made under such a background, and provides a technique for efficiently advancing the oxidation reaction between the raw material liquid and the oxidizing gas under stable reaction conditions.
  • the reactor of the present invention is a reactor for bringing the raw material and the oxidizing agent into contact with each other to proceed with the oxidation reaction.
  • the reactor may have the following features.
  • A) The fine bubble forming portion distributes and supplies fine bubbles of the oxidizing gas within a range of 100 ⁇ m or less in average to the raw material liquid.
  • B) The flow path forming member is a perforated plate in which a plurality of holes, which are the flow passages, are formed, and a plurality of the perforated plates are formed in the reaction vessel along the flow direction of the mixed fluid. Must be spaced apart from each other. A cooling unit for cooling the mixed fluid after flowing through the pores of the perforated plate is provided.
  • C) The flow path forming member is a plurality of reaction tubes, and each reaction tube constitutes the reaction vessel.
  • the mixed fluid is cooled by accommodating the plurality of reaction tubes and providing a shell-type container that forms a shell space partitioned from the inside of these reaction tubes and allowing a coolant to flow in the shell space.
  • the reaction vessel is filled with a solid catalyst for advancing the oxidation reaction.
  • the raw material liquid contains a catalytic substance for advancing the oxidation reaction.
  • the present invention uses a flow path forming member in which a mixed fluid is divided into a plurality of flow paths and circulated when the oxidation reaction is carried out using a mixed fluid in which an oxidizing gas is dispersed in a raw material liquid in the state of fine bubbles. Therefore, it is possible to carry out a treatment suitable for stabilizing the reaction conditions of the oxidation reaction and improving the reactivity.
  • the oxidation reaction involves a large amount of heat generation, deheat treatment may be required.
  • a slow heating mechanism is provided for the bubble tower reactor, it is necessary to slow down the heat while maintaining a uniform gas-liquid mixed state, which is peculiar to the bubble tower reactor that carries out an oxidation reaction.
  • the inventors of the present application supply the oxidative gas in the form of fine bubbles to the raw material liquid, and distribute the mixed fluid in a plurality of flow passages while taking measures according to each of the above-mentioned problems. , It was found that it is possible to proceed with the oxidation reaction.
  • the configuration of the bubble tower reactor 1a according to the first embodiment will be described with reference to FIG.
  • the raw material liquid supply pipe 11 which is a raw material liquid supply unit and the oxidation gas supply pipe 12 which is an oxidation gas supply unit are connected to the lower side of the tower-shaped reaction tower 10 to react.
  • the production liquid extraction pipe 13 and the gas extraction pipe 14 are connected to the upper side of the tower 10.
  • a plurality of perforated plates 21 which are flow path forming members are provided at intervals from each other along the height direction thereof. For example, focusing on the reaction tower of a bubble tower reactor, a large industrial device having a liquid capacity of more than 100 m 3 has been put into practical use from a small device having a diameter of several cm.
  • the raw material liquid supply pipe 11 supplies the raw material liquid toward the space below the lowermost perforated plate 21.
  • a case where a mixed solution of acetaldehyde as a raw material and acetic acid as a diluent is supplied as a raw material solution can be exemplified.
  • the raw material liquid may contain a catalytic substance for advancing the oxidation reaction as a uniform catalyst.
  • the oxidation gas supply pipe 12 supplies the oxidation gas toward the space on the lower side of the lowermost perforated plate 21.
  • the micro-bubble generator 121 which is the micro-bubble forming portion of this example, is inserted from the connection position of the oxidation gas supply pipe 12 to the reaction tower 10 toward the internal space of the reaction tower 10.
  • the micro-bubble generator 121 supplies the oxidation gas in the form of fine bubbles to the raw material liquid supplied from the raw material liquid supply pipe 11 into the reaction tower 10.
  • the bubble diameter range is not particularly limited as long as the fine bubbles are difficult to coalesce with each other and the buoyancy acting on each fine bubble can be suppressed sufficiently small.
  • the microbubble generator 121 of this example can form microbubbles having a bubble diameter distribution called microbubbles having an average bubble diameter of 100 ⁇ m or less. There is no particular lower limit for the average bubble diameter of microbubbles.
  • the microbubbles may be, for example, ultrafine bubbles having an average bubble diameter of less than 1 ⁇ m.
  • the configuration of the micro-bubble generator 121 a case where a tubular porous body having a sealed tip is used can be exemplified.
  • the constituent material of the porous body include ceramics, porous glass, and sintered metal.
  • the plurality of perforated plates 21 are within a height range between the raw material liquid supply position from the raw material liquid supply pipe 11 and the oxidation gas supply position from the microbubble generator 121, and the production liquid extraction pipe 13. Provided. These perforated plates 21 are arranged at preset intervals in a direction intersecting the flow of the mixed fluid from the lower side to the upper side of the reaction column 10.
  • the number of perforated plates 21 to be installed is not particularly limited, but several to several tens of perforated plates 21 are provided depending on the height of the reaction tower 10 and the design reaction conversion rate of the raw material.
  • Each perforated plate 21 is formed with a plurality of holes 211 having a diameter of, for example, about 1 mm to 20 mm. Each hole 211 constitutes a flow path for the mixed fluid.
  • the number of holes 211 formed in each perforated plate 21 is not particularly limited, but the aperture ratio indicating the ratio of the total value of the opening areas of the holes 211 to the total area of the perforated plates 21 is in the range of 1 to 40%. An example can be described in which the opening diameter and the numerical aperture of the hole 211 are adjusted so as to have a value within.
  • a production liquid extraction pipe 13 for extracting the production liquid obtained by reacting the raw material liquid and the oxidizing gas in the reaction tower 10, and exhaust gas from the top of the reaction tower 10. Is connected to the gas extraction pipe 14 for extracting the gas.
  • a mixed solution of acetaldehyde and acetic acid whose acetic acid concentration has increased due to the oxidation reaction is extracted as a production solution. Further, as the exhaust gas, unreacted oxidizing gas (oxygen gas) is extracted.
  • the bubble tower reactor 1a of this example is provided with a cooling unit for removing the reaction heat generated when the oxidation reaction proceeds.
  • the cooling unit of this example is configured as a jacket type cooler 3 in which a jacket through which cooling water (cooling liquid) flows is arranged so as to cover the side wall surface of the reaction tower 10.
  • the cooling water is supplied from the cooling water supply unit 31 connected to the lower side, and the cooling water flows along a flow path (not shown) formed in the jacket type cooler 3.
  • the mixed fluid inside is cooled through the side wall surface of the reaction tower 10.
  • the coil type cooler 3a is submerged in the liquid as shown in FIG. 4 described later. May be installed.
  • the raw material liquid supplied from the raw material liquid supply pipe 11 is blown with fine bubbles of the oxidation gas supplied from the microbubble generator 121, the raw material liquid and the oxidation occur.
  • a mixed fluid with the gas is formed.
  • the raw material liquid and the oxidizing gas come into contact with each other at the interface of each bubble, and the oxidation reaction of the raw material substance contained in the raw material liquid proceeds.
  • the mixed fluid flows in the reaction tower 10 from the lower side to the upper side while the oxidation reaction accompanying gas-liquid contact proceeds inside the mixed fluid. Then, when the arrangement position of the perforated plate 21 is reached, the mixed fluid is divided into a plurality of hole portions 211 which are flow passages, flows through each of the pore portions 211, and then merges on the upper surface side of the perforated plate 21. In this way, when passing through the plurality of perforated plates 21 arranged at intervals from each other, the branching and merging of the mixed fluids are repeated.
  • reaction stage the space sandwiched between the two perforated plates 21 arranged one above the other (hereinafter referred to as "reaction stage"). ) And the reverse mixing between the adjacent reaction stages are suppressed, and a concentration distribution close to the piston flow can be formed.
  • the raw material material is used. It is possible to improve the reaction conversion rate from to the reaction product.
  • the heat of reaction generated as the oxidation reaction progresses while passing through each of the perforated plates 21 is removed by the jacket type cooler 3 provided on the outer surface side of the reaction tower 10.
  • microbubbles such as microbubbles are in a state in which the bubbles are difficult to coalesce with each other.
  • a large gas pool is less likely to be formed on the lower surface of each perforated plate 21 as compared with the millibubble.
  • Each bubble rides on the flow of the mixed fluid while maintaining the state of fine bubbles, and flows in the reaction column 10 from the lower side to the upper side. Even if a flammable air-fuel mixture is formed in the fine bubbles and the combustion reaction proceeds, the energy generated by the combustion is small because each fine bubble is extremely small, and the combustion does not propagate.
  • the fine bubbles when the fine bubbles reach the free interface between the gas pool formed on the upper side of the reaction tower 10 and the mixed fluid, they burst and unreacted oxidized gas is released.
  • the liquid (production liquid) from which the bubbles are discharged is discharged to the outside through the production liquid extraction pipe 13. Further, the gas in the gas pool is discharged to the outside as exhaust gas through the gas extraction pipe 14. If it is difficult for the fine bubbles to coalesce to form a gas pool, as shown in FIG. 2 to be described later, the mixed fluid is extracted from the bubble tower reactor 1b and installed downstream of the bubble tower reactor 1b. Gas and liquid may be separated in a liquid separator (not shown). Further, in order to suppress the formation of a flammable air-fuel mixture in the gas pool, an inert gas such as nitrogen gas may be supplied to the gas pool.
  • the mass transfer capacity coefficient (k La ) is increased by supplying an oxidizing gas in the state of fine bubbles to the raw material liquid to improve the reaction rate. Can be done. Further, by using the perforated plate 21 in which a plurality of holes 211 which are flow passages are formed and repeating branching and mixing of the mixed fluid, a state close to the piston flow can be formed and the reaction conversion rate can be improved. Further, since the oxidation gas is supplied in the state of fine bubbles at this time, the formation of a gas pool of the flammable air-fuel mixture on the lower surface side of the perforated plate 21 can be suppressed.
  • the use of fine bubbles facilitates the design of the perforated plate 21.
  • the pore diameter of the perforated plate 21 needs to reduce the pressure loss so that a gas pool is not formed in consideration of the bubble diameter to be used, so that the rectifying effect tends to be insufficient.
  • fine bubbles the formation of gas pools can be suppressed and the rectifying effect can be obtained, so that the degree of freedom in designing the perforated plate 21 is improved.
  • fixed tube plates 221 are arranged at positions on the lower side and the upper side in the reaction tower 10 configured in the same manner as the above-mentioned bubble tower reactor 1a, and these fixed tube plates are arranged.
  • a plurality of reaction tubes 22 extending in the height direction of the reaction tower 10 are provided so as to connect the 221s.
  • the raw material liquid supply pipe 11 is connected to the bottom of the reaction tower 10, and between the raw material liquid discharge port in the raw material liquid supply pipe 11 and the fixed pipe plate 221 on the lower side.
  • the micro-bubble generator 121 is arranged at the height position.
  • a production liquid extraction pipe 13 from which the mixed fluid containing the production liquid is extracted is connected to the top of the reaction tower 10.
  • Each reaction tube 22 is composed of straight tubes having an outer diameter of about 10 mm to 60 mm, and several to several hundreds are provided depending on the diameter of the reaction tower 10.
  • each of the reaction tubes 22 constitutes a reaction vessel.
  • the plurality of reaction tubes 22 correspond to a flow path forming member that forms a flow path through which the mixed fluid is separated and flows.
  • the space inside the reaction tower 10 (shell type container) in the region sandwiched between the upper and lower fixed tube plates 221 constitutes a shell space 30 partitioned from the inside of each reaction tube 22.
  • the raw material liquid supplied from the raw material liquid supply pipe 11 is blown with fine bubbles of the oxidizing gas supplied from the microbubble generator 121, the raw material liquid is blown into the raw material liquid.
  • the point that a mixed fluid of and the oxidizing gas is formed is the same as that of the bubble tower reactor 1a described with reference to FIG.
  • the mixed fluid When the mixed fluid reaches the arrangement position of the fixed tube plate 221 on the lower side, it separates and flows into a plurality of reaction tubes 22, and the oxidation reaction proceeds inside these reaction tubes 22.
  • the heat of reaction generated by the oxidation reaction is removed by the cooling water flowing through the shell space 30 formed on the outer surface side of each reaction tube 22.
  • the mass transfer capacity coefficient (kLa) can be increased and the reaction rate can be improved by supplying the oxide gas in the state of fine bubbles to the raw material liquid.
  • a state close to the piston flow can be formed and the reaction conversion rate can be improved.
  • the conversion rate can be improved, the reaction tube 22 can be downsized, or the processing amount can be increased, which is the same as that of the bubble column reactor 1a of FIG.
  • FIG. 3 shows an example of a heterogeneous catalyst system in which the reaction tube 22 is filled with the solid catalyst 4.
  • the reaction tube 22 is filled with, for example, a pellet-shaped solid catalyst 4.
  • the outflow of the solid catalyst 4 from the reaction tube 22 can be suppressed by arranging a wire mesh 212 having a mesh diameter smaller than that of the pellets in the openings on the lower end side and the upper end side of the reaction tube 22.
  • the method of cooling the mixed fluid is carried out in a jacket type cooler 3 provided so as to cover the side wall surface of the reaction tower 10 shown in FIG. 1 or in a shell space 30 accommodating a plurality of reaction tubes 22 shown in FIG. It is not limited to the method of circulating cooling water.
  • a coil type cooler 3a is provided in the space (reaction stage) sandwiched between the upper and lower perforated plates 21, and the cooling water supplied from the cooling water supply unit 31 is used.
  • the mixed fluid in the reaction stage may be cooled.
  • the bubble column reactor 1e shown in FIG. 5 shows a modified example in which the perforated plate 21 and the plurality of reaction tubes 22 are alternately arranged along the height direction of the reaction column 10.
  • the mixed fluid can be agitated and mixed using the perforated plate 21, and the reaction tube 22 can be used.
  • a desired process such as cooling using the shell space 30 can be performed.
  • microbubble generator 121 for forming microbubbles using a porous body is shown, but the microbubble forming portion is shown.
  • the configuration is not limited to this example.
  • fine bubbles may be formed by using a swirling flow type microbubble generator in which the oxide gas is tangentially merged with respect to the flow direction of the raw material liquid so as to form a swirling flow.
  • the oxidation reaction carried out by using the above-mentioned bubble tower reactors 1a to 1e is not limited to the above-mentioned example of the formula (1).
  • the production of cumene hydroperoxide (an intermediate substance in the production of phenol and acetone) by the oxidation of cumen the production of acetic acid and methyl ethyl ketone by the oxidation of butane, the production of benzoic acid by the oxidation of toluene, and the production of aldehydes and ketones by the oxidation of alcohol.
  • the bubble column reactors 1a to 1e of this example can be applied to various oxidation reactions such as production.
  • oxygen gas 100 vol% of 1.24 NL / min was supplied as an oxidation gas from a porous body fine bubble generating sparger (fine bubble forming portion).
  • the average bubble diameter of the fine bubbles generated at this time is about 50 ⁇ m.
  • water was supplied as a coolant between the outer pipe and the inner pipe.
  • Example 1 (Example corresponding to the bubble column reactor 1a in FIG. 1)
  • An inner tube using a 1.0 m long double tube type bubble tower reactor 1a consisting of an inner tube with an inner diameter of 45.3 mm and an outer diameter of 48.6 mm and an outer tube with an inner diameter of 57.2 mm and an outer diameter of 60.5 mm.
  • Three perforated plates having a hole diameter of 5 mm and an aperture ratio of 20% were inserted every 250 mm in the length direction of the above.
  • Example 2 (Example corresponding to the bubble column reactor 1b in FIG. 2)
  • the reaction tube 22 eight straight tubes having an outer diameter of 19 mm, an inner diameter of 15.8 mm, and an effective length of 1.0 m were provided, and a multi-tube type bubble tower reactor 1b having a shell outer diameter of 114.3 mm was used. From under the lower tube plate of the reactor, 4.7 L / h of a raw material solution (temperature 30 ° C.) in which 15.5 wt% acetaldehyde dissolved in 0.2 wt% cobalt acetate and 84.5 wt% acetic acid were mixed as a catalyst. Supplied.
  • oxygen gas 100 vol% of 1.24 NL / min was supplied as an oxidation gas from a porous body fine bubble generating spurger (micro bubble generator 121).
  • the average bubble diameter of the fine bubbles generated at this time is about 50 ⁇ m.
  • water was flowed through the shell as a coolant.
  • the conversion rate of acetaldehyde oxidized to acetic acid was 30.2%.
  • the temperature of the production liquid was 35 ° C.
  • oxygen gas 100 vol% of 1.24 NL / min was supplied as oxygen gas from a sparger having three holes having an opening diameter of 1 mm.
  • the average bubble diameter of the bubbles generated at this time is about 5 mm.
  • water was supplied as a coolant between the outer pipe and the inner pipe.
  • oxygen gas is used as the oxidizing agent
  • air, oxygen-enriched air, or the like may be used as the oxidizing agent.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Catalysts (AREA)

Abstract

Le problème décrit par la présente invention est de fournir un réacteur dans lequel une réaction d'oxydation entre un liquide de matière première et un gaz oxydant peut être réalisée efficacement dans une condition de réaction stable. La solution selon l'invention porte sur un réacteur 1a, dans lequel une réaction d'oxydation est réalisée par mise en contact d'une matière première et d'un agent oxydant, comprend : un réservoir de réacteur 10; une unité d'alimentation en liquide de matière première 11 pour fournir un liquide de matière première contenant la matière première; une unité d'alimentation en oxygène gazeux 12 pour fournir un gaz oxydant contenant un agent oxydant; une unité de formation de fines bulles 121 qui fournit de fines bulles du gaz oxydant au liquide de matière première d'une manière distribuée; et un élément de formation de chemin d'écoulement 21 pour faire circuler de manière séparée un mélange de fluide du liquide de matière première et du gaz oxydant dans une pluralité de chemins d'écoulement 211.
PCT/JP2019/042825 2019-05-10 2019-10-31 Réacteur WO2020230348A1 (fr)

Applications Claiming Priority (2)

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JP2019-090059 2019-05-10
JP2019090059A JP2020185511A (ja) 2019-05-10 2019-05-10 反応装置

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4810449B1 (fr) * 1968-12-27 1973-04-03
JPS5018351A (fr) * 1973-06-22 1975-02-26
JP2002512211A (ja) * 1998-04-21 2002-04-23 ユニオン・カーバイド・ケミカルズ・アンド・プラスティックス・テクノロジー・コーポレイション 有機酸の製造
JP2006515558A (ja) * 2001-10-12 2006-06-01 ロディア・ポリアミド・インターミーディエッツ 液体の気体による酸化反応のための反応器
JP2008229485A (ja) * 2007-03-20 2008-10-02 Sumitomo Chemical Co Ltd 気液接触装置
JP2009512546A (ja) * 2005-10-20 2009-03-26 ビーエーエスエフ ソシエタス・ヨーロピア 機器に用いられる気液相混合物のための分配装置
JP2013515604A (ja) * 2009-12-28 2013-05-09 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 底部にガス供給装置を備える反応器
WO2017057141A1 (fr) * 2015-10-01 2017-04-06 株式会社ダイセル Catalyseur pour réaction d'oxydation, et réacteur à écoulement dans lequel est utilisé ledit catalyseur

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4810449B1 (fr) * 1968-12-27 1973-04-03
JPS5018351A (fr) * 1973-06-22 1975-02-26
JP2002512211A (ja) * 1998-04-21 2002-04-23 ユニオン・カーバイド・ケミカルズ・アンド・プラスティックス・テクノロジー・コーポレイション 有機酸の製造
JP2006515558A (ja) * 2001-10-12 2006-06-01 ロディア・ポリアミド・インターミーディエッツ 液体の気体による酸化反応のための反応器
JP2009512546A (ja) * 2005-10-20 2009-03-26 ビーエーエスエフ ソシエタス・ヨーロピア 機器に用いられる気液相混合物のための分配装置
JP2008229485A (ja) * 2007-03-20 2008-10-02 Sumitomo Chemical Co Ltd 気液接触装置
JP2013515604A (ja) * 2009-12-28 2013-05-09 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 底部にガス供給装置を備える反応器
WO2017057141A1 (fr) * 2015-10-01 2017-04-06 株式会社ダイセル Catalyseur pour réaction d'oxydation, et réacteur à écoulement dans lequel est utilisé ledit catalyseur

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