WO1998055216A1 - Reacteur pour effectuer des reactions rapides fortement exothermiques et son utilisation - Google Patents

Reacteur pour effectuer des reactions rapides fortement exothermiques et son utilisation Download PDF

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Publication number
WO1998055216A1
WO1998055216A1 PCT/EP1998/003037 EP9803037W WO9855216A1 WO 1998055216 A1 WO1998055216 A1 WO 1998055216A1 EP 9803037 W EP9803037 W EP 9803037W WO 9855216 A1 WO9855216 A1 WO 9855216A1
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WIPO (PCT)
Prior art keywords
reactor
reactor according
tubes
feed
openings
Prior art date
Application number
PCT/EP1998/003037
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German (de)
English (en)
Inventor
Reinhard Langer
Original Assignee
Bayer Aktiengesellschaft
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Filing date
Publication date
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Publication of WO1998055216A1 publication Critical patent/WO1998055216A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/30—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds
    • C07C209/32—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds by reduction of nitro groups
    • C07C209/36—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds by reduction of nitro groups by reduction of nitro groups bound to carbon atoms of six-membered aromatic rings in presence of hydrogen-containing gases and a catalyst
    • 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
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1812—Tubular reactors
    • B01J19/1837—Loop-type reactors
    • 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
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1868—Stationary reactors having moving elements inside resulting in a loop-type movement
    • B01J19/1881—Stationary reactors having moving elements inside resulting in a loop-type movement externally, i.e. the mixture leaving the vessel and subsequently re-entering it
    • 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
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/243—Tubular reactors spirally, concentrically or zigzag wound
    • 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
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/2435—Loop-type reactors
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/065—Feeding reactive fluids
    • 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
    • B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
    • B01J8/1863—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement outside the reactor and subsequently re-entering it
    • 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
    • B01J8/228—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 externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00081—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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00085—Plates; Jackets; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/185—Details relating to the spatial orientation of the reactor vertical

Definitions

  • the present invention relates to a reactor for carrying out rapid, highly exothermic reactions in the liquid phase.
  • the reactor essentially consists of a cooled tube bundle. Porous lines are installed in the tubes, via which one of the reactants is metered in, in such a way that the heat of reaction is released uniformly along the tube axis and no areas with too high a starting material concentration arise. 'The reaction medium flows through the reactor tubes in a defined manner
  • the reactor is particularly suitable for the bottom phase hydrogenation of dinitrotoluene
  • Reactors for fast, strongly exothermic conversions require an effective removal of the heat of reaction.
  • the known reactors have complex internals and are also equipped with powerful agitators in order to mix the reactants quickly and to transfer the heat released to the heat exchanger surfaces
  • Solid catalysts can also be deposited in areas of the reactor with poor flow conditions
  • the aim is to design a reactor that allows rapid, highly exothermic reactions to be carried out in a controlled manner in the vicinity of the heat exchanger surfaces and that reliably ensures a uniform flow through the entire reactor
  • the invention relates to a tube bundle reactor for rapid, strongly exothermic reactions consisting of a reactor housing with a bundle of tubes, which are optionally connected to one another radially to their length, as a reaction zone, starting material feed lines, product outlet and heat exchanger, characterized in that a starting material feed line is provided in the tubes the bundle of pipelines running and provided with a multiplicity of openings " , the openings in the pipelines being distributed over the entire length or a long section of the reaction zone
  • the reaction tubes preferably have a catalyst bed
  • the maximum pore opening cross section of the openings in the feed line is in particular 1 mm, preferably 0.7 mm
  • the minimum pore cross section of the openings in the feed line is in particular 1 ⁇ m, preferably 7 ⁇ m
  • the feed line is part of a feed loop with a conveying means, for example a circulating pump and a special heat exchanger
  • the reactor has a pumping loop for the
  • Reaction mixture with a conveying agent at least one further feed line and an outlet for the reaction product on.
  • the conveying agent is, for example, a mammoth pump or a circulating pump
  • a gas supply for gaseous reactants and, if necessary, a mixer element, in particular a static and / or dynamic mixer, are arranged in the area in front of the inlet of the bundle of reaction tubes of the reactor in order to achieve a drafty mixing with the circulating reactants
  • an adiabatic dwell zone adjoins the reaction zone formed from the tubes in the reactor. in which the reaction mixture can react further
  • a feed line for catalyst can be provided in the pumping loop if, for example, catalyst is also pumped around in a suspension in the loop.
  • the line for the reaction product is also arranged in the pumping loop.
  • the product discharge is preferably a settling tank with an outlet or particularly preferably a filtration unit, in particular a unit for cross-flow filtration
  • the invention further relates to the use of the reactor according to the invention for carrying out strongly exothermic reactions, in particular for the hydrogenation of dinitrotoluene
  • Tube bundles surrounded by heat exchangers can be used as are known in principle from the prior art, ie tube bundles containing between 10 and 100,000 tubes, preferably between 100 and 10,000 tubes with an inside diameter of 10 to 100 mm, preferably from 20 to Own 50 mm
  • the pipe length is in particular from 1 to 50 m, preferably from 2 to 20 m, particularly preferably from 3 to 10 m
  • the heat of reaction can be removed by evaporative cooling or by means of a liquid heat carrier; steam is preferably generated directly by evaporative cooling.
  • the heat carrier can move in a heat exchanger surrounding the tubes.
  • the reaction zone can be arranged in the tube-like area between a group of heat exchanger tubes. The heat carrier thus flows through a tube bundle, while the reaction takes place in the interconnected tubular spaces (type linder reactor).
  • the reaction preferably takes place in the tubes and the heat carrier is located in the heat exchanger surrounding the reaction tubes
  • Educt lines can be in contact with the heat transfer wall or are at a distance of 1 to 50 mm, preferably 2 to 25 mm. particularly preferably from 4 to 12 mm from the heat exchanger wall
  • the feed lines In cooled areas of the reactor, the feed lines have pores, in particular
  • the openings are in particular arranged at regular intervals in such a way that there is a pore of 10 to 100,000, preferably 30 to 10,000, particularly preferably 100 to 1000 ml of reaction space. Lines made of metal sintered material with a very large number of pores can also be used
  • the pressure loss when flowing through the pores is in particular such that approximately the same amount of starting material slowly flows out of all pores
  • the educt lines are preferably combined to form an educt circuit, so that there are no regions in the lines in which the educt does not flow or only flows very slowly.
  • the educt circuit also has the advantage that the educt can be cooled In order to be able to flow strongly through the reactor, the majority of the material flowing through the reactor must be returned to the reactor inlet in the preferred variant. This is done in the sense of a loop reactor in which the two ends of the reactor are connected by a line
  • a device for pumping around the contents of the reactor loop must be attached at a suitable location.
  • This can be, for example, a centrifugal pump or a propeller
  • a gas for example hydrogen
  • this gas can simply be injected in front of the tube bundle and is circulated with the liquid, the gas is preferably fed in from below, by swirling or specifically by distributing gas over the reactor tubes on the upper end of the reactor separated from the liquid and fed back to the lower end of the reactor
  • the reactor according to the invention is particularly suitable for the hydrogenation of nitroaromatics.
  • Dinitrotoluene is particularly preferably hydrogenated to toluenediamine
  • the reactor can be operated under normal pressure (ambient pressure) or under elevated pressure, the reactor in the range of 10 3 to 3 • 10 5 hPa is preferred. ⁇ particular DERS preferably from 3 to 10 3 to 10 5 hPa operated The invention is explained in more detail below with reference to the figures, without the invention being restricted thereby in detail
  • FIG. 1 shows a schematic view of the tube bundle reactor according to the invention with starting material circuit and pumping loop 10
  • FIG. 2b shows an enlarged detail from the longitudinal section through the tube 6 according to FIG. 2a to explain the arrangement of the opening 7
  • FIG. 2c shows a cross section through a reaction tube 6 according to FIG. 2a
  • FIG. 3 shows a reaction tube 6 corresponding to FIG. 2a with catalyst bed 8
  • FIG. 4a shows a schematic cross section through a tube bundle 3 according to the invention
  • 4b shows a schematic cross section of a variant of the tube bundle 3 according to the invention
  • 5a shows a schematic longitudinal section through a reactor tube 6 with an internal feed line as part of a feed circuit
  • FIG. 5b An enlarged section of Fig. 5a
  • 5c shows a cross section through the bundle tube 6 according to FIG. 5a
  • FIG. 6 shows a schematic longitudinal section through a reaction tube 6 corresponding to FIG. 5a with catalyst bed 8 7 shows a variant of the reactor arrangement according to FIG. 1 with an additional educt circuit for gaseous educts.
  • FIG. 8 shows a variant of the reactor arrangement according to FIG. 7, in which the gas supply takes place in the vicinity of the inlet of the reactor tubes
  • a bundle 3 of reaction tubes 6 is accommodated in a reactor housing 1 and is surrounded in the area of the reaction zone by a heat exchanger 5 with a condensate supply line 15 and a steam discharge line 16.
  • educt feed tubes 4a, 4b, 4c, 4d run concentrically, according to FIG. 4a.
  • the feed lines 4a to 4d are part of a feed circuit 25 in which a feed pump 14 and a heat exchanger 9 are provided.
  • the starting material consumed in the reaction is supplied via a feed pump 17.
  • the reaction tubes 6 have educt lines 4 provided with an opening in a partial area.
  • the educt flows into the reaction zone of the tube 6 through the large number of openings 7 in the educt line 4 (see FIG. 5b).
  • the reactor 1 with the tube bundle 3 is part of a pumping circuit 10 in which the reaction mixture and the further starting material fed in via the starting material feed line 11 or 11 are circulated. 1 with the help of a circulating pump 13.
  • a cross-flow filter unit 20 is also installed in the circulating circuit in order to be able to remove product obtained from the reaction from the circuit. The product is discharged via the discharge line 12.
  • a simple educt feed 4 is provided in the tubes 6 of the tube bundle instead of the educt circuit 25 instead of the educt circuit 25.
  • FIG 3 shows a schematic longitudinal section through the same arrangement, in which the length of the reaction tube 6 is filled on a catalyst bed 8.
  • FIG. 4b A variant of the arrangement of the reaction tubes 6 according to the invention is shown in FIG. 4b.
  • the spaces between heat exchanger tubes 5 form tubular spaces 6- as reaction zones in which the reactant lines 4 run to feed the reactant.
  • the tubular gaps 6'- are radial to their longitudinal expansion via gaps 27 between the heat transfer tubes 5- connected to each other when the heat exchanger tubes are spaced, as shown in Fig. 4b.
  • FIG. 5a shows a schematic longitudinal section through a reaction tube 6 from an arrangement according to FIG. 1, in which the educt feed line 4 is part of an educt circuit, but only has openings 7 on a partial region of the tube length of tube 6 (see FIG. 5b), according to FIG. 5c a concentric arrangement of the educt feed line 4 is provided
  • the tubes 6 of the tube bundle reactor 1 are provided with a catalyst bed over their entire length
  • the variant of the tube bundle reactor arrangement according to FIG. 7 is suitable for the reaction involving further gaseous starting materials.
  • the arrangement described in Example 1 according to FIG. 1 is supplemented by a further educt circuit 21 for supplying gaseous products, e.g. hydrogen gas.
  • the gas is fed to the gas circuit 21 via the feed line 22 and introduced into the pumping circuit of the reactor at the gas inlet 18 upstream of the mixer 13.
  • the gas is passed through the reaction zone of the tubes 6 with the reaction mixture circulating in the pumping circuit 10 in counterflow to the further starting materials supplied via the tubes 4 and separated from the reaction mixture in a gas separator 19.
  • the separated gas is either fed into the Process returned or at outlet 23 to
  • the inlet for the additional feed gas is attached just before or in the pipe opening of the pipes 6.
  • the gas is carried into the reaction tubes 6 by the density-dependent circulation of the reaction mixture (10) and, as in the arrangement according to FIG. 7, is fed back to the inlet of the reactor via a gas separator 19 and a circulating gas compressor 24 Example 3
  • FIG. 9 shows a simplified reactor arrangement of the tube bundle reactor according to the invention, in which a simple product outlet is provided in the pumping circuit 10 instead of the crossflow filtration provided in the arrangement according to Example 1.
  • the outlet of the reactor bundle 3 is followed by an after-reactor 26 as an adiabatic dwell in which the reaction subsides.
  • the starting materials are introduced into the pumping circuit here, as in Example 1, via open-pore pipelines 4 and via an educt feed line 11.
  • the arrangement has a stationary contact 8, or a catalyst slurry is passed through inlet 11 and outlet 12 with the catalyst being separated off for recycling
  • the reaction can also be carried out homogeneously catalyzed.
  • the catalyst with the material flows must be supplied via the pump 17 or the inlet 11.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un réacteur à faisceau de tubes (1) pour réactions rapides fortement exothermiques. Ce réacteur comprend comme zone de réaction, un caisson (2) muni d'un faisceau (3) de tubes (6) qui sont interconnectés éventuellement dans le sens radial par rapport à leur étendue longitudinale. Ce réacteur comprend également des conduits d'évacuation (4, 11), une sortie de produit (12) et un échangeur de chaleur (5). Ce réacteur se caractérise en ce que les conduits d'évacuation (4) se présentent sous forme de conduites tubulaires (4a, 4b, 4c, 4d) s'étendant dans les tubes (6) du faisceau (3) et munies d'une pluralité d'ouvertures (7) réparties dans lesdites conduites tubulaires (4a, 4b, 4c, 4d) sur toute la longueur ou sur une section longitudinale de la zone de réaction.
PCT/EP1998/003037 1997-06-04 1998-05-22 Reacteur pour effectuer des reactions rapides fortement exothermiques et son utilisation WO1998055216A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19723322.8 1997-06-04
DE1997123322 DE19723322A1 (de) 1997-06-04 1997-06-04 Reaktor zur Durchführung rascher stark exothermer Reaktionen und dessen Verwendung

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Publication Number Publication Date
WO1998055216A1 true WO1998055216A1 (fr) 1998-12-10

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001085332A1 (fr) * 2000-05-05 2001-11-15 Deggendorfer Werft Und Eisenbau Gmbh Reacteur tubulaire utilise pour des reactions exothermiques en phase gazeuse
US7109378B2 (en) 2001-08-30 2006-09-19 Air Products And Chemicals, Inc. Monolith catalytic reactor coupled to static mixer
WO2012123469A1 (fr) 2011-03-16 2012-09-20 Basf Se Dosage optimisé des éduits pour un procédé de fabrication d'amines aromatiques par hydrogénation de nitroaromates
US8835688B2 (en) 2011-03-16 2014-09-16 Basf Se Optimized introduction of the starting materials for a process for preparing aromatic amines by hydrogenation of nitroaromatics

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6977064B1 (en) * 2000-05-05 2005-12-20 Saudi Basic Industries Corporation Apparatus for the controlled optimized addition of reactants in continuous flow reaction systems
WO2006097906A1 (fr) * 2005-03-17 2006-09-21 Sasol Technology (Proprietary) Limited Production de produits liquides et eventuellement gazeux a partir de reactifs gazeux
US9068782B2 (en) 2009-03-17 2015-06-30 Dow Global Technologies Llc Tube-side sequentially pulsable-flow shell-and-tube heat exchanger appratus, system, and method
DE102010040757A1 (de) * 2010-09-14 2012-03-15 Man Diesel & Turbo Se Rohrbündelreaktor
DE102012206541A1 (de) * 2012-04-20 2013-10-24 Siemens Aktiengesellschaft Verfahren und Anordnung für die Hochtemperaturelektrolyse
DE102018113735A1 (de) * 2018-06-08 2019-12-12 Man Energy Solutions Se Verfahren, Rohrbündelreaktor und Reaktorsystem zur Durchführung katalytischer Gasphasenreaktionen

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2518583A (en) * 1945-06-27 1950-08-15 Universal Oil Prod Co Catalytic reactor
US2761768A (en) * 1952-03-18 1956-09-04 Pouderies Reunis De Belgiques Circulation nitrating apparatus
US3268299A (en) * 1961-12-27 1966-08-23 Crawford & Russell Inc Apparatus for effecting chemical reactions
GB1548277A (en) * 1971-07-30 1979-07-11 Allied Chem Process for chlorination of hydrocarbons
EP0124010A1 (fr) * 1983-04-27 1984-11-07 Bayer Ag Procédé pour la préparation en continu de diamines aromatiques avec production simultanée de vapeur

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2518583A (en) * 1945-06-27 1950-08-15 Universal Oil Prod Co Catalytic reactor
US2761768A (en) * 1952-03-18 1956-09-04 Pouderies Reunis De Belgiques Circulation nitrating apparatus
US3268299A (en) * 1961-12-27 1966-08-23 Crawford & Russell Inc Apparatus for effecting chemical reactions
GB1548277A (en) * 1971-07-30 1979-07-11 Allied Chem Process for chlorination of hydrocarbons
EP0124010A1 (fr) * 1983-04-27 1984-11-07 Bayer Ag Procédé pour la préparation en continu de diamines aromatiques avec production simultanée de vapeur

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001085332A1 (fr) * 2000-05-05 2001-11-15 Deggendorfer Werft Und Eisenbau Gmbh Reacteur tubulaire utilise pour des reactions exothermiques en phase gazeuse
US7109378B2 (en) 2001-08-30 2006-09-19 Air Products And Chemicals, Inc. Monolith catalytic reactor coupled to static mixer
US7595029B2 (en) 2001-08-30 2009-09-29 Air Products And Chemicals, Inc. Monolith catalytic reactor coupled to static mixer
WO2012123469A1 (fr) 2011-03-16 2012-09-20 Basf Se Dosage optimisé des éduits pour un procédé de fabrication d'amines aromatiques par hydrogénation de nitroaromates
US8835688B2 (en) 2011-03-16 2014-09-16 Basf Se Optimized introduction of the starting materials for a process for preparing aromatic amines by hydrogenation of nitroaromatics
US9308515B2 (en) 2011-03-16 2016-04-12 Basf Se Optimized introduction of the starting materials for a process for preparing aromatic amines by hydrogenation of nitroaromatics

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